A device for extracting and separating coal tar oil slurry by supercritical carbon dioxide

Abstract

The application belongs to the technical field of coal tar and catalytic cracking slurry processing, and relates to an extraction separation device for extracting and separating a coal tar and catalytic cracking slurry mixture (hereinafter referred to as coal catalytic oil slurry) by supercritical carbon dioxide, comprising a liquid coal catalytic oil slurry output unit, a liquid medicine supply unit, an extraction unit, a separation unit, a carbon dioxide supply unit and a water vapor pipeline, wherein the liquid coal catalytic oil slurry output unit, the liquid medicine supply unit, the extraction unit, the separation unit and the carbon dioxide supply unit are sequentially connected, and an output end of the carbon dioxide supply unit is connected with an input end of the extraction unit. The technical scheme provided by the application can accurately separate each component of the coal catalytic oil slurry, and the extraction efficiency and the product quality of the extract can be significantly improved.

Description

Technical Field

[0001] This application relates to the field of coal tar pitch and catalytic cracking slurry processing technology, specifically to a processing technology for supercritical carbon dioxide extraction and separation of a mixture of coal tar pitch and catalytic cracking slurry (hereinafter referred to as coal-catalytic slurry), and more specifically, to an apparatus for supercritical carbon dioxide extraction and separation of coal-catalytic slurry. Background Technology

[0002] Coal tar pitch is a type of coal tar produced during the dry distillation of coal at 500–900℃. After the coal tar undergoes vacuum distillation to extract lighter components, the residue obtained at the bottom of the vacuum distillation tower is coal tar pitch. The density of coal tar pitch at 20℃ is 0.98 g / cm³. 3 ~1.30g / cm 3 The softening point is between 35℃ and 95℃, and the average molecular weight of coal tar pitch is between 1000 and 5000 g / mol. Coal tar pitch contains metallic impurities, quinoline insolubles, sulfides, and nitride impurities.

[0003] Catalytic cracking slurry is a viscous slurry ejected from the bottom of the fractionation tower in the catalytic cracking unit during petroleum refining. Its density at 20°C is 1.01 g / cm³. 3 ~1.25g / cm 3 Catalytic cracking slurry contains approximately 0.1–0.8% metal particles and small amounts of gum and asphaltenes. It has a high content of polycyclic aromatic hydrocarbons and a low hydrogen-carbon atom count, making it an ideal raw material for producing needle coke, carbon black, petroleum aromatic plasticizers, rubber modifiers, asphalt modifiers, solvent deasphalting reinforcing agents, heat transfer oils, and heavy fuel oils. However, the molecular weight of catalytic cracking slurry is only 300–400 g / mol, far lower than the 1000–3000 g / mol molecular weight of coated asphalt. Clearly, it cannot be directly used as a raw material for coated asphalt. Furthermore, before use, the fine metal particles, gum, and asphaltenes in the catalytic cracking slurry must be thoroughly removed to allow its unique properties to be fully realized.

[0004] Existing methods for producing lithium-ion battery and graphite electrode coated asphalt using catalytic cracking slurry are basically as follows: First, the catalytic cracking slurry is filtered to remove impurities. Then, the slurry is fed into a coking furnace for pyrolysis and condensation reactions. This causes large saturated hydrocarbon molecules to break down into lighter oil and gas molecules, which are then discharged from the system. Small aromatic molecules condense into larger molecules, which are then extracted by distillation. Finally, modifiers are added, and the mixture is granulated and pulverized to become the raw material for coated asphalt. While this method can produce coated asphalt with a high softening point, high sintering rate, and low ash content, basically meeting the three important technical requirements of coated asphalt (softening point above 250℃, sintering rate above 75%, and ash content below 0.1%w), the process is complex, has low yield, high investment, and high cost.

[0005] To develop a simple and low-cost method for producing coated asphalt raw materials, this application discloses a method for producing high-end carbon raw materials for coated asphalt using supercritical carbon dioxide extraction and separation of coal-fired catalytic cracking slurry. The principle is as follows: the molecular weight of coated asphalt is 1000–3000 g / mol, while the average molecular weight of coal tar pitch is 1000–5000 g / mol. Therefore, using coal tar pitch as a raw material for coated asphalt is sufficient in terms of molecular weight. The molecular weight of catalytic cracking slurry is only 300–400 g / mol, far lower than that of coated asphalt, and obviously cannot be directly used as a raw material for coated asphalt. If coal tar pitch and catalytic cracking slurry are mixed in a certain proportion, a mixture with a suitable molecular weight for producing coated asphalt raw materials can be prepared. After supercritical carbon dioxide extraction and separation, metallic carbon particles and solid impurities are removed. After removing the lighter components such as 5-8 ring aromatics, pyrene, anthracene oil, and saturated hydrocarbons, asphaltenes and gums remain. The coated asphalt, prepared by mixing these asphaltenes and gums in a specific ratio, will obviously have a high softening point. This is because removing the low-molecular-weight aromatics and saturated hydrocarbons from the mixture, and then using the remaining asphaltenes and gums to produce the coated asphalt, will inevitably result in a high softening point and a high sintering rate. Furthermore, the removal of metallic carbon particles and other solid impurities from the mixture will ensure a low ash content in the resulting coated asphalt. Additionally, the removal of harmful elements such as sulfur and nitrogen from the mixture will result in a high-quality coated asphalt with low sulfur and nitrogen content. Therefore, the produced coated asphalt will undoubtedly be a high-quality product. In addition, the blending raw materials mentioned above can be used as coating asphalt raw materials, and can also be further blended with aromatics and saturated hydrocarbon extracts to synthesize needle coke, carbon black, and wall-protecting agents as high-end carbon raw materials. Summary of the Invention

[0006] The technical problem to be solved by the embodiments of this application is to improve the existing method of producing coated asphalt using catalytic cracking slurry, which is too complicated, difficult to operate, has low yield, large investment and high production cost.

[0007] To address the aforementioned technical problems, this application provides a device for supercritical carbon dioxide extraction and separation of coal-fired oil slurry, employing the following technical solution: A device for supercritical carbon dioxide extraction and separation of coal-fired oil slurry includes a liquid coal-fired oil slurry output unit, a reagent supply unit, an extraction unit, a separation unit, a carbon dioxide supply unit, and a steam pipeline. The liquid coal-fired oil slurry output unit, the reagent supply unit, the extraction unit, the separation unit, and the carbon dioxide supply unit are connected in sequence. The bottom output end of the medium-pressure carbon dioxide recovery tank of the carbon dioxide supply unit is connected to the input end of the carbon dioxide booster pump of the extraction unit. During extraction and separation, the liquid coal-catalyzed oil slurry output unit outputs liquid coal-catalyzed oil slurry to the chemical supply unit. The liquid coal-catalyzed oil slurry is fully mixed with the chemical solution in the chemical supply unit to form a mixture, which is then injected into the extraction unit. The carbon dioxide supply unit injects supercritical carbon dioxide into the extraction unit to perform countercurrent extraction on the mixture and obtain a first extract, a first extract, and a mixture of residual carbon dioxide.

