TWI757337B - A kind of modification method and modification system of low-quality oil - Google Patents

Abstract

The present invention relates to a modification method and modification system of low-quality oil. The upgrading method comprises: (1) subjecting the low-quality oil to a conversion reaction in the presence of hydrogen and optionally in the presence of a conversion catalyst to obtain a conversion product, (2) treating the conversion product to obtain a first A treated product, wherein the first treated product contains a specific content of a specific component, and (3) the first treated product is subjected to extraction separation to obtain an upgraded oil and a residue. The upgrading method and upgrading system have the advantages of stable operation, high upgrading efficiency, green environmental protection, low coke yield or high modified oil yield.

Description

A kind of modification method and modification system of low-quality oil

The invention relates to the field of fuel chemical industry, in particular to a method for upgrading low-quality oil. The invention also relates to a corresponding upgrading system.

In recent years, the trend of low-quality fossil fuels has intensified year by year. Moreover, the output of low-quality fuel oil such as residual oil, inferior oil, shale oil, oil sands heavy oil and coal-derived oil is also increasing year by year. Such low-quality oils are characterized by high density, high viscosity, high content of heteroatoms (sulfur, nitrogen, heavy metals) or high asphaltene content. In addition, the existing processing technology (such as delayed coking) developed for this kind of low-quality oil has problems such as high coke yield, low effective utilization of energy, poor economic benefit, and unenvironmental production process. Therefore, the further development of high-efficiency and green upgrading technologies for such low-quality oils has become one of the development directions and research priorities of the petrochemical industry.

Chinese patent ZL200310104918.2 discloses a method for upgrading low-quality heavy and residual oil, wherein the heavy and residual oil is first subjected to a suspended bed to moderate hydrocracking, so that most or all of the metal impurities are freed from colloid and asphaltenes; the The hydrogenated product passes through the metal adsorption reactor with switchable operation or on-line replacement of the feed to adsorb and remove the free metal impurities in the suspended bed hydrocracking oil; the demetallized product is sent to the residual oil fixed bed hydrotreating unit for deep hydrogenation removal. Other impurities, to produce high-quality heavy oil catalytic cracking raw materials.

The inventors of the present invention have found a novel method and system for upgrading low-quality oil through assiduous research, and thus completed the present invention.

Specifically, the present invention relates to the following aspects.

1. an upgrading method is characterized in that, comprising the following steps: (1) make low-quality oil as upgrading raw material in the presence of hydrogen and optionally in the presence of a conversion catalyst to carry out a conversion reaction to obtain a conversion product, (2) ) processing the conversion product (such as component formulation or component separation) to obtain a first processed product, wherein the first processed product comprises a content of from 20 wt % to 60 wt % (preferably from 25 wt % to 25 wt %) 55% by weight, based on the total weight of the first treated product) having a boiling point or boiling range between 350°C and 524°C (preferably between 355°C and 500°C, such as between 380°C and 524°C) (in particular, at least one hydrocarbon optionally containing heteroatoms), and (3) extracting and separating the first treated product to obtain an upgraded oil and residue, the upgrading method optionally further comprises the following step: (4) recycle all or a part of the residue (such as more than 80% by weight, preferably more than 90% by weight, more preferably at least 95% by weight) to the step (1).

2. The upgrading method according to the aforementioned aspect 1, wherein the step (2) comprises one or more of the following steps: (2-1) Carrying out the conversion product at a first pressure and a first temperature Separating to obtain a gas component and a liquid component, (2-2) separating the liquid component at a second pressure and a second temperature to obtain a second separation product and a first separation product, wherein the separation allows The first isolated product comprises a boiling point or boiling range between 350° C. and 524° C. in an amount of from 20% to 60% by weight (preferably from 25% to 55% by weight, based on the total weight of the first isolated product) (preferably between 355°C and 500°C, such as between 380°C and 524°C, or between 400°C and 500°C) components (in particular at least optionally containing heteroatoms) (2-3) Optionally, separate the second separated product to obtain a hydrocarbon Naphtha and atmospheric gas oil, and (2-4) optionally, recycling said gaseous components to said step (1), wherein said first pressure is greater than said second pressure, preferably said The first pressure is from 4 MPa to 24 MPa greater than the second pressure, more preferably the first pressure is from 7 MPa to 19 MPa greater than the second pressure.

3. The upgrading method according to any one of the aforementioned aspects 1-2, wherein the step (3) comprises one or more of the following steps: (3-1) making the first separated product or the The first treated product is contacted (preferably countercurrently) with a solvent at a third pressure and a third temperature to obtain the upgraded oil and the residue, (3-2) optionally, subjecting the upgraded oil to Hydrotreating to obtain an upgraded oil after hydrogenation, (3-3) Optionally, subjecting the upgraded oil to hydrocracking to obtain a hydrocracking product, and then separating the hydrocracking product into dry gas, liquefied gas, aviation Kerosene, diesel oil and hydrogenated tail oil, (3-4) optionally, catalytically cracking the hydrogenated upgraded oil to obtain a first catalytic cracking product, and then separating the first catalytic cracking product into dry gas, Liquefied gas, gasoline, circulating oil and oil slurry, (3-5) Optionally, catalytic cracking of the hydrogenated reformed oil and the atmospheric gas oil is combined to obtain a second catalytic cracking product, and then the The second catalytic cracking product is separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, (3-6) optionally, catalytic cracking is carried out in combination with the hydrogenated upgraded oil and the second separation product , obtain the third catalytic cracking product, then separate the third catalytic cracking product into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, (3-7) Optionally, the atmospheric gas oil is subjected to Hydrotreating to obtain diesel oil, (3-8) Optionally, hydrotreating the circulating oil obtained in any step of the upgrading method alone or in combination with the upgrading oil to obtain a hydrotreating oil, (3) -9) optionally, catalytically cracking the hydrotreated oil in combination with the second separation product to obtain a fourth catalytic cracking product, and then separating the fourth catalytic cracking product into dry gas, liquefied gas, gasoline , circulating oil and oil slurry, (3-10) Optionally, circulating the oil slurry and/or externally supplied oil slurry obtained in any step of the upgrading method to the step (1), the step (2) and/or the step (3), or (3-11) optionally, the liquefied gas obtained in any step of the upgrading method is recycled to the step (3) or the step (3-1).

4. The upgrading method according to any one of the aforementioned aspects 1-3, wherein the reaction conditions of the conversion reaction include: the partial pressure of hydrogen is from 10.0 MPa to 25.0 MPa, preferably from 13.0 MPa to 20.0 MPa, and the reaction temperature is From 380°C to 470°C, preferably from 400°C to 440°C, the volumetric space velocity of the upgraded raw material is from 0.01h ^-1 to 2.0h ^-1 , preferably from 0.1h ^-1 to 1.0h ^-1 , hydrogen and The volume ratio of the upgraded raw materials is from 500 to 5000, preferably from 800 to 2000, optionally in the presence of a conversion catalyst.

5. The upgrading method according to any one of the preceding aspects 1-4, wherein the first pressure is from 10.0 MPa to 25.0 MPa, preferably from 13.0 MPa to 20.0 MPa, and the first temperature is from 380° C. to 470°C, preferably from 400°C to 440°C, or the second pressure is from 0.1MPa to 5.0MPa, preferably from 0.1MPa to 4.0MPa, and the second temperature is from 150°C to 390°C, preferably from 200°C °C to 370 °C.

6. The upgrading method according to any one of the aforementioned aspects 1-5, wherein the solvent is one or more of C _3-7 hydrocarbons, preferably selected from C _3-5 alkanes and C _3-5 alkenes One or more, such as one or more selected from C _3-4 alkanes and C _3-4 alkenes, and the weight ratio of the solvent to the first separated product or the first processed product is 1-7: 1, preferably 1.5-5:1.

7. The upgrading method according to any one of the preceding aspects 1-6, wherein the third pressure is from 3MPa to 12MPa, preferably from 3.5MPa to 10MPa, and the third temperature is from 55°C to 300°C , preferably from 70°C to 220°C.

8. The upgrading method according to any one of the aforementioned aspects 1-7, wherein the reaction conditions of the step (3-2) or the step (3-8) comprise: the partial pressure of hydrogen is from 5.0 MPa to 20.0 MPa, preferably from 8.0MPa to 15.0MPa, the reaction temperature is from 330°C to 450°C, preferably from 350°C to 420°C, the volumetric space velocity of the raw oil is from 0.1h ^-1 to 3.0h ^-1 , preferably from 0.3h ^-1 to 1.5h ^-1 , the volume ratio of hydrogen to raw oil is from 300 to 3000, preferably from 800 to 1500, in the presence of a hydrogenation catalyst; or, the reaction conditions of the step (3-3) include: hydrogen The partial pressure is from 10.0MPa to 20.0MPa, the reaction temperature is from 310°C to 420°C, the volume space velocity of the reformed oil is from 0.3h ^-1 to 1.2h ^-1 , the volume of hydrogen and the reformed oil is The ratio is from 600 to 1500, in the presence of a hydrocracking catalyst; or, the step (3-4), the step (3-5), the step (3-6) or the step (3- 9) The reaction conditions include: the reaction temperature is from 450°C to 650°C, preferably from 480°C to 560°C, the reaction pressure is from 0.15MPa to 0.4MPa, and the reaction time is from 0.1 seconds to 10 seconds, preferably from 0.2 seconds to 0.2 seconds. 4 seconds, the weight ratio of the cracking catalyst to the feedstock oil is from 3 to 30, preferably from 5 to 15, and the weight ratio of the water vapor to the feedstock oil is from 0.05 to 0.6, preferably from 0.05 to 0.4, in the presence of the cracking catalyst; Alternatively, the reaction conditions of the step (3-7) include: the hydrogen partial pressure is from 7.0MPa to 15.0MPa, the reaction pressure is from 8MPa to 12MPa, and the reaction temperature is from 340°C to 400°C; the normal pressure gas oil The volumetric space velocity is from 0.6 h ^-1 to 1.5 h ^-1 , and the volume ratio of hydrogen to the atmospheric gas oil is from 500 to 800, in the presence of a hydrogenation catalyst.

9. The upgrading method according to any one of the preceding aspects 1-8, wherein the softening point of the residue is less than 150°C.

10. The upgrading method according to any one of the preceding aspects 1 to 9, wherein the low-quality oil comprises one or more of asphaltenes, asphaltenes and pre-asphaltenes, especially asphaltenes, preferably selected from low-quality oils One or more of oil, deoiled bitumen, heavy oil, heavy oil, coal-derived oil, shale oil and petrochemical waste oil, preferably, the heavy oil is selected from topping crude oil, heavy oil obtained from oil sands bitumen and initial boiling point One or more kinds of heavy oil above 350°C, the coal-derived oil is selected from one or more of coal liquefied oil produced by coal liquefaction and coal tar produced by coal pyrolysis, or, the petrochemical waste oil is selected from petrochemical waste One or more of oil sludge, petrochemical residues and their refined products.

11. The upgrading method according to any one of the preceding aspects 1-10, wherein the initial boiling point of the first isolated product or the first processed product is greater than or equal to 330°C, or the first isolated product Or the first processed product further comprises light components with a boiling point or a boiling range less than or equal to 350°C, alternatively, the first separated product or the first processed product further comprises a boiling point or a boiling range greater than 500°C (preferably greater than 500°C). 524°C), preferably the heavy component comprises one or more of asphaltenes, asphaltenes and pre-asphaltenes, especially asphaltenes.

12. The upgrading method according to any one of the preceding aspects 1-11, wherein the step (2) obtains, in addition to the first treatment product, one or more second treatment products, the second treatment product. The treated product, or any of its components, has an end point of less than or equal to 350°C.

13. An upgrading system, characterized in that it comprises a conversion reaction unit, a conversion product treatment unit, a first control unit, an extraction separation unit and an optional residue treatment unit, wherein the conversion reaction unit is configured to enable low-quality The oil undergoes a conversion reaction in the presence of hydrogen and optionally a conversion catalyst, and outputs the conversion product obtained, the conversion product processing unit being configured to be able to process the conversion product (such as component formulation or separation) ), and output the obtained first processed product, the first control unit is configured to be able to control the operating conditions (such as operating temperature and/or operating pressure) of the conversion product processing unit, so that the first processed product It contains a boiling point or boiling range between 350°C and 524°C (preferably between 350°C and 524°C) in an amount of from 20% to 60% by weight (preferably from 25% to 55% by weight, based on the total weight of the first treated product). between 355°C and 500°C, such as between 380°C and 524°C, or between 400°C and 500°C) (in particular at least one hydrocarbon optionally containing heteroatoms), said The extraction and separation unit is configured to be able to extract and separate the first processed product, and output the obtained upgraded oil and the residue respectively, and the residue treatment unit is configured to be capable of removing all or a part of the residue (such as greater than 80% by weight, preferably more than 90% by weight, more preferably at least 95% by weight) is delivered to the conversion reaction unit.

