Coal tar pitch extraction equipment

Abstract

The utility model belongs to the technical field of coal pitch processing, and relates to coal pitch extraction equipment which comprises a liquid coal pitch output device, a first solution supply device, a first extraction device and a supercritical carbon dioxide supply device, and the liquid coal pitch output device, the first solution supply device and the first extraction device are sequentially connected. The supercritical carbon dioxide supply device is connected with the first extraction device. According to the technical scheme provided by the invention, each component of the coal pitch can be accurately separated, the extraction efficiency is improved, and the product quality of an extracted substance is improved.

Description

Technical Field

[0001] The present application relates to the technical field of coal tar processing, and more specifically, to a coal tar extraction device. Background Art

[0002] Coal tar is obtained by placing coal in a distillation furnace and distilling it at 450℃~950℃. After the coal tar is distilled and cut through a normal and low-pressure distillation device to extract the light components, a black viscous liquid is obtained at the bottom of the vacuum tower. It will solidify at room temperature to form a black solid substance.

[0003] The coal tar was analyzed by spectroscopy and mass spectrometry. In addition to containing a large amount of asphaltene and a small amount of metal and solid waste, it also contains a large amount of colloids, aromatic hydrocarbons (anthracene, phenanthrene, naphthalene, fluorene, acenaphthene, pyrene, phenylene, chrysene, indene, biphenyl), saturated hydrocarbons and other substances. These substances are valuable building materials and chemical raw materials.

[0004] In order to extract useful substances from coal tar, extraction methods are usually used to process coal tar. However, traditional extraction methods require a large amount of solvents and equipment to extract a single substance. The process is complex, the operation is difficult, the extraction rate is slow and the production cost is high. At the same time, due to the large amount of solvent used, the extracted substance is mixed with other materials, resulting in poor product quality. Utility Model Content

[0005] The technical problem to be solved by the embodiments of the present application is that the existing extraction method for coal tar is complex in process, difficult to operate, slow in extraction rate, high in production cost and poor in quality of the extracted product.

[0006] In order to solve the above technical problems, the present invention provides a coal tar pitch extraction device, which adopts the following technical solution:

[0007] A coal tar pitch extraction device comprises a liquid coal tar pitch output device, a first solution supply device, a first extraction device and a supercritical carbon dioxide supply device, wherein the liquid coal tar pitch output device, the first solution supply device and the first extraction device are connected in sequence, and the supercritical carbon dioxide supply device is connected to the first extraction device;

[0008] During operation, the liquid coal tar output device outputs liquid coal tar to the first solution supply device. The liquid coal tar is fully mixed with the first solution in the first solution supply device to form a first mixed solution, which is then injected into the first extraction device. The supercritical carbon dioxide supply device injects supercritical carbon dioxide into the first extraction device to perform countercurrent extraction on the first mixed solution to obtain a first extraction substance.

[0009] Furthermore, the liquid coal tar pitch output device includes a first storage tank, a heating device and a coal tar pitch extraction pump;

[0010] The heating device is installed outside the first storage tank and is used to heat the first storage tank to keep the liquid coal tar pitch in the first storage tank fluid;

[0011] The input end of the coal tar extraction pump is connected to the first storage tank.

[0012] Furthermore, the first solution supply device includes a first liquid storage tank, a first dosing pump and a first mixer, the first liquid storage tank is connected to the input end of the first dosing pump, and the output end of the first dosing pump is connected to the first mixer;

[0013] The first mixer includes an axially arranged first inlet and a first outlet, and a radially arranged second inlet; the liquid coal tar pitch output device is connected to the first inlet, the output end of the first dosing pump is connected to the second inlet, and the first outlet is connected to the first extraction device;

[0014] The liquid coal tar pitch and the first solution are fully mixed in the first mixer to form a first mixed solution.