[0008] Furthermore, the liquid coal-fired oil slurry output unit includes a melting tank, a coal-fired oil slurry extraction pump, and a first heating coil; The first heating coil is located outside the melting tank and is used to heat the melting tank so that the material in the melting tank remains fluid. The input end of the coal-fired oil slurry extraction pump is connected to the output end of the melting tank. The outlet end of the coal-fired oil slurry extraction pump is connected in parallel with the liquid coal tar pitch feed pipeline and then connected to the inlet end of the chemical supply unit. The input end of the first heating coil is connected to the steam pipeline. Further, the chemical supply unit includes a chemical tank, a dosing pump, and a mixer. The output end of the chemical tank is connected to the input end of the dosing pump. The output end of the dosing pump is connected to the radial inlet end of the mixer. The liquid coal-fired oil slurry output unit is connected to the axial inlet end of the mixer. The liquid coal-fired oil slurry and the chemical solution are fully mixed in the mixer to form a mixture.

[0009] Furthermore, the extraction unit includes a mixed liquid booster pump, an extractor, a mixed liquid feed distributor, a packing ring, a second heating coil, a carbon dioxide booster pump, a supercritical carbon dioxide heat exchanger, and a flash tank for solid impurities containing metallic carbon particles. The outlet end of the mixed liquid booster pump is connected to the top inlet end of the extractor, the bottom outlet end of the extractor is connected to the inlet end of the flash tank for solid impurities containing metallic carbon particles, and the top outlet end of the extractor is connected to the upper inlet end of the separation unit. The inlet end of the carbon dioxide booster pump is connected to the bottom outlet end of the medium-pressure carbon dioxide recovery tank. The outlet end of the carbon dioxide booster pump is connected to the tube-side inlet end of the supercritical carbon dioxide heat exchanger, and the tube-side outlet end of the supercritical carbon dioxide heat exchanger is connected to the bottom inlet end of the extractor. The inlet end of the second heating coil is connected to the steam pipeline, and the outlet end of the second heating coil is connected to the condensate inlet end of the lithium bromide absorption chiller.

[0010] Furthermore, the separation unit includes, in sequence, the outlet end of a first pressure-reducing valve, the tube-side inlet end and the tube-side outlet end of a first heater, the top inlet end and the upper outlet end of a first separator, the inlet and outlet ends of a second pressure-reducing valve, the tube-side inlet end and the tube-side outlet end of a second heater, the top inlet end and the upper outlet end of a second separator, the inlet and outlet ends of a third pressure-reducing valve, the tube-side inlet end and the tube-side outlet end of a third heater, the top inlet end and the upper outlet end of a third separator, the inlet and outlet ends of a fourth pressure-reducing valve, the tube-side inlet end and the tube-side outlet end of a fourth heater, the top inlet end and the upper outlet end of a fourth separator, the inlet and outlet ends of a fifth pressure-reducing valve, the tube-side inlet end and the tube-side outlet end of a fifth heater, the top inlet end and the upper outlet end of a fifth separator, the inlet and outlet ends of a sixth pressure-reducing valve, the tube-side inlet end and the tube-side outlet end of a saturated hydrocarbon heat exchanger, the top inlet end and the upper outlet end of a sixth separator, and the inlet and outlet ends of a seventh pressure-reducing valve; The inlet of the first pressure reducing valve is connected to the upper outlet of the extraction unit, the outlet of the seventh pressure reducing valve is connected to the inlet of the medium-pressure carbon dioxide recovery tank, and the separation unit further includes a flash tank with the bottom outlet of the first separator connected in sequence to the inlet and top outlet of the asphalt flash tank, a flash tank with the bottom outlet of the second separator connected in sequence to the inlet and top outlet of the colloidal flash tank, a flash tank with the bottom outlet of the third separator connected in sequence to the inlet and top outlet of the 5-8 ring aromatics flash tank, a flash tank with the bottom outlet of the fourth separator connected in sequence to the inlet and top outlet of the pyrene flash tank, a flash tank with the bottom outlet of the fifth separator connected in sequence to the inlet and top outlet of the anthracene oil flash tank, and a flash tank with the bottom outlet of the sixth separator connected in sequence to the inlet and top outlet of the saturated hydrocarbon flash tank.

[0011] Furthermore, the carbon dioxide supply unit includes a low-pressure carbon dioxide recovery tank, a low-pressure carbon dioxide compressor, a medium-pressure carbon dioxide recovery tank, and a lithium bromide absorption chiller. The inlet end of the low-pressure carbon dioxide recovery tank is connected to the lower outlet end of the separation unit, and the other inlet end of the low-pressure carbon dioxide recovery tank is connected to the outside to replenish carbon dioxide. The top outlet end of the low-pressure carbon dioxide recovery tank is connected to the inlet end of the low-pressure carbon dioxide compressor. The outlet end of the low-pressure carbon dioxide compressor is connected to one inlet end of the medium-pressure carbon dioxide recovery tank. The top inlet end of the medium-pressure carbon dioxide recovery tank is connected to the upper outlet end of the separation unit. The bottom outlet end of the medium-pressure carbon dioxide recovery tank is connected to the inlet end of the carbon dioxide booster pump. The outlet end of the carbon dioxide booster pump is connected to the tube side inlet end of the supercritical carbon dioxide heat exchanger. The cold water inlet end of the medium-pressure carbon dioxide recovery tank is connected to the cold water outlet end of the lithium bromide absorption chiller. The hot water outlet end of the medium-pressure carbon dioxide recovery tank is connected to the hot water inlet end of the lithium bromide absorption chiller. Furthermore, the height-to-diameter ratio of the extractor is from 5:1 to 50:1. Attached Figure Description

[0012] To more clearly illustrate the solution of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0013] Figure 1 This is a process flow diagram of an apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry according to an embodiment of this application.

[0014] Figure 2 This is a flowchart of the liquid coal catalytic oil slurry output unit according to an embodiment of this application.

[0015] Figure 3 This is a flowchart of the drug supply unit according to an embodiment of this application.

[0016] Figure 4 This is a flowchart of the extraction unit in an embodiment of this application.

[0017] Figure 5 This is a flowchart of the separation unit in an embodiment of this application.

[0018] Figure 6 This is a flowchart of the carbon dioxide supply unit according to an embodiment of this application.