14. The upgrading system of the preceding aspect 13, wherein the conversion product processing unit comprises a first conversion product separation unit, a second conversion product separation unit, an optional second separation product separation unit, and an optional gas set A portion delivery unit, the first conversion product separation unit is configured to separate the conversion product and output the obtained gas component and liquid component, respectively, and the second conversion product separation unit is configured to be capable of separating The liquid components are separated, and the obtained second separated product and the first separated product are respectively output, and the second separated product separation unit is configured to be able to separate the second separated product and output the obtained separately. Naphtha and atmospheric gas oil, and the gaseous component delivery unit is configured to deliver the gaseous component to the conversion reaction unit.

15. The upgrading system according to any of the preceding aspects 13-14, further comprising a second control unit and a third control unit, wherein the second control unit is arranged to be able to control the first conversion product separation unit the operating pressure (preferably the outlet pressure of the gas components), the third control unit is arranged to be able to control the operating pressure (preferably the outlet pressure of the second separated product) of the second conversion product separation unit, and such that the The operating pressure of the first conversion product separation unit is greater than the operating pressure of the second conversion product separation unit, and preferably, the third control unit is configured to be capable of controlling the operating conditions of the second conversion product separation unit ( such as operating temperature and/or operating pressure) such that the first isolated product comprises a content of from 20 to 60 wt % (preferably from 25 to 55 wt %, based on the total weight of the first isolated product) A group whose boiling point or boiling range is between 350°C and 524°C (preferably between 355°C and 500°C, such as between 380°C and 524°C, or between 400°C and 500°C) (particularly at least one hydrocarbon optionally containing heteroatoms) and such that the second isolated product or any component thereof has an end boiling point less than or equal to 350°C.

16. The upgrading system according to any of the preceding aspects 13-15, wherein the extractive separation unit is arranged to be capable of contacting the first separation product or the first treatment product with a solvent (preferably countercurrent contacting) ), and output the obtained modified oil and the residue respectively.

17. The upgrading system according to any one of the preceding aspects 13 to 16, further comprising one or more of the following units: a first hydrogenation unit configured to be capable of hydrotreating the upgraded oil and outputting The obtained post-hydrogenation upgraded oil, the second hydrogenation unit, is arranged to be able to hydrocracking said upgraded oil and to separate the obtained hydrocracking product into dry gas, liquefied gas, aviation kerosene, diesel oil and hydrogenated tails oil, a first catalytic cracking unit, configured to be capable of catalytically cracking the hydrogenated upgraded oil, and separating the obtained first catalytic cracking product into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, The second catalytic cracking unit is configured to be able to jointly carry out catalytic cracking of the hydrogenated reformed oil and the atmospheric gas oil, and separate the obtained second catalytic cracking product into dry gas, liquefied gas, gasoline, Circulating oil and oil slurry, a third catalytic cracking unit, configured to be capable of catalytically cracking the hydrogenated upgraded oil in combination with the second separation product, and separating the obtained third catalytic cracking product into dry gas , liquefied gas, gasoline, circulating oil and oil slurry, the third hydrogenation unit is arranged to be capable of hydrotreating the atmospheric gas oil and output the obtained diesel oil, and the fourth hydrogenation unit is arranged to be capable of hydrogenating the said atmospheric gas oil The circulating oil obtained by any unit of the reforming system is hydrotreated in combination with the reforming oil, and the obtained hydrotreated oil is output, and a fourth catalytic cracking unit is arranged to be able to combine the hydrotreated oil with the hydrotreated oil. The second separation product is combined for catalytic cracking, and the obtained fourth catalytic cracking product is separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry. The oil slurry and/or externally supplied oil slurry obtained by any one of the units is transported to the conversion reaction unit, the conversion product processing unit and/or the extraction separation unit, or the liquefied gas delivery unit, and is configured to be able to The liquefied gas obtained by any unit of the upgrading system is sent to the extraction and separation unit.

technical effect

According to the reforming method and reforming system of the present invention, at least one of the following technical effects can be achieved, or in a preferred case, at least two or more of the following technical effects can be achieved simultaneously.

(1) The three wastes are less discharged, almost no solid coke is produced, and the production process is green and environmentally friendly.

(2) The low-quality oil can be upgraded with high efficiency and maximum amount into an upgraded oil rich in saturated structure, substantially free of heavy metals, and substantially free of asphaltenes. Here, in a preferred case, the conversion rate of the low-quality oil is generally greater than 90% by weight, preferably greater than 95% by weight, and the content of heavy metals (calculated as Ni+V) in the modified oil is generally less than 10 μg/ g, preferably less than 1 μg/g, and the content of asphaltenes in the modified oil is generally less than 2.0% by weight, preferably less than 0.5% by weight.

(3) The operational stability of the upgrading process (especially the extraction and separation step) can be improved, and the operation period of the upgrading method or the upgrading system can be significantly prolonged.

(4) A high yield of modified oil can be obtained. Here, in a preferred case, the highest yield of the upgraded oil can reach 88%.

(5) A low yield of toluene insoluble matter can be obtained. Here, in a preferred case, the minimum yield of toluene insoluble matter can reach 0.5%.

(6) The obtained modified oil can be further processed to produce high-quality aviation kerosene meeting the national standard, high-octane gasoline or high-quality diesel fuel meeting the national VI index. Here, in a preferred case, the yield of high-octane gasoline is generally greater than 50% by weight, or the yield of high-quality aviation kerosene is generally greater than 35% by weight, etc.

1-6,8,10-12,14-15,17-20‧‧‧Pipeline

7‧‧‧Conversion reaction unit

9‧‧‧First conversion product separation unit

13‧‧‧Second conversion product separation unit

16‧‧‧Extraction and separation unit

21‧‧‧First hydrogenation unit (Fig. 2)/Pipeline (Fig. 3-4)

22‧‧‧Upgraded oil after hydrogenation (Figure 2)/Pipeline (Figure 3-4)

23,25,27,29-33‧‧‧Pipeline (Figure 3)

24‧‧‧The third hydrogenation unit (Figure 3)/Pipeline (Figure 4)

26‧‧‧The third hydrogenation unit (Fig. 3)/Pipeline (Fig. 4)

28‧‧‧ Fractionation system (Fig. 3)/Pipeline (Fig. 4)

20‧‧‧Fourth Hydrogenation Unit (Figure 4)/Pipeline (Figure 1)

23‧‧‧Fourth Catalytic Cracking Unit (Figure 4)/Pipeline (Figure 3)

Figure 1 schematically illustrates a method for upgrading low-quality oil according to one embodiment of the present invention.

Figure 2 schematically illustrates a method for upgrading low-quality oil according to another embodiment of the present invention.

Figure 3 schematically illustrates a method for upgrading low-quality oil according to another embodiment of the present invention.

Figure 4 schematically illustrates a method for upgrading low-quality oil according to another embodiment of the present invention.

The specific embodiments of the present invention will be described in detail below, but it should be noted that the protection scope of the present invention is not limited by these specific embodiments, but is determined by the scope of the patent application in the appendix.

All publications, patent applications, patents and other references mentioned in this specification are incorporated herein by reference in their entirety. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings conventionally understood by those skilled in the art. In case of conflict, the definitions in this specification will control.

When this specification uses the prefixes "traditionally used in the art", "traditionally known in the art", or similar expressions to refer to materials, substances, methods, steps, means or components, etc., the items cited by the prefixes cover the scope of this application. are conventionally used or known in the art at the time, but also include those not commonly used or generally known at present, but which would become known in the art to be suitable for similar purposes.

In the context of the invention of the present application, the term "asphaltene" must be understood in its usual meaning in the field of fuel chemical industry. For example, the toluene-soluble, n-hexane-insoluble substances in the oil are generally referred to as asphaltenes.

In the context of the invention of the present application, the term "pre-asphaltene" must be understood in the usual sense in the field of fuel chemical industry. For example, tetrahydrofuran-soluble, toluene-insoluble substances in oil are generally referred to as pre-asphaltenes.

In the context of the invention of the present application, the term "asphaltene" must be understood in its usual meaning in the field of fuel chemical industry. For example, substances that are insoluble in non-polar small-molecule n-alkanes (such as n-pentane or n-heptane) and soluble in benzene or toluene are generally referred to as asphaltenes in oil.

In the context of the present invention, the term "petroleum oil" generally refers to various oils used as raw materials or manufactured as products in the fuel chemical industry, including fossil fuels, fuel oils, and processed fossil fuel products (such as diesel and kerosene, etc. ), waste oil or waste residue, etc.

In the context of the invention of the present application, the term "low quality oil" refers to any oil in the field of fuel chemical industry for which upgrading is required. Specific examples of the oil include low-quality fossil fuel, low-quality fuel oil, low-quality fossil fuel processed products (eg, low-quality gasoline and diesel), fossil fuel processing waste oil or waste residue, and the like. As the upgrading requirements, for example, chemical reactions can be used to change the molecular structure of one or more components in the oil to obtain fuel chemical products such as gasoline, diesel, kerosene, liquefied gas, and naphtha. As said component, an aromatic component, an asphaltene, etc. are mentioned especially.

In the context of the invention of the present application, the term "poor oil" must be understood in the usual sense in the field of fuel chemical industry. For example, it will generally meet the requirements selected from the group consisting of API degree less than 27, sulfur content greater than 1.5 wt%, TAN (total acid number) greater than 1.0 mgKOH/g, distillation range greater than 500°C, asphaltene content greater than 10 wt% and heavy metals (with The oil whose Ni+V content is more than 100 μg /g in any one or more indexes is called inferior oil.

In the context of the invention of the present application, the term "residue" must be understood in the usual sense in the field of fuel chemical industry. For example, the bottom distillate obtained by the distillation of crude oil at atmospheric and vacuum is generally referred to as residual oil. For further example, the atmospheric bottoms are generally referred to as atmospheric residues (generally the fractions with a boiling point greater than 350°C), or the vacuum bottoms are generally referred to as vacuum residues (generally It is a fraction with a boiling point greater than 500°C or 524°C).

In the context of the invention of the present application, the term "cycle oil" must be understood in the usual sense in the field of fuel chemical industry. For example, a fraction with a distillation range between 205°C and 350°C (also known as a diesel fraction) or a fraction with a distillation range between 343°C and 500°C (also known as a diesel fraction) is generally obtained from a catalytic cracking process. Called heavy cycle oil) is called circulating oil.

In the context of the present invention, the bottom oil obtained from the fractionation step of the cracking process, after being separated by the settler, the product discharged from the upper part of the settler is generally called clarified oil, and the product discharged from the bottom of the settler is generally called oil pulp.

In the context of the invention of the present application, the term "heavy oil" must be understood in its usual meaning in the field of fuel chemical industry. For example, the distillate oil or residual oil with a boiling point above 350°C is generally referred to as heavy oil. For further example, distillate oil generally refers to the distillate products obtained by atmospheric distillation and vacuum distillation of crude oil or secondary processed oil, such as heavy diesel oil, heavy gas oil, lubricating oil fraction or cracking feedstock, etc. .

In the context of the invention of the present application, the term "heavy oil" must be understood in the usual sense in the field of fuel chemical industry. For example, crude oil with high asphaltene and gum content and high viscosity is generally referred to as heavy oil. For a further example, crude oil with a density greater than 0.943 at 20°C on the ground and a viscosity greater than 50 centimeters underground is generally called heavy oil.

In the context of the invention of the present application, the term "deoiled bitumen" must be understood in the usual sense in the field of fuel chemical industry. For example, it generally refers to the raffinate rich in asphaltenes and rich in aromatic components obtained by contacting, dissolving and separating, and extracting the bottom of the tower in the solvent deasphalting unit of the raw material oil. According to the different types of solvents, it can be divided into propane deoiled asphalt, butane deoiled asphalt, pentane deoiled asphalt, etc.

In the context of the invention of the present application, the term "topping crude oil" must be understood in the usual sense in the field of fuel chemical industry. For example, when crude oil is fractionated in the atmospheric and vacuum distillation process, the oil discharged from the bottom of the preliminary distillation column or the bottom of the flash column is generally called top oil.

In the context of the invention of the present application, the term "coal-derived oil" must be understood in the usual sense in the field of fuel chemical industry. For example, the liquid fuel obtained by chemical processing with coal as the raw material is generally called coal-derived oil.

In the context of the invention of the present application, the term "shale oil" must be understood in the usual sense in the field of fuel chemical industry. For example, the brown viscous paste obtained when kerogen shale is retorted at low temperature is generally called shale oil, which has a pungent odor and high nitrogen content.

In the context of the invention of the present application, the term "separation" generally refers to physical separation, such as extraction, liquid separation, distillation, evaporation, flash boiling, condensation, etc., unless otherwise specified or inconsistent with the conventional understanding of those skilled in the art .