[0015] Furthermore, the first extraction device includes a first extractor, at least one first adjustment component, and at least one separator, wherein the first extractor has a first input port located at the top, a second input port located at the bottom, and a first output port disposed near the first input port; the first solution supply device is connected to the first input port, the supercritical carbon dioxide supply device is connected to the second input port, and the first output port is connected to the separator;

[0016] The first regulating component is installed between the first solution supply device and the first extractor, and between the first extractor and the separator, and is used to regulate the pressure or temperature of the first mixed solution and the first extraction substance;

[0017] During operation, the first mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the first extractor to perform countercurrent extraction to obtain a supernatant and a precipitate. The supernatant is injected into the separator through the first output port for separation treatment to obtain the first extract material.

[0018] Furthermore, the first extraction device includes a first separator, a second separator, and a third separator; the input end of the first separator is connected to the first output port of the first extractor, the input end of the second separator is connected to the output end of the first separator, the input end of the third separator is connected to the output end of the second separator, and the output end of the third separator is connected to the supercritical carbon dioxide supply device;

[0019] The first adjusting component is installed between two adjacent separators.

[0020] Furthermore, the coal tar extraction equipment further includes a second solution supply device and a second extraction device, the input end of the second solution supply device is connected to the output end of one of the separators, the output end of the second solution supply device is connected to the second extraction device, and the supercritical carbon dioxide supply device is connected to the second extraction device;

[0021] During operation, the separator outputs the first extraction substance to the second solution supply device. The first extraction substance is fully mixed with the second solution in the second solution supply device to form a second mixed solution, which is then injected into the second extraction device. The supercritical carbon dioxide supply device injects supercritical carbon dioxide into the second extraction device to perform countercurrent extraction on the second mixed solution to obtain the second extraction substance.

[0022] Furthermore, the second solution supply device includes a second liquid storage tank, a second dosing pump and a second mixer, the second liquid storage tank is connected to the input end of the second dosing pump, and the output end of the second dosing pump is connected to the second mixer;

[0023] The second mixer includes an axially arranged third inlet and a second outlet, and a radially arranged fourth inlet; the output end of the separator is connected to the third inlet, the output end of the second dosing pump is connected to the fourth inlet, and the second outlet is connected to the second extraction device;

[0024] The first extraction material and the second solution are fully mixed in the second mixer to form a second mixed solution.

[0025] Furthermore, the second extraction device includes a second extractor, at least one second adjustment component, and at least one separator, wherein the second extractor has a third input port located at the top, a fourth input port located at the bottom, and a second output port disposed near the third input port; the second solution supply device is connected to the third input port, the supercritical carbon dioxide supply device is connected to the fourth input port, and the second output port is connected to the separator;

[0026] The second regulating component is installed between the second solution supply device and the second extractor, and between the second extractor and the separator, and is used to regulate the pressure or temperature of the second mixed solution and the second extraction substance;

[0027] During operation, the second mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the second extractor to perform countercurrent extraction to obtain a supernatant and a precipitate. The supernatant is injected into the separator through the second output port for separation treatment to obtain the second extract material.

[0028] Furthermore, the second extraction device includes a fourth separator, a fifth separator, and a sixth separator; the input end of the fourth separator is connected to the second output port of the second extractor, the input end of the fifth separator is connected to the output end of the fourth separator, the input end of the sixth separator is connected to the output end of the fifth separator, and the output end of the sixth separator is connected to the supercritical carbon dioxide supply device;

[0029] The second adjusting assembly is installed between two adjacent separators.

[0030] Furthermore, the supercritical carbon dioxide supply device includes a second storage tank, a cooling component and a pressurizing component;

[0031] The second storage tank is used to store carbon dioxide;

[0032] The cooling assembly includes a cooling coil and a cooling medium supplier, wherein the cooling coil is installed outside the second storage tank, and the cooling medium supplier is connected to the cooling coil;

[0033] The pressurizing component is connected to the bottom of the second storage tank and is used for pressurizing the carbon dioxide output from the second storage tank.