[0019] Figure label: 100—Liquid coal catalytic oil slurry output unit; 101—Melting tank; 102—Coal catalytic oil slurry extraction pump; 103—First heating coil; 200—Chemical solution supply unit; 201—Chemical solution tank; 202—Dosing pump; 203—Mixer; 300—Extraction Unit: 301—Mixed Liquid Booster Pump, 302—Extractor, 303—Mixed Liquid Feed Distributor, 304—Packaging Ring, 305—Second Heating Coil, 306—Carbon Dioxide Booster Pump, 307—Supercritical Carbon Dioxide Heat Exchanger, 308—Flash Tank for Metallic Carbon Particles and Solid Impurities; 400—Separation Unit: 401—First Pressure Reducing Valve, 402—First Heater, 403—First Separator, 403 / 1—Asphalt Flash Tank, 404—Second Pressure Reducing Valve, 405—Second Heater, 406—Second Separator, 406 / 1—Gel Flash Tank, 407—Third Pressure Reducing Valve, 408—Third Heater, 409—Third Separator, 409 / 1—5-8 Ring Aromatic Hydrocarbon Flash Tank, 410—Fourth Pressure Reducing Valve, 411—Fourth Heater, 412—Fourth Separator. 412 / 1—Pyrene flash tank; 413—Fifth pressure reducing valve; 414—Fifth heater; 415—Fifth separator; 415 / 1—Anthracene oil flash tank; 416—Sixth pressure reducing valve; 417—Saturated hydrocarbon heat exchanger; 418—Fifth separator; 418 / 1—Saturated hydrocarbon flash tank; 419—Seventh pressure reducing valve; 420—Carbon dioxide cooler; 500—Carbon dioxide supply unit; 501—Low-pressure carbon dioxide recovery tank; 502—Low-pressure carbon dioxide compressor; 503—Medium-pressure carbon dioxide recovery tank; 504—Lithium bromide absorption chiller; 600—Steam pipeline; 700—Solid coal tar pitch; 800—Liquid coal tar pitch. Detailed Implementation

[0020] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs; the terminology used herein in the specification of the application is for the purpose of describing particular embodiments only and is not intended to be limiting of the application; the terms "comprising" and "having," and any variations thereof, in the specification, claims, and foregoing drawings of this application are intended to cover non-exclusive inclusion. The terms "first," "second," and "first" in the specification, claims, or foregoing drawings of this application are used to distinguish different objects, not to describe a particular order.

[0021] In this document, the term "embodiment" means that a particular feature, structure, or characteristic described in connection with an embodiment may be included in at least one embodiment of this application. The appearance of this phrase in various places throughout the specification does not necessarily refer to the same embodiment, nor is it a separate or alternative embodiment mutually exclusive with other embodiments. It will be explicitly and implicitly understood by those skilled in the art that the embodiments described herein can be combined with other embodiments.

[0022] Since matter is composed of particles and forces, and different substances have different particles and forces, their molecular structures also differ. Therefore, coal-catalyzed oil slurry can actually be regarded as a colloidal substance composed of asphaltene, resin, 5-8 ring aromatic hydrocarbons, pyrene, anthracene oil, saturated hydrocarbons and gaseous components arranged in rings from the inside out. Among them, asphaltene has the largest molecular weight, the strongest force and the strongest polarity, and it is located at the center of various colloidal substances. Other types of substances are arranged in order of molecular weight from the inside out. In addition, the metal and carbon particle solid impurities in coal-catalyzed oil slurry are insoluble substances.

[0023] Therefore, this application employs supercritical carbon dioxide, utilizing its strong penetrating power and solubility, as well as the fact that these properties can change with pressure and temperature. This allows it to penetrate between the particles of various colloidal substances. By adjusting the pressure and temperature to a suitable level, supercritical carbon dioxide can dissolve these colloidal substances, achieving the desired extract from the coal-fired oil slurry. Simultaneously, it removes metal and carbon particle solid impurities from the coal-fired oil slurry. Then, it separates asphaltene, gums, 5-8 ring aromatics, pyrene, anthracene oil, and saturated hydrocarbons step by step, facilitating the synthesis of various desired products or raw materials as needed.

[0024] This application provides an apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry. The apparatus can accurately separate the components of the coal-fired oil slurry, thereby improving extraction efficiency and product quality.

[0025] like Figure 1 As shown in the figure, this application provides a device for supercritical carbon dioxide extraction and separation of coal-fired oil slurry, including a liquid coal-fired oil slurry output unit 100, a reagent supply unit 200, an extraction unit 300, a separation unit 400, a carbon dioxide supply unit 500, and a steam pipeline 600. The liquid coal-fired oil slurry output unit 100, the reagent supply unit 200, the extraction unit 300, the separation unit 400, and the carbon dioxide supply unit 500 are connected in sequence. The bottom outlet end of the medium-pressure carbon dioxide recovery tank 503 of the carbon dioxide supply unit 500 is connected to the inlet end of the carbon dioxide booster pump 306 of the extraction unit 300. When the supercritical carbon dioxide extraction and separation device for coal-fired oil slurry enters production, the liquid coal-fired oil slurry output unit 100 outputs liquid coal-fired oil slurry to the chemical supply unit 200. The liquid coal-fired oil slurry is thoroughly mixed with the chemical solution in the chemical supply unit 200 to form a mixture, which is then transported to the top inlet of the extractor 302 in the extraction unit 300. The liquid carbon dioxide in the medium-pressure carbon dioxide recovery tank 503 of the carbon dioxide supply unit 500 is pressurized by the carbon dioxide booster pump 306 and converted into supercritical carbon dioxide after heat exchange in the supercritical carbon dioxide heat exchanger 307, and then transported to the bottom inlet of the extractor 302, where supercritical carbon dioxide is injected into the bottom of the extractor 302. Carbon dioxide is used to countercurrently extract the mixture to obtain a first extract, a first extractant, and a mixture of residual carbon dioxide. The first extract is discharged under reduced pressure from the upper outlet of the extractor 302, and the first extractant and the mixture of residual carbon dioxide are discharged from the bottom outlet of the extractor 302. The separation unit 400 performs separation treatment on the first extract at least six times to obtain more than six kinds of extractants and residual mixtures. The extractants and residual carbon dioxide mixtures are then separated by a flash evaporation process. The extractants are discharged from the bottom outlet of their respective flash tanks, and the residual carbon dioxide is collected in the carbon dioxide supply unit 500 for recycling.

[0026] The asphalt and resin are blended in a certain proportion to form a high-end carbon raw material for coating asphalt, wherein the asphalt content in the coated asphalt raw material is 20% to 80% and the resin content in the coated asphalt raw material is 80% to 20%.