In the context of the present invention, boiling point, boiling range (sometimes also referred to as distillation range), final boiling point and initial boiling point or similar parameters refer to values at normal pressure (101325 Pa).

All percentages, parts, ratios, etc. mentioned in this specification are based on weight unless otherwise specified, unless the traditional understanding of those skilled in the art is not in accordance with the weight.

It should be noted that two or more aspects (or embodiments) disclosed in the context of this specification can be combined with each other arbitrarily, and the technical solutions (such as methods or systems) formed thereby belong to the original disclosure content of this specification. part, and also fall within the protection scope of the present invention.

According to the present invention, it first relates to a modification method. Here, the modification method includes at least step (1), step (2) and step (3).

Step (1): The low-quality oil is subjected to a conversion reaction in the presence of hydrogen to obtain a conversion product (hereinafter this step is referred to as a raw material conversion step). At this time, the low-quality oil is used as the raw material for upgrading.

According to one aspect of the present invention, in the step (1), in order to make one or more of the technical effects described in the present invention more significant, the low-quality oil may contain asphaltenes, may contain asphaltenes, Pre-asphaltene may be included, or two or more of asphaltenes, asphaltenes, and pre-asphaltene may be included, especially asphaltenes and/or pre-asphaltene. One of these low-quality oils may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. The present invention does not intend to specify the specific content of the asphaltene, the asphaltene or the pre-asphaltene in the low-quality oil, as long as it is judged as "contained" according to the traditional understanding of those skilled in the art , but for the convenience of understanding, the content is generally at least 0.5% by weight or more.

According to an aspect of the present invention, in the step (1), as the low-quality oil, specific examples include low-quality oil, deoiled asphalt, heavy oil, heavy oil, coal-derived oil, shale oil, and petrochemical waste oil. . More specifically, examples of the heavy oil include topping crude oil, heavy oil obtained from oil sand bitumen, and heavy oil having an initial boiling point higher than 350°C. In addition, specific examples of the coal-derived oil include coal liquefied oil produced by liquefaction of coal and coal tar produced by pyrolysis of coal. In addition, specific examples of the petrochemical waste oil include petrochemical waste sludge, petrochemical oil residue, and refined products thereof. One of these low-quality oils may be used alone, or a plurality of them may be used in combination in an arbitrary ratio.

According to one aspect of the present invention, in the step (1), as the conversion reaction (also referred to as hydrothermal conversion reaction), it can be carried out in any manner known in the art, and is not particularly limited. In addition, the transformation reaction can be carried out in any transformation reaction apparatus known in the art, such as a thermal transformation reactor, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (1), the hydrogen partial pressure can be selected with reference to the tradition in the art, but is generally from 10.0 MPa to 25.0 MPa, preferably from 13.0 MPa to 20.0 MPa.

According to one aspect of the present invention, in the step (1), the reaction temperature can be selected with reference to the traditional in the art, but is generally from 380°C to 470°C, preferably from 400°C to 440°C.

According to an aspect of the present invention, in the step (1), the volumetric space velocity of the upgraded raw material (such as the low-quality oil) can be selected with reference to the traditional method in the field, but is generally from 0.01h ⁻¹ to 2.0h ^-1 , preferably from 0.1h ^-1 to 1.0h ^-1 .

According to one aspect of the present invention, in the step (1), the volume ratio of hydrogen to the upgraded raw material (such as the low-quality oil) can be selected with reference to the traditional choices in the field, but generally from 500 to 5000, Preferably from 800 to 2000.

According to one aspect of the present invention, in the step (1), the conversion reaction may be carried out in the presence of a conversion catalyst, or may not be carried out in the presence of a conversion catalyst. Here, as the reforming catalyst, for example, any reforming catalyst conventionally used for this purpose in the art can be cited, or it can be produced according to any production method conventionally known in the art, and is not particularly limited. Specifically, examples of the reforming catalyst include bulk-type reforming catalysts, and more specifically, compounds of metals from Group VB of the periodic table, compounds of metals from Group VIB of the periodic table, and Compounds of Group VIII metals, and the like, particularly Mo compounds, W compounds, Ni compounds, Co compounds, Fe compounds, V compounds, Cr compounds, and the like. These compounds may be used alone or in combination of two or more in arbitrary ratios. In addition, as the amount of the conversion catalyst, based on the total weight of the reformed raw material (such as the low-quality oil), it is generally from 10 μg/g to 50000 μg/g, preferably from 30 μg/g to 25000 μg/g .

Step (2): The conversion product is processed to obtain a first processed product (hereinafter referred to as the conversion product processing step).

According to one aspect of the present invention, in the step (2), the treatment can be performed in any manner known in the art, as long as the conversion product can contain a content of from 20 to 20 after the treatment. % by weight to 60% by weight (hereinafter referred to as specific content) components with a boiling point or a boiling range between 350 ° C and 524 ° C (hereinafter referred to as special components) are sufficient, thereby obtaining the first processed product . Here, as the treatment, for example, adding a predetermined amount of the special component to the conversion product or reducing a predetermined amount from the conversion product, so that the finally obtained first treatment product contains the A method for a specific content of the special component (hereinafter referred to as a component formulation method), or, the conversion product is subjected to component separation, so that the finally obtained first treatment product contains the specific content of the A special component method (hereinafter referred to as a component separation method).

According to one aspect of the present invention, in the step (2), by making the first treated product contain the specific component in the specific content, at least the efficiency of the upgrading process (especially the extraction and separation step) can be improved. Operational stability. Here, as the specific content, it is generally from 20% by weight to 60% by weight, preferably from 25% by weight to 55% by weight, based on the total weight of the first processed product.

According to one aspect of the present invention, in the step (2), the boiling point or boiling range of the special component may further be between 350°C and 524°C, such as between 380°C and 524°C, Or between 400°C and 500°C.

According to one aspect of the present invention, in the step (2), the special component is derived from petrochemical oil, and is generally a hydrocarbon, especially a mixture of multiple hydrocarbons. Here, the hydrocarbon refers to a compound basically composed of carbon atoms and hydrogen atoms, but may further contain hetero atoms such as O, N, P, Cl, or S in the molecular structure thereof. The present invention does not intend to clarify the specific chemical structure of the specific component, as long as its content and boiling point (or boiling range) satisfy any of the aforementioned corresponding provisions in this specification. Moreover, the special component can be purchased from the market, and can also be manufactured by a simple method, as long as it belongs to petrochemical oil (especially the hydrocarbon or the hydrocarbon mixture), and the boiling point (or boiling range) satisfies the present Any one of the above-mentioned corresponding provisions of the specification is sufficient. In view of this, as its source, the special component can be directly derived from the conversion product since it is usually contained in the conversion product as a constituent component. Alternatively, the special component may also be derived from the upgraded raw material or the petrochemical oil obtained in any step of the upgrading method described in this specification, especially from the residue and oil slurry described in the following description of this specification, etc. . Furthermore, as a method for producing the special component, for example, distilling the petrochemical oil, and leaving a fraction whose boiling point (or boiling range) satisfies any of the corresponding provisions in this specification, the special component can be obtained. Component. In addition, as a method for measuring the specific content of the special component, for example, the first treated product can be distilled, and all the boiling points (or boiling ranges) that satisfy any one of the corresponding provisions in this specification are reserved. Fraction, the percentage of the fraction in the total weight of the first processed product is taken as the specific content.

According to one aspect of the present invention, in the step (2), the initial boiling point of the first processed product is generally greater than or equal to 300°C, such as greater than or equal to 330°C, further such as greater than or equal to 350°C.

According to one aspect of the present invention, in the step (2), in addition to the special components, the first treated product may further include light components with a boiling point or a boiling range of less than or equal to 350°C. The present invention does not intend to specify the specific content of the light component in the first processed product, but for example, the content of the light component may be from 1 wt % to 10 wt %, based on the total weight of the first treated product.

According to one aspect of the present invention, in the step (2), in addition to the special components, the first processed product may further comprise a recombination with a boiling point or a boiling range greater than 500°C (preferably greater than 524°C). share. Here, the so-called "boiling point or boiling range greater than 500°C" means that the heavy component exhibits a boiling point or boiling range greater than 500°C, but also includes that the heavy component is thermally decomposed at a temperature greater than 500°C. No indication of boiling point or boiling range. In addition, in order to make one or more of the technical effects described in the present invention more significant, in a preferred case, the heavy component contains asphaltene, asphaltene, pre-asphaltene or a combination thereof as a constituent, especially Asphaltene is contained as a constituent. The present invention does not intend to specify the specific content of the heavy component in the first processed product, but for example, the content of the heavy component may be the balance, based on the total weight of the first processed product .

According to one aspect of the present invention, in the step (2), in addition to the special component and the light component, the first processed product may further contain a boiling point or a boiling range greater than 500° C. (preferably greater than 524°C). Here, the so-called "boiling point or boiling range greater than 500°C" means that the heavy component exhibits a boiling point or boiling range greater than 500°C, but also includes that the heavy component is thermally decomposed at a temperature greater than 500°C. No indication of boiling point or boiling range. In addition, in order to make one or more of the technical effects described in the present invention more significant, in a preferred case, the heavy component contains asphaltene, asphaltene, pre-asphaltene or a combination thereof as a constituent, especially Asphaltene is contained as a constituent. The present invention does not intend to specify the specific content of the heavy component in the first processed product, but for example, the content of the heavy component may be the balance, based on the total weight of the first processed product .

According to one aspect of the present invention, in the step (2), in addition to the first treatment product, it is also possible to obtain one or more second treatment products. Here, the second process product or any component thereof exhibits an end point of less than or equal to 350°C.

According to an aspect of the present invention, in the step (2), as the component separation method, specific examples include evaporation, distillation, and flash boiling. These component separation methods can be performed in any manner conventionally known in the art as long as it can finally obtain the first processed product. More specifically, as the component separation method, for example, a separation method including step (2-1) and step (2-2) can be mentioned.

Step (2-1): The conversion product is separated at a first pressure and a first temperature to obtain a gas component and a liquid component.

According to one aspect of the present invention, in the step (2-1), as the separation, it can be carried out according to any method and any manner known in the art, such as distillation, fractional distillation, and flash boiling, etc., Especially distillation. In addition, the separation can be carried out in any separation device known in the art, such as a distillation column, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (2-1), the gas component is generally rich in hydrogen, or the gas component is mainly composed of hydrogen. Here, the present invention does not intend to specify the specific content of hydrogen in the gas component, but as an example, the content of hydrogen is generally at least 85% by weight or more. According to need, the gas component may be recycled to the step (1) as hydrogen to participate in the conversion reaction. Also, for example, when the separation is performed using a pressurized distillation column or the like, the gaseous component represents the overhead fraction and the liquid component represents the bottoms fraction.

According to one aspect of the present invention, in the step (2-1), the first pressure is generally from 10.0 MPa to 25.0 MPa, preferably from 13.0 MPa to 20.0 MPa. Here, for the convenience of measurement, the first pressure generally refers to the pressure of the gas component, or in other words, when the separation device is used for the separation, the first pressure generally refers to The outlet pressure of the gas component as it leaves the separation device.

According to one aspect of the present invention, in the step (2-1), the first temperature is generally from 380°C to 470°C, preferably from 400°C to 440°C. Here, for the convenience of measurement, the first temperature generally refers to the temperature of the liquid component, or in other words, when the separation device is used for the separation, the first temperature generally refers to The outlet temperature of the liquid component as it leaves the separation device.

Step (2-2): separating the liquid components at a second pressure and a second temperature to obtain a second separated product and a first separated product.

According to one aspect of the present invention, in the step (2-2), as the separation, it can be carried out according to any method and any manner known in the art, for example, distillation and fractional distillation can be mentioned, especially the conventional Pressurized or pressurized distillation. In addition, the separation can be carried out in any separation device known in the art, such as an atmospheric distillation tank or a pressurized distillation column, which can be reasonably selected by those skilled in the art.

According to an aspect of the present invention, in the step (2-2), the second pressure is generally from 0.1 MPa to 5.0 MPa, preferably from 0.1 MPa to 4.0 MPa. Here, for the convenience of measurement, the second pressure generally refers to the pressure of the second separation product, or in other words, when the separation device is used for the separation, the second pressure generally refers to is the outlet pressure at which the second separation product leaves the separation device.

According to an aspect of the present invention, in the step (2-2), the second temperature is generally from 150°C to 390°C, preferably from 200°C to 370°C. Here, for the convenience of measurement, the second temperature generally refers to the temperature of the first separation product, or in other words, when a separation device is used for the separation, the second temperature generally refers to is the outlet temperature of the first separation product as it leaves the separation device.

According to one aspect of the present invention, in order to make one or more of the technical effects described in the present invention more pronounced, the first pressure is generally greater than the second pressure, preferably the first pressure is greater than the second pressure The pressure is greater from 4 MPa to 24 MPa, more preferably the first pressure is greater than the second pressure from 7 MPa to 19 MPa.