[0034] Compared with the prior art, the embodiments of the present application have the following beneficial effects:

[0035] The present invention provides a coal tar pitch extraction device. A first solution supply device is provided to provide a first solution for thorough mixing with the coal tar pitch. The first solution is used to demulsify, strongly disperse, and penetrate the coal tar pitch, and to carry out light components. This prevents severe emulsification caused by the mixing of supercritical carbon dioxide and coal tar pitch. At the same time, the thoroughly mixed first mixed solution can improve the extraction effect and efficiency of the supercritical carbon dioxide.

[0036] By introducing supercritical carbon dioxide and combining it with a countercurrent extraction method, the useful substances in coal tar are fully dissolved in supercritical carbon dioxide, thereby removing asphaltene, solid waste and metal substances in the coal tar, thereby improving the purity of the extracted substances and improving the product quality of the extracted substances. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] In order to more clearly illustrate the solution of the present application, a brief introduction is given below to the drawings required for use in the description of the embodiments. Obviously, the drawings described below are some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without any creative work.

[0038] Figure 1 This is a process flow chart of the coal tar extraction equipment of an embodiment of the present application.

[0039] Reference numerals:

[0040] 100, liquid coal tar output device; 101, first storage tank; 102, coal tar extraction pump; 200, first solution supply device; 201, first liquid storage tank; 202, first dosing pump; 203, first mixer; 300, first extraction device; 301, first extractor; 302, first separator; 303, second separator; 304, third separator; 305, first booster pump; 306, first pressure reducing valve; 307, first heater; 308, second pressure reducing valve; 309, second heater; 310, third pressure reducing valve; 311, fourth pressure reducing valve; 400, second solution supply device; 401, second liquid storage tank; 402, second dosing pump; 403, second mixer; 500. Second extraction device; 501. Second extractor; 502. Fourth separator; 503. Fifth separator; 504. Sixth separator; 505. Second booster pump; 506. Fifth pressure reducing valve; 507. Third heater; 508. Sixth pressure reducing valve; 509. Fourth heater; 510. Seventh pressure reducing valve; 511. Eighth pressure reducing valve; 600. Supercritical carbon dioxide supply device; 601. Second storage tank; 602. Cooling medium supply device; 603. Cooling coil; 604. Third booster pump; 605. Fourth booster pump; 700. Water vapor supply device; 701. First heating coil; 702. Second heating coil; 703. Third heating coil; 800. Coal tar solid. DETAILED DESCRIPTION

[0041] Unless otherwise defined, all technical and scientific terms used herein have the same meanings as commonly understood by those skilled in the art to which this application belongs. The terms used in the specification of the application are only for the purpose of describing specific embodiments and are not intended to limit this application. The terms "including" and "having" and any variations thereof in the specification and claims of this application and the above-mentioned drawings are intended to cover non-exclusive inclusions. The terms "first", "second", etc. in the specification and claims of this application or the above-mentioned drawings are used to distinguish different objects, not to describe a specific order.

[0042] References herein to "embodiments" mean that a particular feature, structure, or characteristic described in connection with the embodiments may be included in at least one embodiment of the present application. The appearance of this phrase in various places in the specification does not necessarily refer to the same embodiment, nor does it constitute an independent or alternative embodiment that is mutually exclusive of other embodiments. It is understood, both explicitly and implicitly, by those skilled in the art that the embodiments described herein may be combined with other embodiments.

[0043] Since matter is composed of particles and forces, different substances have different particles and forces, and their molecular structures are also different. Therefore, coal tar can actually be regarded as a colloid composed of asphaltene, gum, aromatic hydrocarbons, saturated hydrocarbons and gas components that are ring-shaped from the inside to the outside. Among them, asphaltene has the largest molecular weight, the greatest force and the strongest polarity. It is located in the center of various colloids. Other types of substances are arranged from the inside to the outside according to their molecular weight.