[0027] The carbon dioxide supply unit 500 injects carbon dioxide into the extraction unit 300. After pressurization and heat exchange, the carbon dioxide becomes supercritical carbon dioxide. The supercritical carbon dioxide performs countercurrent extraction on the mixture in the extractor to obtain a first extract, a first extract, and a residual mixture. The first extract and the residual mixture are flashed in a metal carbon particle solid impurity flash tank 308 to separate the extract from the residual carbon dioxide. The first extract is discharged from the bottom outlet of the metal carbon particle solid impurity flash tank 308, and the residual carbon dioxide is collected in the carbon dioxide supply unit 500. Specifically, the discharge of the first extract from the bottom outlet of the metal carbon particle solid impurity flash tank 308 is intermittent, and the first extract is metal carbon particle solid impurity.

[0028] This application provides an apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry. A reagent supply unit 200 provides reagents to thoroughly mix with the coal-fired oil slurry. The reagents demulsify, strongly disperse, and penetrate the slurry, carrying away light components and preventing severe emulsification during mixing with supercritical carbon dioxide. Simultaneously, the thoroughly mixed solution improves the extraction effect and efficiency of supercritical carbon dioxide. By introducing supercritical carbon dioxide and using countercurrent extraction, the useful substances in the coal-fired oil slurry are fully dissolved in the supercritical carbon dioxide, thereby removing metallic carbon particles and solid impurities. Then, through at least six separation processes, asphaltenes, gums, 5-8 ring aromatics, pyrene, anthracene oil, and saturated hydrocarbons are separated, improving the purity and quality of the extract.

[0029] In some embodiments, since coal tar pitch solidifies into a black solid at room temperature with a density of 0.90 g / cm3 to 1.30 g / cm3 and a softening point of 35°C to 95°C, the coal tar pitch to be processed usually exists in a solid form and needs to be melted into liquid coal tar pitch to facilitate subsequent transfer, extraction, and separation steps.

[0030] like Figure 2 As shown, in some embodiments, the liquid coal-fired slurry output unit 100 includes a melting tank 101, a coal-fired slurry extraction pump 102, and a first heating coil 103; the outlet end of the melting tank 101 is connected to the inlet end of the coal-fired slurry extraction pump 102, the outlet end of the coal-fired slurry extraction pump 102 is connected in parallel with the liquid coal tar pitch 800 feed pipeline and then connected to the axial inlet end of the mixer 203, and the inlet end of the first heating coil 103 is connected to the steam pipeline.

[0031] In some embodiments, the melting tank 101 is used to store solid coal tar pitch and 700 and liquid catalytic cracking slurry; In some embodiments, the first heating coil 103 is installed outside the melting tank 101 to heat the material in the melting tank 101, so that the liquid coal-fired oil slurry in the melting tank 101 remains fluid. In this embodiment, the coal-fired oil slurry extraction unit 300 further includes a steam supply pipeline 600, and the heater is a second heating coil 305. The second heating coil 305 is installed outside the extractor 302 cylinder and connected to the steam supply pipeline 600.

[0032] In some embodiments, the input end of the coal-fired oil slurry extraction pump 102 is connected to the melting tank 101, and the output end of the coal-fired oil slurry extraction pump 102 is connected in parallel to the liquid coal tar pitch 800 feed pipeline and then connected to the axial inlet end of the mixer 203. In this embodiment, the steam pipeline 600 outputs low-pressure or medium-pressure steam to the first heating coil 103 to heat the material in the melting tank 101, raising the temperature of the material in the melting tank 101 to 90°C to 145°C, so that the solid or semi-solid coal catalytic oil slurry 700 in the melting tank 101 melts into liquid coal catalytic oil slurry, which is then extracted by the coal catalytic oil slurry extraction pump 102 and transported to the axial inlet end of the mixer 203.

[0033] In other embodiments, the first heating coil 103 may also be connected to a thermal oil furnace, through which thermal oil is introduced into the first heating coil 103 to heat the melting tank 101, so that the coal-fired oil slurry in the melting tank 101 melts to form liquid coal-fired oil slurry.

[0034] In other embodiments, liquid coal tar pitch and catalytic cracking slurry can be directly transported from the outside to mix with the reagent to form a mixture.

[0035] This embodiment of the application sets up a liquid coal-catalyzed oil slurry output unit 100 and combines it with related preparation steps to provide coal-catalyzed oil slurry melted to a liquid state for mixing with the pharmaceutical solution. This fully utilizes the pharmaceutical solution to demulsify and strongly disperse and penetrate the coal-catalyzed oil slurry, thereby increasing the supercritical carbon dioxide extraction rate. Then, through at least six separation processes, asphaltene, gum, 5-8 ring aromatics, pyrene, anthracene oil, and saturated hydrocarbons are separated to improve the purity of the extract and the quality of the product, so as to meet the needs of continuous large-scale industrial production.

[0036] like Figure 3 As shown, in some embodiments, the drug supply unit 200 includes a drug tank 201, a dosing pump 202, and a mixer 203. The drug tank 201 is connected to the input end of the dosing pump 202, and the output end of the dosing pump 202 is connected to the radial input end of the mixer 203.

[0037] The medicine tank 201 is used to store medicine, wherein the medicine comprises medicine and diesel oil, which are mixed under normal temperature and pressure conditions.

[0038] The mixer 203 is provided with an axial inlet end, an axial outlet end, and a radial inlet end; the outlet end of the coal-catalyzed oil slurry extraction pump 102 is connected in parallel with the liquid coal tar pitch 800 feed pipeline and then connected to the axial inlet end of the mixer 203; the output end of the dosing pump 202 is connected to the radial inlet end of the mixer 203; the liquid coal-catalyzed oil slurry and the chemical solution are fully mixed in the mixer 203 to form a mixture.

[0039] When the supercritical carbon dioxide extraction and separation device for coal-fired oil slurry is in operation, the mixed liquid booster pump 301 pressurizes the mixed liquid to 7MPa~40MPa and then transfers it to the top inlet end of the extractor 302.

[0040] In some embodiments, the mass percentage concentration of the drug in the liquid solution is 1% to 60%. Specifically, the mass percentage concentration of the drug can be set to any one of 2%, 5%, 10%, 15%, 20%, 25%, 30%, 40%, and 50%, or a range between any two of these values.

[0041] In some embodiments, the material of the drug is selected from at least one of polyacrylic acid, fatty alcohol ether phosphate, sulfonic acid and sulfonate, sulfate, maleic anhydride sulfonate, alkyl sulfonate, methanol, and toluene; In some embodiments, the amount of the drug solution added to the mixture is 0.85% to 2.50% of the liquid coal catalytic oil slurry. Specifically, the amount of the drug solution added is any one or any two of the following values: 1.0%, 1.5%, 1.7%, 1.9%, and 2% of the liquid coal catalytic oil slurry.