According to an aspect of the present invention, in the step (2-2), in order to make one or more of the technical effects described in the present invention more significant, after the separation, the finally obtained first An isolated product contains components with a boiling point or a boiling range between 350°C and 524°C (hereinafter referred to as special components) in an amount of from 20 wt % to 60 wt % (hereinafter referred to as specific contents), while the The second isolated product, or any of its components, has an end boiling point less than or equal to 350°C.

According to one aspect of the present invention, in the step (2-2), the specific content of the special component is generally from 20% by weight to 60% by weight, preferably from 25% by weight to 55% by weight , based on the total weight of the first isolated product.

According to one aspect of the present invention, in the step (2-2), the boiling point or boiling range of the special component may further be between 350°C and 500°C, such as between 380°C and 524°C. between 400°C and 500°C.

According to one aspect of the present invention, in the step (2-2), the special component is generally a hydrocarbon, especially a mixture of multiple hydrocarbons. Here, the hydrocarbon refers to a compound basically composed of carbon atoms and hydrogen atoms, but may further contain hetero atoms such as O, N, P, Cl, or S in the molecular structure thereof. The present invention does not intend to clarify the specific chemical structure of the specific component, as long as its content and boiling point (or boiling range) satisfy any of the aforementioned corresponding provisions in this specification. In addition, it is known from the manner in which it is obtained that the special component is originally contained as a constituent component in the conversion product or the liquid component. Then, after the separation, (a part or all of) the particular component turns into an essential constituent of the first separated product. In addition, as a method for measuring the specific content of the special component, for example, the first separation product can be distilled, and all the boiling points (or boiling ranges) that satisfy any one of the corresponding provisions in this specification are reserved. Fraction, the percentage of the fraction in the total weight of the first separation product is taken as the specific content.

According to one aspect of the present invention, in the step (2-2), the initial boiling point of the first separation product is generally greater than or equal to 300°C, such as greater than or equal to 330°C, further such as greater than or equal to 350°C.

According to one aspect of the present invention, in the step (2-2), in addition to the special components, the first separation product may further include light components with a boiling point or a boiling range of less than or equal to 350°C . The present invention does not intend to specify the specific content of the light component in the first separated product, but for example, the content of the light component may be from 1 wt % to 10 wt %, based on the total weight of the first isolated product.

According to one aspect of the present invention, in the step (2-2), in addition to the special components, the first separation product may further comprise a boiling point or boiling range greater than 500°C (preferably greater than 524°C) of the heavy components. Here, the so-called "boiling point or boiling range greater than 500°C" means that the heavy component exhibits a boiling point or boiling range greater than 500°C, but also includes that the heavy component is thermally decomposed at a temperature greater than 500°C. No indication of boiling point or boiling range. In addition, in order to make one or more of the technical effects described in the present invention more significant, in a preferred case, the heavy component contains asphaltene, asphaltene, pre-asphaltene or a combination thereof as a constituent, especially Asphaltene is contained as a constituent. The present invention does not intend to specify the specific content of the heavy component in the first separated product, but for example, the content of the heavy component may be the balance, based on the total weight of the first separated product .

According to one aspect of the present invention, in the step (2-2), in addition to the special component and the light component, the first separation product may further contain a boiling point or a boiling range greater than 500° C. (preferably greater than 524°C). Here, the so-called "boiling point or boiling range greater than 500°C" means that the heavy component exhibits a boiling point or boiling range greater than 500°C, but also includes that the heavy component is thermally decomposed at a temperature greater than 500°C. No indication of boiling point or boiling range. In addition, in order to make one or more of the technical effects described in the present invention more significant, in a preferred case, the heavy component contains asphaltene, asphaltene, pre-asphaltene or a combination thereof as a constituent, especially Asphaltene is contained as a constituent. The present invention does not intend to specify the specific content of the heavy component in the first separated product, but for example, the content of the heavy component may be the balance, based on the total weight of the first separated product .

According to one aspect of the present invention, in the step (2-2), for example, when the separation is performed using a distillation column, a quench tank or the like, the first separation product represents the bottom liquid or Tank bottom condensate, and the second separation product represents the overhead light component or the tank top quenched light component.

According to one aspect of the present invention, the conversion product treatment step may optionally further comprise step (2-3), step (2-4), or a combination of both.

Step (2-3): separating the second processed product (including the second separated product) to obtain naphtha and atmospheric gas oil.

According to one aspect of the present invention, in the step (2-3), as the separation, it can be carried out according to any method and any manner known in the art, for example, distillation and fractional distillation can be cited, especially fractional distillation . In addition, the separation can be carried out in any separation device known in the art, such as a fractionation column, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (2-3), the operating pressure is generally from 0.05 MPa to 2.0 MPa, preferably from 0.1.0 MPa to 1.0 MPa.

According to one aspect of the present invention, in the step (2-3), the operating temperature is generally from 50°C to 350°C, preferably from 150°C to 330°C.

Step (2-4): Recycle the gas component to the step (1).

According to one aspect of the present invention, in the step (2-4), the gas component can be recycled as hydrogen to any operation step in the upgrading method that requires hydrogen to participate, such as the step (1).

Step (3): Extracting and separating the first processed product (including the first separated product) to obtain an upgraded oil and a residue (hereinafter referred to as the extraction and separation step).

According to one aspect of the present invention, in the step (3), in order to make one or more of the technical effects described in the present invention more significant, especially in order to further improve the operational stability of the extraction and separation step, The softening point of the residue is generally less than 150°C.

According to one aspect of the present invention, the step (3) can be carried out according to the extraction and separation method comprising the step (3-1).

Step (3-1): contacting the first processed product (including the first separated product) with a solvent at a third pressure and a third temperature to obtain the upgraded oil and the residue.

According to one aspect of the present invention, in the step (3-1), as the contact, any method and any manner known in the art can be performed, as long as the first treated product can be made to be affected by the solvent The above-mentioned reformed oil and the above-mentioned residue may be obtained by sufficient extraction, and specific examples thereof include countercurrent contact and the like. In addition, the extraction can be carried out in any extraction device known in the art (such as an extraction column), which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-1), as the solvent, for example, C _3-7 hydrocarbons can be cited, and more specifically, C _3-5 alkanes and C _3-5 alkenes can be cited , especially C _3-4 alkanes and C _3-4 alkenes. These solvents may be used alone or in combination of two or more in arbitrary ratios. In addition, as the solvent or a part thereof, the liquefied gas described later in this specification can also be used.

According to one aspect of the present invention, in the step (3-1), the weight ratio (referred to as solvent ratio) of the solvent to the first processed product (including the first separated product) is generally 1- 7:1, preferably 1.5-5:1.

According to an aspect of the present invention, in the step (3-1), the third pressure is generally from 3 MPa to 12 MPa, preferably from 3.5 MPa to 10 MPa.

According to one aspect of the present invention, in the step (3-1), the third temperature is generally from 55°C to 300°C, preferably from 70°C to 220°C.

According to one aspect of the present invention, as required, the extraction and separation step may optionally further include one or more of steps (3-2) to (3-11).

Step (3-2): Optionally, hydrotreating the upgraded oil to obtain an upgraded oil after hydrogenation.

According to an aspect of the present invention, in the step (3-2), the hydrogenation treatment can be performed in any manner known in the art, and is not particularly limited. In addition, the hydrotreating can be carried out in any hydrotreating apparatus known in the art (eg, fixed bed reactor, fluidized bed reactor), which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-2), the partial pressure of hydrogen can be selected with reference to the tradition in the art, but is generally from 5.0 MPa to 20.0 MPa, preferably from 8.0 MPa to 15.0 MPa.

According to one aspect of the present invention, in the step (3-2), the reaction temperature can be selected with reference to the tradition in the art, but is generally from 330°C to 450°C, preferably from 350°C to 420°C.

According to one aspect of the present invention, in the step (3-2), the volumetric space velocity of the feedstock oil (referring to the upgraded oil) can be selected with reference to the tradition in the field, but is generally from 0.1h ^-1 to 3.0h ^-1 , preferably from 0.3h ^-1 to 1.5h ^-1 .

According to one aspect of the present invention, in the step (3-2), the volume ratio of hydrogen gas to the raw material oil (referring to the upgraded oil) can be selected with reference to the tradition in the field, but is generally from 300 to 3000 , preferably from 800 to 1500.

According to one aspect of the present invention, in the step (3-2), the hydrogenation treatment is generally carried out in the presence of a hydrogenation catalyst. Here, as the hydrogenation catalyst, for example, any hydrogenation catalyst conventionally used for this purpose in the art can be mentioned, or it can be produced according to any production method conventionally known in the art, and the hydrogenation catalyst is produced in the step. The amount used can refer to the traditional knowledge in the art, and is not particularly limited. Specifically, the hydrogenation catalyst generally includes a support and an active metal component. More specifically, as the active metal components, for example, metals from Group VIB of the Periodic Table of Elements and non-precious metals from Group VIII of the Periodic Table of Elements can be cited, especially the combination of nickel and tungsten, the combination of nickel, tungsten and cobalt. A combination, a combination of nickel and molybdenum, or a combination of cobalt and molybdenum. These active metal components may be used alone or in combination in any ratio. In addition, as the carrier, for example, aluminum oxide, silicon dioxide, amorphous silicon-alumina, and the like can be mentioned. One of these carriers may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. The present invention has no particular limitation on the respective contents of the carrier and the active metal component, and reference can be made to the conventional knowledge in the art.

Step (3-3): Optionally, hydrocracking the upgraded oil to obtain a hydrocracking product.

According to one aspect of the present invention, in the step (3-3), the hydrocracking can be carried out in any manner known in the art, and is not particularly limited. In addition, the hydrocracking can be carried out in any hydrocracking unit known in the art (eg, fixed bed reactor, fluidized bed reactor), which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-3), the hydrocracking product is further separated into dry gas, liquefied gas, aviation kerosene, diesel oil and hydrogenated tail oil. Here, the separation can be carried out according to any method and method known in the art, and specific examples include distillation and fractional distillation, especially fractional distillation. In addition, the separation can be carried out in any separation device known in the art, such as a fractionation column, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-3), the partial pressure of hydrogen can be selected with reference to the tradition in the art, but is generally from 10.0 MPa to 20.0 MPa.

According to one aspect of the present invention, in the step (3-3), the reaction temperature can be selected with reference to the tradition in the art, but is generally from 310°C to 420°C.

According to one aspect of the present invention, in the step (3-3), the volumetric space velocity of the upgraded oil can be selected with reference to the traditional methods in the art, but is generally from 0.3h ^-1 to 1.2h ^-1 .

According to an aspect of the present invention, in the step (3-3), the volume ratio of hydrogen to the upgraded oil can be selected with reference to the traditional method in the art, but is generally from 600 to 1500.

According to one aspect of the present invention, in the step (3-3), the hydrocracking is generally carried out in the presence of a hydrocracking catalyst. Here, as the hydrocracking catalyst, for example, any hydrocracking catalyst conventionally used for this purpose in the art can be cited, or it can be produced according to any production method conventionally known in the art, and the hydrocracking catalyst is The amount used in the above steps can refer to the traditional knowledge in the art, and is not particularly limited. For example, the hydrocracking catalyst generally includes a carrier, an active metal component and a cracking active component. More specifically, as the active metal component, for example, sulfides of metals in group VIB of the periodic table, sulfides of base metals in group VIII of the periodic table, or noble metals in group VIII of the periodic table, etc. , especially Mo sulfide, W sulfide, Ni sulfide, Co sulfide, Fe sulfide, Cr sulfide, Pt and Pd, etc. These active metal components may be used alone or in combination in any ratio. In addition, as the cleavage active component, for example, amorphous silica alumina, molecular sieve, etc. can be mentioned. These cleavage active components may be used alone or in combination in any ratio. In addition, as the carrier, for example, alumina, silicon oxide, titanium oxide, activated carbon, and the like can be mentioned. One of these carriers may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. The present invention has no particular limitation on the respective contents of the carrier, the active metal component and the cleavage active component, and reference may be made to the conventional knowledge in the art.

Step (3-4): Optionally, catalytic cracking (abbreviated as FCC) of the hydrogenated upgraded oil is performed to obtain a first catalytic cracking product.

According to one aspect of the present invention, in the step (3-4), the first catalytic cracking product can be further separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry. Here, the separation can be carried out according to any method and method known in the art, and specific examples include distillation and fractional distillation, especially fractional distillation. In addition, the separation can be carried out in any separation device known in the art, such as a fractionation column, which can be reasonably selected by those skilled in the art.

According to an aspect of the present invention, in the step (3-4), the catalytic cracking can be performed in any manner known in the art, and there is no particular limitation. In addition, the catalytic cracking can be carried out in any catalytic cracking apparatus known in the art, such as a fluidized bed reactor, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-4), the reaction temperature can be selected with reference to the tradition in the art, but is generally from 450°C to 650°C, preferably from 480°C to 560°C.