[0044] Therefore, the present application adopts supercritical carbon dioxide, utilizing its characteristics of not only strong permeability and solubility, but also the characteristics that the permeability and solubility can change with changes in pressure and temperature, so that it can penetrate into the particles of each colloid. By adjusting to appropriate pressure and temperature, the supercritical carbon dioxide has the ability to dissolve each colloid, thereby achieving the effect of extracting relevant extraction substances from coal tar; at the same time, by further adjusting to appropriate pressure and temperature to further change the solubility of supercritical carbon dioxide, each extraction substance is precipitated from the solution and extracted, thereby achieving the effect of separating each extraction substance one by one.

[0045] However, when using supercritical carbon dioxide to extract oil sludge, the extraction rate is low and does not meet the needs of continuous large-scale industrial production.

[0046] Therefore, based on the above working principle and existing technical defects, an embodiment of the present application provides a coal tar extraction device, which can accurately separate the various components of coal tar, improve the extraction efficiency and improve the product quality of the extracted material.

[0047] See also Figure 1As shown, an embodiment of the present application provides a coal tar extraction device, including a liquid coal tar output device 100, a first solution supply device 200, a first extraction device 300 and a supercritical carbon dioxide supply device 600, wherein the liquid coal tar output device 100, the first solution supply device 200 and the first extraction device 300 are connected in sequence, and the supercritical carbon dioxide supply device 600 is connected to the first extraction device 300.

[0048] When the coal tar extraction equipment is working, the liquid coal tar output device 100 outputs liquid coal tar to the first solution supply device 200. The liquid coal tar is fully mixed with the first solution in the first solution supply device 200 to form a first mixed solution, and is injected into the first extraction device 300. The supercritical carbon dioxide supply device 600 injects supercritical carbon dioxide into the first extraction device 300 to perform countercurrent extraction on the first mixed solution to obtain a first extraction substance.

[0049] An embodiment of the present application provides a coal tar extraction device, which provides a first solution for thorough mixing with the coal tar by providing a first solution supply device 200, and utilizes the first solution to demulsify, strongly disperse, and penetrate the coal tar, and to carry out light components, thereby avoiding serious emulsification caused by the mixing of supercritical carbon dioxide and coal tar. At the same time, the thoroughly mixed first mixed solution can improve the extraction effect and extraction efficiency of supercritical carbon dioxide; by introducing supercritical carbon dioxide and coordinating with a countercurrent extraction treatment method, the useful substances in the coal tar are fully dissolved in the supercritical carbon dioxide, thereby eliminating asphaltene, solid waste, and metal substances in the coal tar, thereby improving the purity of the extracted substances and improving the product quality of the extracted substances.

[0050] In some embodiments, since coal tar will solidify to form a black solid under normal temperature conditions, its density is 0.90g / cm3~1.30g / cm3, and its softening point is 35℃~95℃, therefore, the coal tar to be treated usually exists in the form of coal tar solid, which needs to be melted to form liquid coal tar for subsequent extraction and separation steps.

[0051] See also Figure 1 As shown, in some embodiments, the liquid coal tar output device 100 includes a first storage tank 101 , a heating device and a coal tar extraction pump 102 .

[0052] In some embodiments, the first storage tank 101 is used to store coal tar pitch solids 800;

[0053] In some embodiments, the heating device is installed outside the first storage tank 101 and is used to heat the first storage tank 101 so that the liquid coal tar in the first storage tank 101 maintains fluidity. In this embodiment, the coal tar extraction equipment also includes a water vapor supply device 700, and the heating device is a first heating coil 701. The first heating coil 701 is installed outside the first storage tank 101 and is connected to the water vapor supply device 700.

[0054] In some embodiments, the input end of the coal tar extraction pump 102 is connected to the first storage tank 101 .

[0055] In this embodiment, the water vapor supply device 700 outputs low-pressure water vapor or medium-pressure water vapor into the first heating coil 701 to heat the first storage tank 101, so that the temperature in the first storage tank 101 is heated to 120°C to 160°C, so that the coal tar solid 800 in the first storage tank 101 is melted to form liquid coal tar, which is then extracted by the coal tar extraction pump 102 and moved toward the first extraction device 300.