[0042] In this embodiment, liquid coal-catalyzed oil slurry and chemical solution are thoroughly mixed in mixer 203 to form a mixture. The chemical solution is used to demulsify, strongly disperse, and penetrate the coal-catalyzed oil slurry, while simultaneously carrying out light components (such as asphaltene, gum, 5-8 ring aromatics, pyrene, anthracene oil, and saturated hydrocarbons). This facilitates the separation of metallic carbon particle solid impurities from the coal-catalyzed oil slurry in a very short time. Then, asphaltene, gum, 5-8 ring aromatics, pyrene, anthracene oil, and saturated hydrocarbons are separated step by step, thereby improving the extraction and separation efficiency of supercritical carbon dioxide to meet the needs of continuous large-scale industrial production.

[0043] like Figure 4As shown, in some embodiments, the extraction unit 300 includes a mixture booster pump 301, an extractor 302, a mixture feed distributor 303, and a packing ring 304. The device, comprising a second heating coil 305, a carbon dioxide booster pump 306, a supercritical carbon dioxide heat exchanger 307, and a flash tank for solid impurities containing metallic carbon particles 308, is used for supercritical carbon dioxide extraction and separation of coal-fired oil slurry. During operation, the outlet end of the mixed liquid booster pump 301 is connected to the top inlet end of the extractor 302 to inject the mixed liquid into the extractor. The outlet end of the carbon dioxide booster pump 306 is connected to the tube-side inlet end of the supercritical carbon dioxide heat exchanger 307, and the tube-side outlet end of the supercritical carbon dioxide heat exchanger 307 is connected to the bottom inlet end of the extractor 302 to inject supercritical carbon dioxide into the extractor 302. The inlet end of the flash tank for solid impurities containing metallic carbon particles 308 is connected to the bottom outlet end of the extractor 302 to output a mixture of the first extractant and residual carbon dioxide. The second heating coil 305 is located outside the cylinder of the extractor 302 and is used to heat the material at the bottom of the extractor 302.

[0044] Specifically, the height-to-diameter ratio of the extractor 302 is from 5:1 to 50:1. The height-to-diameter ratio of the extractor 302 can be adjusted to any one of the following values ​​or a range between any two values: 6:1, 7:1, 8:1, 9:1, 10:1, 15:1, 20:1, 25:1, 30:1, 35:1, 40:1, and 45:1. The extractor 302 is equipped with a mixed liquid feed distributor 303, which is used to directly transfer the mixed liquid to the packing ring layer and disperse it into the packing ring layer. The extractor 302 is also equipped with a packing ring 304, which is used to allow the mixed liquid to fully countercurrently contact with the supercritical carbon dioxide.

[0045] Furthermore, such as Figure 5As shown, in some embodiments, the separation unit 400 includes, in sequence, the outlet end of a first pressure reducing valve 401, the inlet and outlet ends of a first heater 402, the top inlet and upper outlet end of a first separator 403, the inlet and outlet ends of a second pressure reducing valve 404, the inlet and outlet ends of a second heater 405, the top inlet and upper outlet end of a second separator 406, the inlet and outlet ends of a third pressure reducing valve 407, the inlet and outlet ends of a third heater 408, and the top inlet end of a third separator 409. The inlet and outlet ends of the upper outlet, the inlet and outlet ends of the fourth pressure reducing valve 410, the tube-side inlet and outlet ends of the fourth heater 411, the top inlet and upper outlet ends of the fourth separator 412, the inlet and outlet ends of the fifth pressure reducing valve 413, the tube-side inlet and outlet ends of the fifth heater 414, the top inlet and upper outlet ends of the fifth separator 415, the inlet and outlet ends of the sixth pressure reducing valve 416, the tube-side inlet and outlet ends of the saturated hydrocarbon heat exchanger 417, the top inlet and upper outlet ends of the sixth separator 418, and the inlet end of the seventh pressure reducing valve 419. The inlet end of the first pressure reducing valve 401 is connected to the upper outlet end of the extraction unit 300, and the outlet end of the seventh pressure reducing valve 419 is connected to the inlet end of the medium-pressure carbon dioxide recovery tank 503. The separation unit 400 further includes a pitch flash tank 403 / 1 connected sequentially to the bottom outlet of the first separator 403, a colloidal flash tank 406 / 1 connected sequentially to the bottom outlet of the second separator 406, a 5-8 ring aromatics flash tank 409 / 1 connected sequentially to the bottom outlet of the third separator 409, a pyrene flash tank 412 / 1 connected sequentially to the bottom outlet of the fourth separator 412, and an anthracene oil flash tank 415 connected sequentially to the bottom outlet of the fifth separator 415. The inlet and top outlet of 5 / 1 are sequentially connected to the inlet and top outlet of the saturated hydrocarbon flash tank 418 / 1, which are connected to the bottom outlet of the sixth separator 418. The top outlets of the seven tanks, namely the metal carbon particle solid impurity flash tank 308, the asphalt flash tank 403 / 1, the colloidal flash tank 406 / 1, the 5-8 ring aromatic hydrocarbon flash tank 409 / 1, the pyrene flash tank 412 / 1, the anthracene oil flash tank 415 / 1, and the saturated hydrocarbon flash tank 418 / 1, are connected in parallel and then sequentially connected to the shell-side inlet and shell-side outlet of the carbon dioxide cooler, and then connected to one inlet of the carbon dioxide supply unit.

[0046] Specifically, to facilitate the flash separation of the extract and residual carbon dioxide, the pressure of the seven flash tanks is controlled at 1.2–1.6 MPa, and the temperature is controlled at 95–120°C. In this embodiment, the residual carbon dioxide is cooled to ≤60°C by the carbon dioxide cooler 420 and then transported to the low-pressure carbon dioxide recovery tank 501 via pipeline. After that, it is compressed by the low-pressure carbon dioxide compressor 502 and transported to the medium-pressure carbon dioxide recovery tank 503. Then, the carbon dioxide in the carbon dioxide recovery tank 503 is refrigerated to a liquid state by the lithium bromide absorption chiller 504, so that it can be pressurized by the carbon dioxide booster pump 306 and heat-exchanged by the supercritical carbon dioxide heat exchanger 307 before being transported to the bottom inlet of the extractor 302.

[0047] The liquid carbon dioxide has a temperature of 1–15°C and a pressure of 3.6–5.1 MPa. Specifically, the medium in the 420-tube side of the carbon dioxide cooler is circulating cooling water. Further, such as... Figure 5 As shown, during the operation of the supercritical carbon dioxide extraction and separation device for coal-fired oil slurry, the first extract output from the upper outlet of the extractor under reduced pressure undergoes at least six separation processes to obtain at least six extracts, including the following steps: The first extractant, which is depressurized and output from the upper outlet of the extractor 302, is input into the first separator 403. The first extractant is separated in the first separator 403 to obtain a second extractant, a second extract, and a residual mixture. The second extract and the residual carbon dioxide mixture are further separated to obtain a second extract, which is asphaltenes.