According to an aspect of the present invention, in the step (3-4), the reaction pressure can be selected with reference to the traditional methods in the art, but is generally from 0.15 MPa to 0.4 MPa.

According to one aspect of the present invention, in the step (3-4), the reaction time can be selected with reference to the traditional choices in the art, but is generally from 0.1 seconds to 10 seconds, preferably from 0.2 seconds to 4 seconds.

According to one aspect of the present invention, in the step (3-4), the weight ratio of the cracking catalyst to the feedstock oil (referring to the hydrogenated upgraded oil) can be selected with reference to the traditional choice in the art, but is generally selected from 3 to 30, preferably from 5 to 15.

According to one aspect of the present invention, in the step (3-4), the weight ratio of the steam to the feedstock oil (referring to the hydrogenated upgraded oil) can be selected with reference to the traditional choices in the field, but is generally selected from 0.05 to 0.6, preferably from 0.05 to 0.4.

According to one aspect of the present invention, in the step (3-4), the catalytic cracking is generally carried out in the presence of a cracking catalyst. Here, as the cracking catalyst, for example, any cracking catalyst conventionally used for this purpose in the art can be cited, or it can be produced according to any conventionally known production method in the art, and is not particularly limited. Specifically, the cracking catalyst is generally a solid acid catalyst, preferably comprising a cracking active component and a carrier. As a more specific example, as the cracking active component, for example, zeolite can be cited, especially Y-type zeolite optionally containing rare earth elements, HY-type zeolite optionally containing rare earth elements, ultra-thin zeolite optionally containing rare earth elements. Stable Y-type zeolite and β-type zeolite optionally containing rare earth elements, etc. These cleavage active components may be used alone or in combination in any ratio. In addition, as the carrier, for example, refractory inorganic oxides, natural clays, alumina, silica, amorphous silica-alumina, and the like can be mentioned. One of these carriers may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. In the present invention, the respective contents of the cleavage active component and the carrier are not particularly limited, and conventional knowledge in the art can be referred to.

Step (3-5): optionally, catalytically cracking the hydrogenated reformed oil in combination with the atmospheric pressure gas oil to obtain a second catalytic cracking product.

According to an aspect of the present invention, in the step (3-5), the so-called combination means that the hydrogenated upgraded oil and the atmospheric gas oil are used together as the raw material for the catalytic cracking. To this end, the two can be pre-mixed in a predetermined ratio before the catalytic cracking is performed, or the catalytic cracking can be performed simultaneously in a predetermined ratio, which is not particularly limited.

According to one aspect of the present invention, in the step (3-5), the second catalytic cracking product can be further separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry. Here, the separation can be carried out according to any method and method known in the art, and specific examples include distillation and fractional distillation, especially fractional distillation. In addition, the separation can be carried out in any separation device known in the art, such as a fractionation column, which can be reasonably selected by those skilled in the art.

According to an aspect of the present invention, in the step (3-5), the catalytic cracking can be performed in any manner known in the art, and is not particularly limited. In addition, the catalytic cracking can be carried out in any catalytic cracking apparatus known in the art, such as a fluidized bed reactor, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-5), the reaction temperature can be selected with reference to the tradition in the art, but is generally from 450°C to 650°C, preferably from 480°C to 560°C.

According to an aspect of the present invention, in the step (3-5), the reaction pressure can be selected with reference to the traditional methods in the art, but is generally from 0.15 MPa to 0.4 MPa.

According to one aspect of the present invention, in the step (3-5), the reaction time can be selected with reference to the traditional choices in the art, but is generally from 0.1 seconds to 10 seconds, preferably from 0.2 seconds to 4 seconds.

According to an aspect of the present invention, in the step (3-5), the weight ratio of the cracking catalyst to the feedstock oil (referring to the hydrogenated upgraded oil and the atmospheric gas oil) can be referred to in the art Traditionally chosen, but generally from 3 to 30, preferably from 5 to 15.

According to one aspect of the present invention, in the step (3-5), the weight ratio of water vapor to feedstock oil (referring to the hydrogenated upgraded oil and the atmospheric gas oil) can be referred to in the art Traditionally chosen, but generally from 0.05 to 0.6, preferably from 0.05 to 0.4.

According to one aspect of the present invention, in the step (3-5), the catalytic cracking is generally carried out in the presence of a cracking catalyst. Here, as the cracking catalyst, for example, any cracking catalyst conventionally used for this purpose in the art can be cited, or it can be produced according to any conventionally known production method in the art, and is not particularly limited. Specifically, the cracking catalyst is generally a solid acid catalyst, preferably comprising a cracking active component and a carrier. As a more specific example, as the cracking active component, for example, zeolite can be cited, especially Y-type zeolite optionally containing rare earth elements, HY-type zeolite optionally containing rare earth elements, ultra-thin zeolite optionally containing rare earth elements. Stable Y-type zeolite and β-type zeolite optionally containing rare earth elements, etc. These cleavage active components may be used alone or in combination in any ratio. In addition, as the carrier, for example, refractory inorganic oxides, natural clays, alumina, silica, amorphous silica-alumina, and the like can be mentioned. One of these carriers can be used alone, or a plurality of them can be used in combination in any ratio. In the present invention, the respective contents of the cleavage active component and the carrier are not particularly limited, and conventional knowledge in the art can be referred to.

Step (3-6): optionally, catalytically cracking the hydrogenated upgraded oil in combination with the second separation product to obtain a third catalytic cracking product.

According to an aspect of the present invention, in the step (3-6), the so-called combination means that the hydrogenated upgraded oil and the second separation product are used together as the raw material for the catalytic cracking. To this end, the two can be pre-mixed in a predetermined ratio before the catalytic cracking is performed, or the catalytic cracking can be performed simultaneously in a predetermined ratio, which is not particularly limited.

According to an aspect of the present invention, in the step (3-6), the third catalytic cracking product can be further separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry. Here, the separation can be carried out according to any method and method known in the art, and specific examples include distillation and fractional distillation, especially fractional distillation. In addition, the separation can be carried out in any separation device known in the art, such as a fractionation column, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-6), the catalytic cracking can be performed in any manner known in the art, and there is no particular limitation. In addition, the catalytic cracking can be carried out in any catalytic cracking apparatus known in the art, such as a fluidized bed reactor, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-6), the reaction temperature can be selected according to the tradition in the art, but is generally from 450°C to 650°C, preferably from 480°C to 560°C.

According to one aspect of the present invention, in the step (3-6), the reaction pressure can be selected with reference to the traditional methods in the art, but is generally from 0.15 MPa to 0.4 MPa.

According to one aspect of the present invention, in the step (3-6), the reaction time can be selected with reference to the traditional choices in the art, but is generally from 0.1 seconds to 10 seconds, preferably from 0.2 seconds to 4 seconds.

According to one aspect of the present invention, in the step (3-6), the weight ratio of the cracking catalyst to the feedstock oil (referring to the hydrogenated upgraded oil and the second separation product) can be referred to in the art Traditionally chosen, but generally from 3 to 30, preferably from 5 to 15.

According to one aspect of the present invention, in the step (3-6), the weight ratio of water vapor to feedstock oil (referring to the hydrogenated upgraded oil and the second separation product) can be referred to in the art Traditionally chosen, but generally from 0.05 to 0.6, preferably from 0.05 to 0.4.

According to one aspect of the present invention, in the step (3-6), the catalytic cracking is generally carried out in the presence of a cracking catalyst. Here, as the cracking catalyst, for example, any cracking catalyst conventionally used for this purpose in the art can be cited, or it can be produced according to any conventionally known production method in the art, and is not particularly limited. Specifically, the cracking catalyst is generally a solid acid catalyst, preferably comprising a cracking active component and a carrier. As a more specific example, as the cracking active component, for example, zeolite can be cited, especially Y-type zeolite optionally containing rare earth elements, HY-type zeolite optionally containing rare earth elements, ultra-thin zeolite optionally containing rare earth elements. Stable Y-type zeolite and β-type zeolite optionally containing rare earth elements, etc. These cleavage active components may be used alone or in combination in any ratio. In addition, as the carrier, for example, refractory inorganic oxides, natural clays, alumina, silica, amorphous silica-alumina, and the like can be mentioned. One of these carriers may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. In the present invention, the respective contents of the cleavage active component and the carrier are not particularly limited, and conventional knowledge in the art can be referred to.

Step (3-7): Optionally, hydrotreating the atmospheric gas oil to obtain diesel oil.

According to an aspect of the present invention, in the step (3-7), the hydrogenation treatment can be performed in any manner known in the art, and is not particularly limited. In addition, the hydrotreating can be carried out in any hydrotreating apparatus known in the art (eg, fixed bed reactor, fluidized bed reactor), which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-7), the partial pressure of hydrogen can be selected with reference to the traditional methods in the art, but is generally from 7.0 MPa to 15.0 MPa.

According to one aspect of the present invention, in the step (3-7), the reaction pressure can be selected with reference to the traditional methods in the art, but is generally from 8 MPa to 12 MPa.

According to one aspect of the present invention, in the step (3-7), the reaction temperature can be selected with reference to the traditional methods in the art, but is generally from 340°C to 400°C.

According to an aspect of the present invention, in the step (3-7), the volumetric space velocity of the atmospheric gas oil can be selected with reference to the traditional methods in the art, but is generally from 0.6h ^-1 to 1.5h ^-1 .

According to one aspect of the present invention, in the step (3-7), the volume ratio of hydrogen gas to the atmospheric gas oil can be selected with reference to the traditional methods in the art, but is generally from 500 to 800.

According to one aspect of the present invention, in the step (3-7), the hydrogenation treatment is generally carried out in the presence of a hydrogenation catalyst. Here, as the hydrogenation catalyst, for example, any hydrogenation catalyst conventionally used for this purpose in the art can be mentioned, or it can be produced according to any production method conventionally known in the art, and the hydrogenation catalyst is produced in the step. The amount used can refer to the traditional knowledge in the art, and is not particularly limited. Specifically, the hydrogenation catalyst generally includes a support and an active metal component. More specifically, as the active metal components, for example, metals from Group VIB of the Periodic Table of Elements and non-precious metals from Group VIII of the Periodic Table of Elements can be cited, especially the combination of nickel and tungsten, the combination of nickel, tungsten and cobalt. A combination, a combination of nickel and molybdenum, or a combination of cobalt and molybdenum. These active metal components may be used alone or in combination in any ratio. In addition, as the carrier, for example, aluminum oxide, silicon dioxide, amorphous silicon-alumina, and the like can be mentioned. One of these carriers may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. In the present invention, the respective contents of the carrier and the active metal component are not particularly limited, and conventional knowledge in the art can be referred to.

Step (3-8): optionally, hydrotreating the circulating oil obtained in any step of the upgrading method and the upgrading oil in combination to obtain a hydroprocessing oil.

According to an aspect of the present invention, in the step (3-8), the so-called combination means that the circulating oil and the upgraded oil are used together as the raw material for the hydrotreatment. To this end, the two may be pre-mixed in a predetermined ratio and then subjected to the hydrogenation treatment, or the hydrogenation treatment may be carried out simultaneously in a predetermined ratio, which is not particularly limited.

According to an aspect of the present invention, in the step (3-8), the hydrogenation treatment can be performed in any manner known in the art, and is not particularly limited. In addition, the hydrotreating can be carried out in any hydrotreating apparatus known in the art (eg, fixed bed reactor, fluidized bed reactor), which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-8), the hydrogen partial pressure can be selected with reference to the traditional methods in the art, but is generally from 5.0 MPa to 20.0 MPa, preferably from 8.0 MPa to 15.0 MPa.

According to one aspect of the present invention, in the step (3-8), the reaction temperature can be selected with reference to the tradition in the art, but is generally from 330°C to 450°C, preferably from 350°C to 420°C.

According to one aspect of the present invention, in the step (3-8), the volumetric space velocity of the feedstock oil (referring to the circulating oil and the upgraded oil) can be selected with reference to the traditional selection in the field, but is generally From 0.1h ^-1 to 3.0h ^-1 , preferably from 0.3h ^-1 to 1.5h ^-1 .

According to one aspect of the present invention, in the step (3-8), the volume ratio of hydrogen to the feedstock oil (referring to the circulating oil and the upgraded oil) can be selected with reference to the traditional choices in the field, but generally is from 300 to 3000, preferably from 800 to 1500.