[0056] In other embodiments, the first heating coil 701 may also be connected to a thermal oil furnace, and thermal oil may be input into the first heating coil 701 through the thermal oil furnace to heat the first storage tank 101, so that the coal tar in the first storage tank 101 is melted to form liquid coal tar.

[0057] In other embodiments, liquid coal tar can be directly delivered from the outside to mix with the first solution to form the first mixed solution.

[0058] The embodiment of the present application provides a liquid coal tar output device 100 and combines it with relevant preparation steps to provide coal tar melted into a liquid state for mixing with the first solution, giving full play to the first solution to demulsify, strongly disperse and penetrate the coal tar, thereby improving the supercritical carbon dioxide extraction rate to meet the needs of continuous large-scale industrial production.

[0059] Please continue reading Figure 1 As shown, in some embodiments, the first solution supply device 200 includes a first liquid storage tank 201, a first dosing pump 202 and a first mixer 203, the first liquid storage tank 201 is connected to the input end of the first dosing pump 202, and the output end of the first dosing pump 202 is connected to the first mixer 203.

[0060] The first liquid storage tank 201 is used to store a first solution, wherein the first solution includes a first drug and diesel, and the first drug and diesel are mixed under normal temperature and pressure conditions.

[0061] The first mixer 203 includes an axially arranged first inlet and a first outlet, and a radially arranged second inlet; the liquid coal tar output device 100 is connected to the first inlet, the output end of the first dosing pump 202 is connected to the second inlet, and the first outlet is connected to the first extraction device 300.

[0062] When the coal tar pitch extraction equipment is in operation, the liquid coal tar pitch and the first solution are fully mixed in the first mixer 203 to form a first mixed solution.

[0063] In some embodiments, in the first solution, the mass percentage concentration of the first drug is 1% to 30%. Specifically, the mass percentage concentration of the first drug can be set to any one of 1%, 2%, 5%, 10%, 15%, 20%, 25%, 30% or a range formed between any two values.

[0064] In some embodiments, the material of the first drug is selected from at least one of fatty alcohol ether phosphate, polycarboxylic acid higher alcohol ester, carboxylic acid and carboxylate, phosphate, fatty alcohol vinyl ether, alkyl sulfonate, methanol, and toluene.

[0065] In some embodiments, in the first mixed solution, the amount of the first solution added is 1.5% to 2% of the liquid coal tar. Specifically, the amount of the first solution added is any one of 1.5%, 1.6%, 1.7%, 1.8%, 1.9%, and 2% of the liquid coal tar, or a range formed between any two values.

[0066] In the embodiment of the present application, liquid coal tar and a first solution are fully mixed in a first mixer 203 to form a first mixed solution, and the first solution is used to demulsify, strongly disperse, and penetrate the coal tar, while carrying out light components (such as colloids, aromatic hydrocarbons, and saturated hydrocarbons), so as to separate asphaltene and solid waste such as metals from the coal tar in a very short time, thereby improving the extraction efficiency of supercritical carbon dioxide, so as to meet the needs of continuous large-scale industrial production.

[0067] See also Figure 1 As shown, in some embodiments, the first extraction device 300 includes a first extractor 301, at least one first adjustment component and at least one separator, the first extractor 301 has a first input port located at the top, a second input port located at the bottom and a first output port arranged near the first input port; the first solution supply device 200 is connected to the first input port, the supercritical carbon dioxide supply device 600 is connected to the second input port, and the first output port is connected to the separator.

[0068] When the coal tar extraction equipment is in operation, the first mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the first extractor 301 to perform countercurrent extraction to obtain a supernatant and a precipitate. The supernatant is injected into the separator through the first output port for separation treatment to obtain the first extraction substance, wherein the first extraction substance includes colloid, aromatic hydrocarbons and saturated hydrocarbons.

[0069] In the embodiment of the present application, the first mixed solution and the supercritical carbon dioxide are introduced from both ends of the first extractor 301 to accelerate the mixing process of the first mixed solution and the supercritical carbon dioxide, thereby improving the extraction efficiency of the supercritical carbon dioxide to meet the needs of continuous large-scale industrial production.