[0048] In this embodiment, the first extract is discharged from the extractor 302 to the first pressure reducing valve 401. The first pressure reducing valve 401 adjusts the pressure of the first extract to 7MPa to 35MPa. Specifically, the pressure of the first extract can be adjusted to any one of 10MPa, 15MPa, 20MPa, 25MPa, and 30MPa, or a range formed between any two of these values.

[0049] The first extract enters the first heater 402 after passing through the first pressure reducing valve 401. The first heater 402 adjusts the temperature of the first extract to 95℃~105℃. Specifically, the temperature of the first extract can be adjusted to any one of 98℃ and 100℃ or a range between any two of these values.

[0050] The second extract is discharged under reduced pressure from the upper outlet end of the first separator 403 and introduced into the second separator 406. The mixture of the second extract and residual carbon dioxide is discharged from the bottom outlet end of the first separator 403. The mixture of the second extract and residual carbon dioxide is transferred to the asphalt flash tank 403 / 1 for flash evaporation to remove the remaining residual carbon dioxide. The second extract is discharged from the bottom outlet end of the asphalt flash tank 403 / 1, and the residual carbon dioxide is discharged from the top outlet end of the asphalt flash tank 403 / 1 and transported through pipeline to the shell-side inlet end of the carbon dioxide cooler 420. In this embodiment, the second extract is asphaltene, the temperature of the flash tank 403 / 1 is 95℃~103℃, and the pressure of the flash tank 403 / 1 is 1.2~1.5MPa. The second extract is passed into the second separator 406, where it is separated to obtain a third extract and a mixture of the third extract and residual carbon dioxide. The mixture of the third extract and residual carbon dioxide is further separated to obtain the third extract, which is a gum.

[0051] In this embodiment, the second extract is discharged from the upper outlet end of the first separator 403 to the second pressure reducing valve 404. The second pressure reducing valve 404 adjusts the pressure of the second extract to 7MPa to 30MPa. Specifically, the pressure of the second extract can be adjusted to any one of 10MPa, 15MPa, 20MPa, and 25MPa, or a range formed between any two of these values.

[0052] The second extract enters the second heater 405 after passing through the second pressure reducing valve 404. The second heater 405 adjusts the temperature of the second extract to 100℃~115℃. Specifically, the temperature of the second extract can be adjusted to any one of 105℃ and 110℃ or a range between any two of these values.

[0053] The third extract is discharged under reduced pressure from the upper outlet end of the second separator 406 and introduced into the third separator 409. The mixture of the third extract and residual carbon dioxide is discharged from the lower end of the second separator 406. The mixture of the third extract and residual carbon dioxide is transferred to the colloidal flash tank 406 / 1 for flash evaporation to remove the remaining residual carbon dioxide. The third extract is discharged from the bottom outlet end of the colloidal flash tank 406 / 1, and the residual carbon dioxide is discharged from the top outlet end of the colloidal flash tank 406 / 1 and transported through pipeline to the shell-side inlet end of the carbon dioxide cooler 420. In this embodiment, the third extract is a colloid, the temperature of the flash evaporator 406 / 1 is 95℃~110℃, and the pressure of the flash evaporator 406 / 1 is 1.2~1.5MPa. The third extract is passed into the third separator 409, where it is separated to obtain a fourth extract, a fourth extract, and a mixture of residual carbon dioxide. The mixture of the fourth extract and residual carbon dioxide is further separated to obtain the fourth extract, which is a 5-8 ring aromatic hydrocarbon.

[0054] In this embodiment, the third extract is discharged from the upper outlet end of the second separator 406 to the third pressure reducing valve 410. The third pressure reducing valve 410 adjusts the pressure of the third extract to 7MPa to 25MPa. Specifically, the pressure of the third extract can be adjusted to any one of 10MPa, 15MPa, and 20MPa or a range formed between any two of these values.

[0055] The third extract enters the third heater 408 after passing through the third pressure reducing valve 407. The third heater 408 adjusts the temperature of the third extract to 105℃~118℃. Specifically, the temperature of the third extract can be adjusted to any one of 110℃ and 115℃ or a range between any two of these values.

[0056] The fourth extract is discharged under reduced pressure from the upper outlet of the third separator 409 and fed into the fourth separator 412. The mixture of the fourth extract and residual carbon dioxide is discharged from the bottom outlet of the third separator 409. The mixture of the fourth extract and residual carbon dioxide is then transferred to the 5-8 ring aromatics flash tank 409 / 1 for flash evaporation to remove the remaining residual carbon dioxide. The fourth extract is then discharged from the bottom outlet of the 5-8 ring aromatics flash tank 409 / 1, and the aforementioned residual carbon dioxide is discharged from the top outlet of the 5-8 ring aromatics flash tank 409 / 1 and transferred through pipeline to the second separator 412. At the shell-side inlet of the carbon oxidizing cooler 420, in this embodiment, the fourth extract is a 5-8 ring aromatic hydrocarbon. The temperature of the flash tank 409 / 1 is 100℃-115℃, and the pressure of the flash tank 409 / 1 is 1.2-1.5MPa. The fourth extract is passed into the fourth separator 412, where it is separated to obtain a fifth extract, a fifth extract, and a mixture of residual carbon dioxide. The fifth extract and the mixture of residual carbon dioxide are further separated to obtain the fifth extract, which is pyrene.

[0057] In this embodiment, the fourth extract is discharged from the upper outlet end of the third separator 409 to the fourth pressure reducing valve 410. The fourth pressure reducing valve 410 adjusts the pressure of the fourth extract to 7MPa to 15MPa. Specifically, the pressure of the fourth extract can be adjusted to any one of 10MPa or any range between two values.

[0058] The fourth extract enters the fourth heater 411 after passing through the fourth pressure reducing valve 410. The fourth heater 411 adjusts the temperature of the fourth extract to 110℃~120℃. Specifically, the temperature of the fourth extract can be adjusted to any one of 115℃ and 118℃ or a range between any two of these values.

[0059] The fifth extract is discharged under reduced pressure from the upper outlet of the fourth separator 412 and fed into the fifth separator 415. The mixture of the fifth extract and residual carbon dioxide is discharged from the bottom outlet of the fourth separator 412. The mixture of the fifth extract and residual carbon dioxide is then transferred to the pyrene flash tank 412 / 1 for flash evaporation to remove the remaining residual carbon dioxide. The fifth extract is discharged from the bottom outlet of the pyrene flash tank 412 / 1, and the residual carbon dioxide is discharged from the top outlet of the pyrene flash tank 412 / 1 and transported through pipeline to a carbon dioxide cooling system. At the inlet of device 420, in this embodiment, the fifth extract is pyrene. The temperature of flash tank 412 / 1 is 105℃~115℃, and the pressure of flash tank 412 / 1 is 1.2~1.5MPa. The fifth extract is passed into the fifth separator 415, where it is separated to obtain a sixth extract, a sixth extract, and a mixture of residual carbon dioxide. The sixth extract and the mixture of residual carbon dioxide are further separated to obtain the sixth extract, which is anthracene oil.