According to one aspect of the present invention, in the step (3-8), the hydrogenation treatment is generally carried out in the presence of a hydrogenation catalyst. Here, as the hydrogenation catalyst, for example, any hydrogenation catalyst conventionally used for this purpose in the art can be mentioned, or it can be produced according to any production method conventionally known in the art, and the hydrogenation catalyst is produced in the step. The amount used can refer to the traditional knowledge in the art, and is not particularly limited. Specifically, the hydrogenation catalyst generally includes a support and an active metal component. More specifically, as the active metal components, for example, metals from Group VIB of the Periodic Table of Elements and non-precious metals from Group VIII of the Periodic Table of Elements can be cited, especially the combination of nickel and tungsten, the combination of nickel, tungsten and cobalt. A combination, a combination of nickel and molybdenum, or a combination of cobalt and molybdenum. These active metal components may be used alone or in combination in any ratio. In addition, as the carrier, for example, aluminum oxide, silicon dioxide, amorphous silicon-alumina, and the like can be mentioned. One of these carriers may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. In the present invention, the respective contents of the carrier and the active metal component are not particularly limited, and conventional knowledge in the art can be referred to.

Step (3-9): optionally, catalytically cracking the hydrotreated oil in combination with the second separation product to obtain a fourth catalytic cracking product.

According to an aspect of the present invention, in the step (3-9), the so-called combination means that the hydrotreated oil and the second separation product are used together as the raw material for the catalytic cracking. To this end, the two can be pre-mixed in a predetermined ratio before the catalytic cracking is performed, or the catalytic cracking can be performed simultaneously in a predetermined ratio, which is not particularly limited.

According to an aspect of the present invention, in the step (3-9), the fourth catalytic cracking product can be further separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry. Here, the separation can be carried out according to any method and method known in the art, and specific examples include distillation and fractional distillation, especially fractional distillation. In addition, the separation can be carried out in any separation device known in the art, such as a fractionation column, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-9), the catalytic cracking can be performed in any manner known in the art, and is not particularly limited. In addition, the catalytic cracking can be carried out in any catalytic cracking apparatus known in the art, such as a fluidized bed reactor, which can be reasonably selected by those skilled in the art.

According to one aspect of the present invention, in the step (3-9), the reaction temperature can be selected with reference to the traditions in the art, but is generally from 450°C to 650°C, preferably from 480°C to 560°C.

According to an aspect of the present invention, in the step (3-9), the reaction pressure can be selected with reference to the traditional methods in the art, but is generally from 0.15 MPa to 0.4 MPa.

According to an aspect of the present invention, in the step (3-9), the reaction time can be selected with reference to the traditional choices in the art, but is generally from 0.1 seconds to 10 seconds, preferably from 0.2 seconds to 4 seconds.

According to one aspect of the present invention, in the step (3-9), the weight ratio of the cracking catalyst to the feedstock oil (referring to the hydrotreated oil and the second separation product) can be selected with reference to the traditional selection in the art , but generally from 3 to 30, preferably from 5 to 15.

According to one aspect of the present invention, in the step (3-9), the weight ratio of water vapor to feedstock oil (referring to the hydrotreated oil and the second separation product) can be selected with reference to the traditional choices in the art , but generally from 0.05 to 0.6, preferably from 0.05 to 0.4.

According to one aspect of the present invention, in the step (3-9), the catalytic cracking is generally carried out in the presence of a cracking catalyst. Here, as the cracking catalyst, for example, any cracking catalyst conventionally used for this purpose in the art can be cited, or it can be produced according to any conventionally known production method in the art, and is not particularly limited. Specifically, the cracking catalyst is generally a solid acid catalyst, preferably comprising a cracking active component and a carrier. As a more specific example, as the cracking active component, for example, zeolite can be cited, especially Y-type zeolite optionally containing rare earth elements, HY-type zeolite optionally containing rare earth elements, ultra-thin zeolite optionally containing rare earth elements. Stable Y-type zeolite and β-type zeolite optionally containing rare earth elements, etc. These cleavage active components may be used alone or in combination in any ratio. In addition, as the carrier, for example, refractory inorganic oxides, natural clays, alumina, silica, amorphous silica-alumina, and the like can be mentioned. One of these carriers may be used alone, or a plurality of them may be used in combination in an arbitrary ratio. In the present invention, the respective contents of the cleavage active component and the carrier are not particularly limited, and conventional knowledge in the art can be referred to.

Step (3-10): optionally, circulating the oil slurry and/or externally supplied oil slurry obtained in any step of the upgrading method to the step (1), the step (2) and/or or the step (3).

According to one aspect of the present invention, in the step (3-10), the so-called externally supplied oil slurry refers to the oil slurry not derived from any step of the upgrading method of the present invention, but derived from other ways (such as Oil slurry delivered or purchased from outside.

According to an aspect of the present invention, in the step (3-10), by recycling the oil slurry as such, at least the operational stability of the upgrading method can be improved, or in a preferred case, At least the yield of the reformed oil can be further improved.

According to an aspect of the present invention, in the step (3-10), as the circulation mode of the oil slurry, for example, the oil slurry is circulated to the step (1), and the oil slurry is circulated to the step (1). The quality oil is used as the upgrading raw material to continue the conversion reaction, or, the oil slurry is recycled to the step (2), and mixed with the conversion product according to a predetermined ratio, so that the conversion product is The method of performing component formulation, or the method of recycling the oil slurry to the step (3), thereby enabling the extraction and separation to be performed in the presence of the oil slurry. One of these methods may be used alone, or a plurality of them may be used in any combination.

Step (3-11): Optionally, the liquefied gas obtained in any step of the upgrading method is recycled to the step (3).

According to an aspect of the present invention, in the step (3-11), the liquefied gas is recycled to the step (3), including the step (3-1), as the solvent or the solvent a part of.

According to one aspect of the present invention, the upgrading method may optionally further comprise step (4).

Step (4): Recycle all or a part of the residue to the step (1) (hereinafter referred to as a residue recycling step).

According to one aspect of the present invention, in the step (4), a part of the residue (such as more than 80% by weight, preferably more than 90% by weight, more preferably at least 95% by weight) can be recycled to the step (1) ), continue to carry out the conversion reaction together with the low-quality oil as an upgraded raw material, and the remaining part is thrown out. The ratio of the residue of the slaughtered part to the total residue is called the slag slaughter rate, and the unit is % by weight.

According to the present invention, it also relates to a reforming system. Since the upgrading system is specially designed to implement the upgrading method of the present invention, any content, term, feature or limitation, etc. that is not specifically described or explained with respect to the upgrading system in the context of this specification, All can directly refer to the corresponding descriptions or explanations for the modification method in the context of this specification. Additionally, one or more aspects (or embodiments) disclosed in the context of this specification for the upgrading method and one or more aspects (or embodiments) disclosed in the context of this specification for the upgrading system may Arbitrarily combined with each other, the resulting technical solutions (such as methods or systems) are part of the original disclosure content of the present specification, and also fall within the protection scope of the present invention.

According to one aspect of the present invention, the upgrading system includes a conversion reaction unit, a conversion product processing unit, a first control unit, and an extraction separation unit.

According to an aspect of the present invention, in the upgrading system, the conversion reaction unit is configured to enable the conversion reaction of the low-quality oil in the presence of hydrogen and optionally in the presence of a conversion catalyst, and output the obtained conversion product. Here, specific examples of the conversion reaction unit include a hydrothermal conversion reactor.

According to an aspect of the present invention, in the upgrading system, the conversion product processing unit is configured to process the conversion product and output the obtained first processed product. Here, specific examples of the conversion product treatment unit include a flash tank, a fractionation column, or a distillation column.

According to an aspect of the present invention, in the upgrading system, the first control unit is configured to be capable of controlling the operating conditions (such as operating temperature and/or operating pressure) of the conversion product processing unit, so that the The first treatment product comprises components having a boiling point or boiling range between 350°C and 524°C in an amount of from 20% to 60% by weight. Here, specific examples of the first control means include a temperature control device or a pressure control device.

According to an aspect of the present invention, in the upgrading system, the extraction and separation unit is configured to be capable of extracting and separating the first processed product, and outputting the obtained upgraded oil and residue respectively. Here, specific examples of the extraction separation unit include an extraction column.

According to one aspect of the present invention, the upgrading system optionally further comprises a residue treatment unit. The residue treatment unit is configured to be able to deliver all or a portion of the residue to the conversion reaction unit. Here, specific examples of the residue treatment unit include a pump or a transfer line.

According to one aspect of the present invention, in the upgrading system, the conversion product processing unit may further comprise a first conversion product separation unit, a second conversion product separation unit, an optional second separation product separation unit, and an optional gas component delivery unit.

According to an aspect of the present invention, in the upgrading system, the first conversion product separation unit is configured to be able to separate the conversion product and output the obtained gas component and liquid component, respectively. Here, specific examples of the first conversion product separation unit include a pressurized distillation column.

According to an aspect of the present invention, in the upgrading system, the second conversion product separation unit is configured to be capable of separating the liquid components, and to output the obtained second separation product and first separation product, respectively . Here, specific examples of the second conversion product separation unit include a flash tank or an atmospheric distillation column.

According to an aspect of the present invention, in the upgrading system, the second separation product separation unit is configured to be able to separate the second separation product and output the obtained naphtha and atmospheric gas oil respectively . Here, specific examples of the second separation product separation unit include a fractionation column.

According to an aspect of the present invention, in the reforming system, the gas component delivery unit is configured to deliver the gas component to the conversion reaction unit. Here, specific examples of the gas component delivery unit include a gas delivery line.

According to an aspect of the present invention, the reforming system may further include a second control unit and a third control unit.

According to an aspect of the present invention, in the upgrading system, the second control unit is configured to be able to control the operating pressure of the first conversion product separation unit, and the third control unit is configured to be able to control all the The operating pressure of the second conversion product separation unit is adjusted, and the operating pressure of the first conversion product separation unit is made greater than the operating pressure of the second conversion product separation unit. Here, specific examples of the second control unit include a pressure control device and a system. In addition, specific examples of the third control means include a pressure control device and a system.

According to an aspect of the present invention, in the upgrading system, the third control unit may be configured to be able to control the operating conditions (such as operating temperature and/or operating pressure) of the second conversion product separation unit, causing the first isolated product to comprise components having a boiling point or boiling range between 350°C and 524°C in an amount from 20% to 60% by weight, and causing the second isolated product or any component thereof Has an end boiling point less than or equal to 350°C. Here, specific examples of the third control unit include a pressure control device and system or a temperature control device and system.

According to an aspect of the present invention, in the upgrading system, for the convenience of operation and measurement, preferably, the second control unit is configured to be able to control the gas composition of the first conversion product separation unit the outlet pressure and/or the outlet temperature, the third control unit is arranged to be able to control the outlet pressure and/or the outlet temperature of the second separated product of the second conversion product separation unit.

According to an aspect of the present invention, in the upgrading system, the extraction separation unit is configured to be capable of contacting the first separation product or the first processed product with a solvent, and respectively outputting the obtained The upgraded oil and the residue. Here, specific examples of the extraction separation unit include an extraction column.

According to one aspect of the present invention, the upgrading system optionally further comprises one or more of the following units.

The first hydrogenation unit is provided so as to be capable of subjecting the reformed oil to hydrotreating, and to output the obtained reformed oil after hydrogenation. Here, specific examples of the first hydrogenation unit include a fixed bed hydrogenation reactor.

The second hydrogenation unit is configured to be capable of hydrocracking the upgraded oil, and separating the obtained hydrocracking product into dry gas, liquefied gas, aviation kerosene, diesel oil and hydrogenated tail oil. Here, specific examples of the second hydrogenation unit include a fixed bed hydrocracking reactor.

The first catalytic cracking unit is configured to be capable of catalytic cracking the hydrogenated reformed oil, and separating the obtained first catalytic cracking product into dry gas, liquefied gas, gasoline, circulating oil and oil slurry. Here, as the first catalytic cracking unit, for example, a fluidized-bed catalytic cracking reactor can be specifically mentioned.

The second catalytic cracking unit is configured to be able to jointly carry out catalytic cracking of the hydrogenated reformed oil and the atmospheric gas oil, and separate the obtained second catalytic cracking product into dry gas, liquefied gas, gasoline, Circulating oil and oil slurry. Here, as the second catalytic cracking unit, for example, a fluidized-bed catalytic cracking reactor can be specifically mentioned.

The third catalytic cracking unit is configured to be able to jointly carry out catalytic cracking of the hydrogenated modified oil and the second separation product, and separate the obtained third catalytic cracking product into dry gas, liquefied gas, gasoline, Circulating oil and oil slurry. Here, as the third catalytic cracking unit, for example, a fluidized-bed catalytic cracking reactor can be specifically mentioned.

The third hydrogenation unit is configured to be capable of hydrotreating the atmospheric gas oil and outputting the obtained diesel oil. Here, specific examples of the third hydrogenation unit include a fixed bed hydrogenation reactor.

The fourth hydrogenation unit is provided so as to be capable of hydrotreating the recycle oil obtained by any unit of the reforming system in combination with the reforming oil, and outputting the obtained hydrotreated oil. Here, specific examples of the fourth hydrogenation unit include a fixed bed hydrogenation reactor.