[0070] In some embodiments, the first regulating component is installed between the first solution supply device 200 and the first extractor 301, and between the first extractor 301 and the separator, and the first regulating component is used to regulate the pressure or temperature of the first mixed solution and the first extraction substance.

[0071] In this embodiment, the first regulating component includes a first booster pump 305, which is connected between the first mixer 203 and the top of the first extractor 301, so as to pressurize the first mixed solution before the first mixed solution and supercritical carbon dioxide are respectively introduced into the two ends of the first extractor 301.

[0072] In this embodiment, the first booster pump 305 performs pressurization processing on the first mixed solution. After the pressurization processing is completed, the pressure of the first mixed solution is 25 MPa to 35 MPa.

[0073] In addition, the supercritical carbon dioxide supply device 600 includes a boosting component, wherein the boosting component includes a third boosting pump 604, so that the carbon dioxide is pressurized to form supercritical carbon dioxide before the first mixed solution and supercritical carbon dioxide are respectively introduced into the two ends of the first extractor 301.

[0074] In this embodiment, the third booster pump 604 performs pressurization processing on the carbon dioxide. After the pressurization processing is completed, the carbon dioxide is converted into the supercritical carbon dioxide. The pressure of the supercritical carbon dioxide is 25 MPa to 35 MPa.

[0075] In the embodiment of the present application, a first booster pump 305 is provided on the first extraction device 300 and a third booster pump 604 is provided on the supercritical carbon dioxide supply device 600 to adjust the pressure of the first mixed solution and the supercritical carbon dioxide, thereby increasing the solubility of the supercritical carbon dioxide in the first mixed solution, so that the asphaltene and solid waste can be separated in a short time, thereby improving the extraction efficiency of the supercritical carbon dioxide.

[0076] After the first mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the first extractor 301, the ratio of the first mixed solution to the supercritical carbon dioxide in the first extractor 301 is 1:(10~90). Specifically, in the first extractor 301, the ratio of the first mixed solution to the supercritical carbon dioxide can be set to any one of 1:10, 1:20, 1:30, 1:40, 1:50, 1:60, 1:70, 1:80, 1:90 or a range formed between any two values.

[0077] In the embodiment of the present application, since the asphaltene in the coal tar has the largest molecular weight, the largest force, and the strongest polarity, it is difficult to separate. Therefore, by setting the ratio of the first mixed solution and the supercritical carbon dioxide, the asphaltene and solid waste can be separated in a short time, thereby improving the extraction efficiency of the supercritical carbon dioxide.

[0078] In some embodiments, the first extraction device 300 further includes a second heating coil 702, which is sleeved outside the first extractor 301 and connected to a water vapor supply device 700. The water vapor supply device 700 transmits low-pressure water vapor or medium-pressure water vapor to the second heating coil 702. The second heating coil 702 heats the first extractor 301 to maintain the temperature inside the first extractor 301 above 90°C, ensuring that the coal tar remains in liquid form and avoiding condensation and blockage in the first extractor 301.

[0079] In some embodiments, the first mixed solution is introduced at the top of the first extractor 301, and the supercritical carbon dioxide is introduced from the bottom of the first extractor 301. The first mixed solution and the supercritical carbon dioxide are continuously countercurrently extracted in the first extractor 301 to obtain a first supernatant and a first precipitate, wherein the first supernatant is discharged from the upper end of the first extractor 301, and the first precipitate is discharged from the lower end of the first extractor 301.

[0080] In this embodiment, the first precipitate includes asphaltene, solid waste and other insoluble substances with the largest molecular weight, the largest force and the strongest polarity, and the first supernatant includes colloid, aromatic hydrocarbons, saturated hydrocarbons and supercritical carbon dioxide.