[0060] In this embodiment, the fifth extract is discharged from the upper outlet end of the fourth separator 412 to the fifth pressure reducing valve 413. The fifth pressure reducing valve 413 adjusts the pressure of the fifth extract to 7MPa to 10MPa. Specifically, the pressure of the fifth extract can be adjusted to any one of 8MPa and 9MPa or a range formed between any two values.

[0061] The fifth extract enters the fifth heater 414 after passing through the fifth pressure reducing valve 413. The fifth heater 414 adjusts the temperature of the fifth extract to 115℃~125℃. Specifically, the temperature of the fifth extract can be adjusted to any one of 120℃ and 122℃ or a range between any two of these values.

[0062] The sixth extract is discharged under reduced pressure from the upper outlet of the fifth separator 415 and fed into the sixth separator 418. The mixture of the sixth extract and residual carbon dioxide is discharged from the bottom outlet of the fifth separator 415. The mixture of the sixth extract and residual carbon dioxide is then transferred to anthracene oil flash tank 415 / 1 for flash evaporation to remove the remaining residual carbon dioxide. The sixth extract is discharged from the bottom outlet of the anthracene oil flash tank 415 / 1, and the aforementioned residual carbon dioxide is discharged from the top outlet of the anthracene oil flash tank 415 / 1 and transported to the carbon dioxide cooler 42 via pipeline. At the shell-side inlet end, in this embodiment, the sixth extract is anthracene oil. The temperature of the flash tank 415 / 1 is 110℃~120℃, and the pressure of the flash tank 415 / 1 is 1.2~1.5MPa. The sixth extract is passed into the sixth separator 418, where it is separated to obtain a mixture of carbon dioxide that has de-supercriticaled, the seventh extract, and residual carbon dioxide. The mixture of the seventh extract and residual carbon dioxide is further separated to obtain the seventh extract, which is a saturated hydrocarbon.

[0063] In this embodiment, the pressure of the sixth separator 418 is regulated to 0.5–0.6 MPa by the sixth reducing valve 416, and the temperature is regulated to 50–55°C by the saturated hydrocarbon heat exchanger 417, causing the medium inside the sixth separator 418 to leave the supercritical state. This facilitates the separation of carbon dioxide and saturated hydrocarbons. In this embodiment, the seventh extractant is carbon dioxide, and the medium in the shell side of the saturated hydrocarbon heat exchanger 417 is catalytic cracking slurry. The carbon dioxide is discharged from the upper outlet of the sixth separator 418 and fed into the medium-pressure carbon dioxide recovery tank 503, while the seventh extractant is discharged from the bottom outlet of the sixth separator 418. The mixture of the seventh extract and residual carbon dioxide is transferred to a saturated hydrocarbon flash evaporator 418 / 1 for flash evaporation to remove the remaining residual carbon dioxide. The seventh extract is discharged from the bottom outlet of the saturated hydrocarbon flash evaporator 418 / 1, and the residual carbon dioxide is discharged from the top outlet of the saturated hydrocarbon flash evaporator 418 / 1 and transported via pipeline to the shell-side inlet of the carbon dioxide cooler 420. The seventh extract is a saturated hydrocarbon. The temperature of the flash evaporator 418 / 1 is 45℃~50℃, and the pressure of the flash evaporator 418 / 1 is 0.5~0.6MPa. Further, such as... Figure 6As shown, the carbon dioxide supply unit 500 includes: a low-pressure carbon dioxide recovery tank 501, a low-pressure carbon dioxide compressor 502, a medium-pressure carbon dioxide recovery tank 503, and a lithium bromide absorption chiller 504. The residual carbon dioxide is cooled by the carbon dioxide cooler 420 and then transported to the low-pressure carbon dioxide recovery tank 501 through pipelines. After that, it is compressed by the low-pressure carbon dioxide compressor 502 and transported to the medium-pressure carbon dioxide recovery tank 503. Then, the carbon dioxide in the medium-pressure carbon dioxide recovery tank 503 is frozen to a liquid state by the lithium bromide absorption chiller 504, so that it can be pressurized by the carbon dioxide booster pump 306 and then heat-exchanged by the supercritical carbon dioxide heat exchanger 307 and transported to the bottom inlet end of the extractor 302.

[0064] Specifically, the other inlet of the low-pressure carbon dioxide recovery tank 501 is connected to the outside world for filling or replenishing carbon dioxide from the outside.

[0065] Specifically, the medium input to the tube side of the carbon dioxide cooler 420 is circulating cooling water. The cooling water cools the low-pressure carbon dioxide in the shell side to below 60°C, so that the low-pressure carbon dioxide can be compressed to 3.6-5.1 MPa by the low-pressure carbon dioxide compressor 502 and transferred to the medium-pressure carbon dioxide recovery tank 503. The liquid carbon dioxide in the medium-pressure carbon dioxide recovery tank 503 is pressurized by the carbon dioxide booster pump 306 and heat-exchanged by the supercritical carbon dioxide heat exchanger 307, and has been converted into supercritical carbon dioxide. The pressure of the supercritical carbon dioxide is 7-40 MPa, the temperature is 32°C-115°C, and the concentration of the carbon dioxide is 95%-99.9%.

[0066] Furthermore, the steam pipeline 600 is connected in parallel to the steam inlet ends of seven devices: the first heater 402, the second heater 405, the third heater 408, the fourth heater 411, the fifth heater 414, the supercritical carbon dioxide heat exchanger 307, and the second coil 305. This connection is used to heat the materials within these seven devices. The steam condensate outlet ends, after heat exchange with the materials in these seven devices, are connected in parallel and flow into the condensate inlet end of the lithium bromide absorption chiller 504. The residual heat of the steam condensate is used to heat the lithium bromide, causing it to vaporize and absorb heat from the chilled water. After cooling, the chilled water is used to cool the carbon dioxide in the medium-pressure carbon dioxide recovery tank 503, causing the carbon dioxide to cool and become liquid carbon dioxide.

[0067] The liquid carbon dioxide in the medium-pressure carbon dioxide recovery tank 503 has a temperature of 1–15°C and a pressure of 3.6–5.1 MPa. Obviously, the embodiments described above are only some embodiments of this application, not all embodiments. The accompanying drawings show preferred embodiments of this application, but do not limit the patent scope of this application. This application can be implemented in many different forms; conversely, the purpose of providing these embodiments is to make the understanding of the disclosure of this application more thorough and comprehensive. Although this application has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing specific embodiments, or make equivalent substitutions for some of the technical features. Any equivalent structures made using the content of this application's specification and drawings, directly or indirectly applied to other related technical fields, are similarly within the scope of patent protection of this application.