The fourth catalytic cracking unit is set up to be able to jointly carry out catalytic cracking of the hydrotreated oil and the second separation product, and separate the obtained fourth catalytic cracking product into dry gas, liquefied gas, gasoline, and circulating oil and oil slurry. Here, as the fourth catalytic cracking unit, for example, a fluidized bed catalytic cracking reactor can be specifically mentioned.

An oil slurry conveying unit configured to be capable of conveying the oil slurry and/or externally supplied oil slurry obtained by any unit of the upgrading system to the conversion reaction unit, the conversion product processing unit and/or the Extraction separation unit. Here, as the oil slurry conveying unit, for example, a conveying line or a pump can be specifically mentioned.

The liquefied gas delivery unit is configured to be able to deliver the liquefied gas obtained by any unit of the upgrading system to the extraction and separation unit. Here, specific examples of the liquefied gas delivery unit include a gas delivery line.

Hereinafter, the present specification will further illustrate and illustrate the modification method and modification system of the present invention with reference to the accompanying drawings, but the present invention is not limited thereto.

According to FIG. 1 , the low-quality oil is sent to the reforming reaction unit 7 as the reforming raw material through the pipeline 1, the reforming catalyst through the pipeline 2, the circulating hydrogen through the pipeline 3, the fresh hydrogen through the pipeline 4 and the residue through the pipeline 5 to the transformation reaction unit 7 for transformation reaction. The transformed product is transported to the first transformed product separation unit 9 through the pipeline 8 for pressurized distillation, and is separated into a gas component and a liquid component, and then the gas component is transported to the transformation through the pipeline 10, the pipeline 3 and the pipeline 6 as the circulating hydrogen successively. The reaction unit 7 is led out of the system through pipeline 10 and pipeline 11 successively. The liquid component is conveyed via line 12 to the second conversion product separation unit 13 for pressure drop and separation into the second separated product and the first separated product. The second separated product is drawn out of the system through line 15, and the first separated product is transported to the extraction and separation unit 16 through line 14 to be in countercurrent contact with the solvent from line 17 for extraction and separation to obtain upgraded oil and residue. The upgraded oil is drawn out of the system through the pipeline 18, and a part of the residue is thrown out through the pipeline 19 and the pipeline 20 successively. The conversion reaction is continued together. Alternatively, all the residues can be thrown out successively through the pipeline 19 and the pipeline 20 without being circulated.

According to FIG. 2 , on the basis of FIG. 1 , (1) the upgraded oil is transported through the pipeline 18 to the first hydrogenation unit 21 for further hydrogenation treatment to obtain the hydrogenated upgraded oil 22 with further improved quality.

According to Fig. 3, on the basis of Fig. 1, (2) the second separation product is transported to the second separation product separation unit through the pipeline 15, and the naphtha and atmospheric gas oil (AGO) are obtained by fractionation, and the naphtha is obtained through the pipeline Line 21 is led out of the system, AGO is transported to the third hydrogenation unit 24 through pipeline 22 and pipeline 23, and the high-quality diesel oil that meets the national V index is obtained after hydrogenation, and the high-quality diesel oil is led out of the system through pipeline 25; (3) Modified The high-quality oil is transported to the second hydrogenation unit 26 through the pipeline 18 for hydrocracking reaction to obtain a hydrocracking product, and the hydrocracking product is transported to the fractionation system 28 through the pipeline 27, and is separated to obtain dry gas, liquefied gas, aviation kerosene meeting the national standard, high Quality diesel and hydrogenated tailstocks. Dry gas, liquefied gas, aviation kerosene meeting the national standard, high-quality diesel oil and hydrogenated tail oil are drawn out of the system through pipeline 29, pipeline 30, pipeline 31, pipeline 32 and pipeline 33 respectively; and (4) hydrogenated tail oil can be used as steam Cracking raw material for ethylene production.

According to FIG. 4 , on the basis of FIG. 1 , (1) the upgraded oil is transported to the fourth hydrogenation unit 20 via the pipeline 18 and the circulating oil via the pipeline 26 for joint hydrotreating to obtain a hydrotreating oil with further improved quality; (2) ) The hydrotreated oil passes through the pipeline 21 and the pipeline 22, and the second separation product is transported to the fourth catalytic cracking unit 23 through the pipeline 15 and the pipeline 22 to jointly carry out the catalytic cracking reaction. Alkane gasoline, circulating oil and oil slurry; (3) dry gas is drawn out of the system through pipeline 24, a part of liquefied gas is recycled to extraction and separation unit 16 as solvent through pipeline 28 and pipeline 17, and the other part of liquefied gas is passed through pipeline 28 , the pipeline 29 is drawn out of the system, and the high-octane gasoline is drawn out of the system as a product through the pipeline 25; (4) the oil slurry is used as an upgraded raw material to be circulated to the conversion reaction unit 7 through the pipeline 27, the pipeline 6 and continue together with the low-quality oil The conversion reaction is carried out.

Example

Hereinafter, the present invention will be described in further detail by using examples, but the present invention is not limited to these examples.

In the context of the present invention, including in the following examples and comparative examples, the determination method of heavy metal (calculated as Ni+V) content is in accordance with ASTM D5708; the determination method of asphaltene content is in accordance with SH/T 0266-92 ( 1998); conversion rate of low-quality oil=(1-residue rejection rate)×100%;residue rejection rate=outer rejection residue mass/modified raw material mass×100%; modified oil yield=modified oil mass/ Quality of modified raw material × 100%; yield of toluene insoluble matter = mass of toluene insoluble matter / mass of modified raw material × 100%; gasoline yield = mass of gasoline / mass of catalytic cracking feedstock oil × 100%; aviation kerosene yield = aviation kerosene Mass/mass of hydrocracking feedstock oil×100%; diesel yield=diesel mass/mass of hydrocracking feedstock×100%.

The cetane number of diesel oil was determined according to the standard method of GB T386-2010.

The operational stability of the reforming process was evaluated by the number of days of stable operation of the reforming system. Specifically, if any one of the following conditions occurs in the reforming system, it is determined that it cannot run stably: (1) the maximum temperature deviation ΔT (absolute value) of different temperature measurement points inside the conversion reactor is greater than 5°C; (2) The modified oil appears black, which normally appears yellow or yellow-green.

The following examples and comparative examples are carried out according to the embodiments similar to those in the accompanying drawings.

In the following examples and comparative examples, as the low-quality oil, the modified raw material A and the modified raw material B are vacuum residue oil, the modified raw material C is Venezuelan heavy oil reduced residue, and the modified raw material D is high-temperature coal tar, The reformed raw material E is deoiled pitch. The properties of these five low-quality oils are shown in Table 1.

Example 1 to Example 5

On a medium-sized plant, the low-quality oil is first subjected to the conversion reaction, and then the conversion product is processed to obtain a first isolated product and a second isolated product. The specific conditions and results of the conversion reaction and the treatment of the conversion product are listed in Table 2.

Example 6 to Example 8

On a medium-sized plant, the low-quality oil is first subjected to the conversion reaction, and then the conversion product is processed to obtain a first isolated product and a second isolated product. The specific conditions and results of the conversion reaction and the treatment of the conversion product are listed in Table 3.

Example 9 to Example 11

On a medium-sized device, the first separated products obtained in Example 2, Example 4 and Example 7 were extracted and separated respectively. The specific conditions and results of extraction and separation are listed in Table 4.

Example 12 to Example 13

On a medium-sized device, the low-quality oil is used as an upgraded raw material for the conversion reaction, and then the conversion product is processed to obtain the first separated product and the second separated product. The first separated product is then extracted and separated to obtain an upgraded oil and a residue. A part of the residue is recycled back to the conversion reaction, mixed with the low-quality oil and used as an upgraded raw material for the conversion reaction, and the rest of the residue is thrown out. The conversion product of (low quality oil + residue) is processed to obtain a first isolated product and a second isolated product. The first separated product is then extracted and separated to obtain an upgraded oil and a residue. The second separation product is separated to obtain a naphtha fraction and atmospheric gas oil. The specific conditions and results of each step are listed in Table 5.

Comparing the results in Tables 4 and 5, it can be seen that recycling the residue is beneficial to improve the conversion rate of low-quality oil and the yield of modified oil.

Example 14

The reformed oil obtained in Example 12 was subjected to hydrogenation treatment. The specific conditions and results of this hydrotreatment are listed in Table 6.

From the properties of the raw material oil in Table 6, it can be known that the asphaltene content of the modified oil is less than 0.5%, and the heavy metal content is less than 2 μg /g, which realizes the high asphaltene conversion rate and high metal removal rate of the modified raw material. After hydrotreating, the properties of the obtained hydrogenated upgraded oil meet the FCC feed requirements.

Example 15

The modified oil obtained in Example 12 was subjected to hydrocracking. The specific conditions and results of this hydrocracking are listed in Table 7-1 and Table 7-2.

The properties of the aviation kerosene are shown in the table below.

From the results of these tables, it can be seen that by hydrocracking the modified oil, high-quality aviation kerosene and high-quality diesel can be obtained, and the yield of aviation kerosene is greater than 38%.

Example 16

The hydrogenated reformed oil obtained in Example 14 was subjected to catalytic cracking. The specific conditions and results of the catalytic cracking are listed in Table 8.

It can be seen from the results in Table 8 that the hydrogenated reformed oil is subjected to catalytic cracking to obtain high-octane gasoline. The yield of the high-octane gasoline was 49.40%, and its research octane number was 92.1.

Example 17

The atmospheric pressure gas oil obtained in Example 12 and the upgraded oil after hydrogenation obtained in Example 14 were subjected to catalytic cracking together. The specific conditions and results of the catalytic cracking are listed in Table 9.

It can be seen from the results in Table 9 that the catalytic cracking of the hydrogenated reformed oil and atmospheric gas oil together can obtain high-octane gasoline with an octane number greater than 92. The yield of the high-octane gasoline was 52.62%.

Example 18

The atmospheric pressure gas oil obtained in Example 12 was hydrogenated. The specific conditions and results of this hydrotreatment are listed in Table 10.

It can be seen from the results in Table 10 that the atmospheric gas oil can be hydrogenated to obtain high-quality diesel oil with a cetane number greater than 51.

Example 19

The circulating oil obtained in Example 16 or Example 17 is hydrotreated together with the upgraded oil obtained in Example 12, and the obtained hydrotreated oil is then subjected to catalytic cracking. The specific conditions and results of the hydrotreatment and catalytic cracking are listed in Table 11.

From the results in Table 11, it can be seen that the circulating oil and the modified oil are hydrotreated together and then subjected to catalytic cracking to obtain a high-octane gasoline component with an octane number greater than 93, and the yield of the high-octane gasoline component can reach 56.47. %.

Example 20

On a medium-sized device, based on Example 12, the oil slurry obtained in Example 16 was recycled back to the conversion reaction, mixed with the low-quality oil and the recycle residue, and used as an upgraded raw material for the conversion reaction, and then the conversion product was processed to obtain the first An isolated product and a second isolated product. The first separated product is then extracted and separated to obtain an upgraded oil and a residue. Part of the residue is circulated and the rest is thrown out. The specific conditions and results of each step are listed in Table 12.

The results in Table 12 show that through the oil slurry circulation, it is beneficial to improve the conversion rate of low-quality oil and the yield of modified oil by 2.0 percentage points and 1.5 percentage points, respectively, the yield of toluene insoluble matter decreased by 25%, and the number of stable operation days exceeded 30. It is beneficial to the long-term stable operation of the reforming system.

Example 21

On a medium-sized device, the reformed raw material B is used as the reformed raw material to carry out the conversion reaction, and then the conversion product is processed to obtain the first separated product and the second separated product. The first separated product is then subjected to extraction and separation (the extraction and separation conditions are the same as those in Example 12) to obtain upgraded oil and residue. A part of the residue is recycled back to the conversion unit, and the rest is thrown out. The conversion products of the mixed raw materials are subjected to successive product treatments to obtain a first isolated product and a second isolated product. The first product is then subjected to extraction and separation (the extraction and separation conditions are the same as those in Example 12) to obtain an upgraded oil and a residue. The specific conditions and results of each step are listed in Table 13.

Comparative Example 1 to Comparative Example 4

It is the same as Example 21, except that it is changed according to Table 13.

The results in Table 13 show that when the special components do not meet the corresponding requirements of the present invention, the conversion rate of low-quality oil will be reduced by 6 to 10 percentage points, the yield of modified oil will be reduced by 5 to 8 percentage points, and the yield of toluene insoluble matter will be increased. 1~2.5 percentage points, and because △T>5℃ or the modified oil appears black, the stable operation days of the modified system are greatly reduced.