Claims

1. A device for supercritical carbon dioxide extraction and separation of coal-fired oil slurry, characterized in that, The system includes a liquid coal catalytic oil slurry output unit, a chemical supply unit, an extraction unit, a separation unit, a carbon dioxide supply unit, and a steam pipeline. The liquid coal catalytic oil slurry output unit, the chemical supply unit, the extraction unit, the separation unit, and the carbon dioxide supply unit are connected in sequence. The bottom output end of the medium-pressure carbon dioxide recovery tank of the carbon dioxide supply unit is connected to the input end of the carbon dioxide booster pump of the extraction unit. During extraction and separation, the liquid coal catalytic oil slurry output unit outputs liquid coal catalytic oil slurry to the chemical supply unit. The liquid coal catalytic oil slurry is fully mixed with the chemical solution in the chemical supply unit to form a mixture, which is then injected into the extraction unit. The carbon dioxide supply unit injects supercritical carbon dioxide into the extraction unit to perform countercurrent extraction on the mixture and obtain a first extract, a first extract, and a mixture of residual carbon dioxide.

2. The apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry according to claim 1, characterized in that, The liquid coal catalytic oil slurry output unit includes a melting tank, a coal catalytic oil slurry extraction pump, and a first heating coil. The first heating coil is located outside the melting tank and is used to heat the melting tank to keep the material in the melting tank fluid. The input end of the coal catalytic oil slurry extraction pump is connected to the output end of the melting tank, and the outlet end of the coal catalytic oil slurry extraction pump is connected in parallel with the liquid coal tar pitch feed pipeline and then connected to the inlet end of the liquid supply unit. The input end of the first heating coil is connected to the steam pipeline.

3. The apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry according to claim 1, characterized in that, The liquid supply unit includes a liquid tank, a dosing pump, and a mixer. The output end of the liquid tank is connected to the input end of the dosing pump, the output end of the dosing pump is connected to the radial inlet end of the mixer, and the liquid coal catalytic oil slurry output unit is connected to the axial inlet end of the mixer. The liquid coal catalytic oil slurry and the liquid are fully mixed in the mixer to form a mixture.

4. The apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry according to claim 1, characterized in that, The extraction unit includes a mixed liquid booster pump, an extractor, a mixed liquid feed distributor, a packing ring, a second heating coil, a carbon dioxide booster pump, a supercritical carbon dioxide heat exchanger, and a flash tank for solid impurities containing metallic carbon particles. The outlet end of the mixed liquid booster pump is connected to the top inlet end of the extractor, the bottom outlet end of the extractor is connected to the inlet end of the flash tank for solid impurities containing metallic carbon particles, and the top outlet end of the extractor is connected to the upper inlet end of the separation unit. The inlet end of the carbon dioxide booster pump is connected to the bottom outlet end of the medium-pressure carbon dioxide recovery tank. The outlet end of the carbon dioxide booster pump is connected to the tube-side inlet end of the supercritical carbon dioxide heat exchanger, and the tube-side outlet end of the supercritical carbon dioxide heat exchanger is connected to the bottom inlet end of the extractor. The inlet end of the second heating coil is connected to the steam pipeline, and the outlet end of the second heating coil is connected to the condensate inlet end of the lithium bromide absorption chiller.

5. The apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry according to claim 1, characterized in that, The separation unit includes, in sequence, the outlet end of a first pressure reducing valve, the tube-side inlet end and the tube-side outlet end of a first heater, the top inlet end and the upper outlet end of a first separator, the inlet and outlet ends of a second pressure reducing valve, the tube-side inlet end and the tube-side outlet end of a second heater, the top inlet end and the upper outlet end of a second separator, the inlet and outlet ends of a third pressure reducing valve, the tube-side inlet end and the tube-side outlet end of a third heater, the top inlet end and the upper outlet end of a third separator, the inlet and outlet ends of a fourth pressure reducing valve, the tube-side inlet end and the tube-side outlet end of a fourth heater, the top inlet end and the upper outlet end of a fourth separator, the inlet and outlet ends of a fifth pressure reducing valve, the tube-side inlet end and the tube-side outlet end of a fifth heater, the top inlet end and the upper outlet end of a fifth separator, the inlet and outlet ends of a sixth pressure reducing valve, the tube-side inlet end and the tube-side outlet end of a saturated hydrocarbon heat exchanger, the top inlet end and the upper outlet end of a sixth separator, and the inlet and outlet ends of a seventh pressure reducing valve. The inlet end of the first pressure reducing valve is connected to the upper outlet end of the extraction unit, and the outlet end of the seventh pressure reducing valve is connected to the inlet end of the medium-pressure carbon dioxide recovery tank. The separation unit further includes a flash tank inlet and top outlet connected sequentially to the bottom outlet of the first separator, a flash tank inlet and top outlet connected sequentially to the bottom outlet of the second separator, a flash tank inlet and top outlet connected sequentially to the bottom outlet of the third separator, a flash tank inlet and top outlet connected sequentially to the bottom outlet of the third separator, a flash tank inlet and top outlet connected sequentially to the bottom outlet of the fourth separator, a flash tank inlet and top outlet connected sequentially to the bottom outlet of the fifth separator, and a flash tank inlet and top outlet connected sequentially to the bottom outlet of the sixth separator.

6. The apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry according to claim 1, characterized in that, The carbon dioxide supply unit includes a low-pressure carbon dioxide recovery tank, a low-pressure carbon dioxide compressor, a medium-pressure carbon dioxide recovery tank, and a lithium bromide absorption chiller. The inlet end of the low-pressure carbon dioxide recovery tank is connected to the lower outlet end of the separation unit, and the other inlet end of the low-pressure carbon dioxide recovery tank is connected to the outside to replenish carbon dioxide. The top outlet end of the low-pressure carbon dioxide recovery tank is connected to the inlet end of the low-pressure carbon dioxide compressor. The outlet end of the low-pressure carbon dioxide compressor is connected to one inlet end of the medium-pressure carbon dioxide recovery tank. The top inlet end of the medium-pressure carbon dioxide recovery tank is connected to the upper outlet end of the separation unit. The bottom outlet end of the medium-pressure carbon dioxide recovery tank is connected to the inlet end of the carbon dioxide booster pump. The outlet end of the carbon dioxide booster pump is connected to the tube-side inlet end of the supercritical carbon dioxide heat exchanger. The cold water inlet end of the medium-pressure carbon dioxide recovery tank is connected to the cold water outlet end of the lithium bromide absorption chiller, and the hot water outlet end of the medium-pressure carbon dioxide recovery tank is connected to the hot water inlet end of the lithium bromide absorption chiller.

7. The apparatus for supercritical carbon dioxide extraction and separation of coal-fired oil slurry according to claim 4, characterized in that, The height-to-diameter ratio of the extractor is from 5:1 to 50:1.

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