In the description of the invention of the present application, a large amount of specific technical information is described. However, those skilled in the art can understand that the invention of the present application can also be implemented without these specific technical information. In some aspects or embodiments of the invention of the present application, well-known methods, structures and techniques are not explained or described in detail, but this does not affect the understanding of the invention of the present application by those skilled in the art.

Similarly, it should be understood that, in order to simplify the description of the invention of the present application and help those skilled in the art to understand the spirit of the invention of the present application, the modification method or the modification system of the present invention is exemplified in the context of the present specification. When describing or illustrating, various aspects (or implementations) are sometimes presented in combination in specific embodiments or figures. However, this description or illustration should not be construed to reflect the following intention: the technical solution claimed by the invention of the present application has a larger number of features than the technical solution literally described in the patent scope of the application. More specifically, as reflected in the scope of the patent application, the technical solutions claimed by the invention of the present application contain fewer technical features than the specific embodiments or drawings described or illustrated in the context of this specification.

In the context of the present invention, relational terms such as first and second are used only to distinguish one entity or operation from another entity or operation, without requiring or implying an actual relationship between these entities or operations. There is such a relationship or order. Moreover, the expressions "comprising", "comprising" or similar expressions are a non-exclusive expression, so that the process, method, article or apparatus to which these expressions are directed includes not only one or more of those expressly described in this specification elements, and may also include other elements or elements not expressly described in this specification, such as one or more elements inherent in the process, method, article, or apparatus.

The embodiments disclosed in this specification are only used to illustrate the specific implementation of the invention of the present application, but not to limit them. Although the present specification has explained or described the invention of the present application in detail with reference to these embodiments, it should be understood that those skilled in the art can still modify or change the technical solutions described in these embodiments, or modify some of the technical solutions in these embodiments. Features are replaced with equivalents. Since the technical solutions obtained through such modifications, changes or substitutions do not depart from the spirit and essence of the invention of the present application, they still belong to the protection scope of the invention of the present application.

1-6,8,10-12,14-15,17-20‧‧‧Pipeline

7‧‧‧Conversion reaction unit

9‧‧‧First conversion product separation unit

13‧‧‧Second conversion product separation unit

16‧‧‧Extraction and separation unit

Claims (21)

An upgrading method is characterized in that, comprising the following steps: (1) making low-quality oil as an upgrading raw material to carry out a transformation reaction in the presence of hydrogen to obtain a transformed product, (2) treating the transformed product to obtain the first A treatment product, wherein the first treatment product comprises, based on the total weight of the first treatment product, in an amount of from 20% to 60% by weight boiling point or boiling range between 350°C and 524°C components, and (3) extracting and separating the first treated product to obtain an upgraded oil and a residue, wherein the low-quality oil comprises one or more of asphaltenes, asphaltenes, and pre-asphaltenes. The reforming method according to claim 1, further comprising the following steps: (4) recycling all or a part of the residue to the step (1). The upgrading method according to claim 1 or 2, wherein the step (2) comprises one or more of the following steps: (2-1) carrying out the conversion product at a first pressure and a first temperature Separating to obtain a gas component and a liquid component, (2-2) separating the liquid component at a second pressure and a second temperature to obtain the first processed product and the second separated product, wherein the to separate to obtain the first treated product comprising components having a boiling point or a boiling range between 350°C and 524°C in an amount from 20% to 60% by weight, and make the second isolated product or any of its components Having an end boiling point less than or equal to 350°C, (2-3) separating the second separation product to obtain naphtha and atmospheric gas oil, and (2-4) recycling the gas component to In the step (1), the first pressure is greater than the second pressure by 4MPa to 24MPa. The upgrading method according to claim 1 or 2, wherein the step (3) comprises one or more of the following steps: (3-1) subjecting the first processed product to a solvent at a third pressure and a third pressure Contact at three temperatures to obtain the reformed oil and the residue, (3-2) hydrogenating the reformed oil to obtain the reformed oil after hydrogenation, (3-3) subjecting the reformed oil to Carry out hydrocracking to obtain a hydrocracking product, then separate the hydrocracking product into dry gas, liquefied gas, aviation kerosene, diesel oil and hydrogenated tail oil, (3-4) catalytically cracking the modified oil after the hydrogenation, Obtain the first catalytic cracking product, then separate the first catalytic cracking product into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, (3-5) combine the hydrogenated modified oil with the normal pressure The gas oil is combined for catalytic cracking to obtain a second catalytic cracking product, and then the second catalytic cracking product is separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, (3-6) Combined catalytic cracking of the hydrogenated modified oil and the second separation product to obtain a third catalytic cracking product, and then separating the third catalytic cracking product into dry gas, liquefied gas, and gasoline , circulating oil and oil slurry, (3-7) hydrogenation of the atmospheric gas oil to obtain diesel oil, (3-8) the circulating oil obtained in any step of the upgrading method alone or with the Hydrotreating the upgraded oil in combination to obtain a hydrotreating oil, (3-9) combining the hydrotreating oil and the second separation product for catalytic cracking to obtain a fourth catalytic cracking product, and then synthesizing the fourth The catalytic cracking product is separated into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, and (3-10) the oil slurry and/or externally supplied oil slurry obtained in any step of the upgrading method are recycled to the Step (1), the step (2) and/or the step (3), or (3-11) the liquefied gas obtained in any step of the upgrading method is recycled to the step (3) Or the step (3-1). The upgrading method according to claim 1 or 2, wherein the reaction conditions of the conversion reaction include: a hydrogen partial pressure of 10.0 MPa to 25.0 MPa, a reaction temperature of 380° C. to 470° C., and the volume of the upgraded raw material is empty. The speed is 0.01h ^-1 to 2.0h ^-1 , and the volume ratio of hydrogen to the modified raw material is 500 to 5000. The modification method according to claim 3, wherein the first pressure is 10.0 MPa to 25.0 MPa, and the first temperature is 380° C. to 470° C., or, the The second pressure is from 0.1 MPa to 5.0 MPa, and the second temperature is from 150°C to 390°C. The upgrading method of claim 4, wherein the solvent is one or more of C _3-7 hydrocarbons, and the weight ratio of the solvent to the first processed product is 1-7:1. The upgrading method of claim 4, wherein the third pressure is 3 MPa to 12 MPa, and the third temperature is 55°C to 300°C. The modification method according to claim 4, wherein the reaction conditions of the step (3-2) or the step (3-8) include: a hydrogen partial pressure of 5.0 MPa to 20.0 MPa, and a reaction temperature of 330 to 330° C. 450°C, the volumetric space velocity of the feedstock oil is 0.1h ^-1 to 3.0h ^-1 , the volume ratio of hydrogen to feedstock oil is 300 to 3000, in the presence of a hydrogenation catalyst; or, in the step (3-3) The reaction conditions include: the partial pressure of hydrogen is 10.0MPa to 20.0MPa, the reaction temperature is 310°C to 420°C, the volume space velocity of the reformed oil is 0.3h ^-1 to 1.2h ^-1 , the hydrogen and the reformed oil are The volume ratio is 600 to 1500, in the presence of a hydrocracking catalyst; or, the step (3-4), the step (3-5), the step (3-6) or the step (3) The reaction conditions of -9) include: the reaction temperature is 450°C to 650°C, the reaction pressure is 0.15MPa to 0.4MPa, the reaction time is 0.1s to 10s, the weight ratio of the cracking catalyst to the raw oil is 3 to 30, the water vapor is The weight ratio to the raw oil is 0.05 to 0.6, in the presence of a cracking catalyst; or, the reaction conditions of the step (3-7) include: the partial pressure of hydrogen is 7.0 MPa to 15.0 MPa, and the reaction pressure is 8 MPa to 12 MPa, The reaction temperature is 340°C to 400°C; the volumetric space velocity of the normal pressure gas oil is 0.6h ^-1 to 1.5h ^-1 , and the volume ratio of hydrogen to the normal pressure gas oil is 500 to 800. exist. The modification method according to claim 1 or 2, wherein the softening point of the residue is less than 150°C. The upgrading method according to claim 1, wherein the low-quality oil is selected from one or more of inferior oil, deoiled asphalt, heavy oil, heavy oil, coal-derived oil, shale oil and petrochemical waste oil. The upgrading method according to claim 1 or 2, wherein the initial boiling point of the first processed product is greater than or equal to 330°C, or, the first processed product further comprises a boiling point or a boiling range less than or equal to 350°C Light components, alternatively, the first treatment product further comprises heavier components with a boiling point or boiling range greater than 500°C. The upgrading method according to claim 1 or 2, wherein in the step (2), in addition to obtaining the first treatment product, one or more second treatments are also obtained The product, the second processed product, or any component thereof, has an end boiling point less than or equal to 350°C. An upgrading system, characterized in that it comprises a conversion reaction unit, a conversion product processing unit, a first control unit and an extraction separation unit, wherein the conversion reaction unit is configured to enable the conversion reaction of low-quality oil in the presence of hydrogen , and output the obtained conversion product, the conversion product processing unit is set to be able to process the conversion product, and output the obtained first processed product, the first control unit is set to be able to control the conversion by The operating conditions of the product treatment unit such that the first treatment product comprises a content of from 20% to 60% by weight, based on the total weight of the first treatment product, with a boiling point or boiling range between 350°C and 524°C The components in between, and the extraction and separation unit is configured to be capable of extracting and separating the first processed product, and outputting the obtained upgraded oil and residue respectively. The upgrading system of claim 14, further comprising a residue processing unit, the residue processing unit being configured to be capable of delivering all or a portion of the residue to the conversion reaction unit. The upgrading system according to claim 14 or 15, wherein the conversion product processing unit comprises a first conversion product separation unit, a second conversion product separation unit unit, the first conversion product separation unit is arranged to be able to separate the conversion product and output the obtained gas components and liquid components respectively, and the second conversion product separation unit is arranged to be able to The liquid components are separated and outputted to obtain the first treated product and the second separated product. The upgrading system of claim 16, wherein the conversion product processing unit further comprises a second separation product separation unit and a gas component delivery unit, the second separation product separation unit being configured to be capable of converting the second separation product The separation product is separated, and the obtained naphtha and atmospheric gas oil are respectively output, and the gas component delivery unit is arranged to be able to deliver the gas component to the conversion reaction unit. The upgrading system of claim 16, further comprising a second control unit and a third control unit, wherein the second control unit is configured to control the operating pressure of the first conversion product separation unit, the The third control unit is arranged to be able to control the operating pressure of the second conversion product separation unit and make the operating pressure of the first conversion product separation unit greater than the operating pressure of the second conversion product separation unit. The upgrading system of claim 18, wherein the third control order The unit is configured to be able to control the operating conditions of the second conversion product separation unit such that the first separation product comprises a boiling point or a boiling range between 350°C and 524°C in an amount of 20% to 60% by weight components, and make the second separated product or any of its components have an end boiling point less than or equal to 350°C. The upgrading system of claim 14 or 15, wherein the extractive separation unit is configured to contact the first treatment product with a solvent and output the obtained upgraded oil and the residue, respectively. The upgrading system of claim 14 or 15, further comprising one or more of the following units: a first hydrogenation unit, configured to be capable of hydrotreating the upgraded oil and outputting the obtained post-hydrogenation reformation high-quality oil, a second hydrogenation unit, configured to be capable of hydrocracking the upgraded oil, and separating the obtained hydrocracking product into dry gas, liquefied gas, aviation kerosene, diesel oil and hydrogenated tail oil, the first catalytic a cracking unit, configured to be capable of catalytic cracking the hydrogenated reformed oil, and separating the obtained first catalytic cracking product into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, and a second catalytic cracking unit , is set to be able to jointly carry out catalytic cracking of the hydrogenated reformed oil and the atmospheric gas oil, and separate the obtained second catalytic cracking product into dry gas, liquefied gas, gasoline, circulating oil and oil slurry , The third catalytic cracking unit is configured to be able to jointly carry out catalytic cracking of the hydrogenated modified oil and the second separation product, and separate the obtained third catalytic cracking product into dry gas, liquefied gas, gasoline, Circulating oil and oil slurry, a third hydrogenation unit, configured to hydrotrease the atmospheric gas oil and outputting the obtained diesel oil, and a fourth hydrogenation unit, configured to be capable of converting any one of the reforming systems unit for hydrotreating the recycle oil obtained in combination with the upgraded oil and outputting the obtained hydrotreating oil, a fourth catalytic cracking unit configured to be able to co-process the hydrotreating oil with the second separation product Catalytic cracking, and separating the obtained fourth catalytic cracking product into dry gas, liquefied gas, gasoline, circulating oil and oil slurry, the oil slurry conveying unit is set to be able to obtain any unit of the upgrading system The oil slurry and/or externally supplied oil slurry are transported to the conversion reaction unit, the conversion product processing unit and/or the extraction separation unit, or the liquefied gas delivery unit, and are configured to be able to convert the upgrading system. The liquefied gas obtained in any unit is sent to the extraction and separation unit.

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