[0081] The embodiment of the present application adjusts the solubility of supercritical carbon dioxide by adjusting the pressure of the first mixed solution and supercritical carbon dioxide, and adjusting the temperature in the first extractor 301, so that the light components of the liquid coal tar (such as colloids, aromatic hydrocarbons, and saturated hydrocarbons) are fully dissolved in the supercritical carbon dioxide, and the asphaltene, solid waste and metal substances in the coal tar are removed; at the same time, the addition of additional solvents is avoided, the purity of the extracted material is improved, and the product quality of the extracted material is improved.

[0082] See also Figure 1 As shown, in this embodiment, the first extraction device 300 includes a first separator 302, a second separator 303 and a third separator 304; the input end of the first separator 302 is connected to the first output port of the first extractor 301, the input end of the second separator 303 is connected to the output end of the first separator 302, the input end of the third separator 304 is connected to the output end of the second separator 303, and the output end of the third separator 304 is connected to the supercritical carbon dioxide supply device 600;

[0083] In some embodiments, the first regulating component is installed between two adjacent separators. In this embodiment, the first regulating component includes a first pressure reducing valve 306 and a first heater 307 connected between the first extractor 301 and the first separator 302, a second pressure reducing valve 308 and a second heater 309 connected between the first separator 302 and the second separator 303, a third pressure reducing valve 310 connected between the second separator 303 and the third separator 304, and a fourth pressure reducing valve 311 connected between the third separator 304 and the second storage tank 601.

[0084] In this embodiment, the first supernatant is further separated to obtain a first extract, which specifically includes the following steps:

[0085] The first supernatant is passed into the first separator 302 .

[0086] The first supernatant is subjected to a first separation treatment in the first separator 302 to obtain a second supernatant and a second precipitate.

[0087] In this embodiment, the first supernatant is discharged from the first extractor 301 to the first pressure reducing valve 306, and the first pressure reducing valve 306 adjusts the pressure of the first supernatant to 20 MPa to 25 MPa. Specifically, the pressure of the first supernatant can be adjusted to any one of 20 MPa, 21 MPa, 22 MPa, 23 MPa, 24 MPa, and 25 MPa, or a range formed between any two values.

[0088] The first supernatant passes through the first pressure reducing valve 306 and enters the first heater 307. The first heater 307 adjusts the temperature of the first supernatant to 100°C to 115°C. Specifically, the temperature of the first supernatant can be adjusted to any one of 100°C, 110°C, and 115°C, or a range formed between any two values.

[0089] The second supernatant is discharged from the upper end of the first separator 302 and passed into the second separator 303 , and the second precipitate is discharged from the lower end of the first separator 302 .

[0090] In this embodiment, the second precipitate is colloid.

[0091] The second supernatant is subjected to a second separation treatment in the second separator 303 to obtain a third supernatant and a third precipitate.

[0092] The second supernatant is discharged from the first separator 302 to the second pressure reducing valve 308, and the second pressure reducing valve 308 adjusts the pressure of the second supernatant to 10 MPa to 20 MPa. Specifically, the pressure of the second supernatant can be adjusted to any one of 10 MPa, 15 MPa, and 20 MPa, or a range formed between any two values.

[0093] The second supernatant passes through the second pressure reducing valve 308 and enters the second heater 309. The second heater 309 adjusts the temperature of the second supernatant to 105°C to 120°C. Specifically, the temperature of the second supernatant can be adjusted to any one of 105°C, 110°C, 115°C, and 120°C, or a range formed between any two values.

[0094] The third supernatant is discharged from the upper end of the second separator 303 and passed into the third separator 304 , and the third precipitate is discharged from the lower end of the second separator 303 .

[0095] In this embodiment, the third precipitate is aromatic hydrocarbons.

[0096] The third supernatant is subjected to a third separation treatment in the third separator 304 to obtain a fourth supernatant and a fourth precipitate.

[0097] In this embodiment, the third supernatant is discharged from the second separator 303 to the third pressure reducing valve 310, and the third pressure reducing valve 310 adjusts the pressure of the third supernatant to 6 MPa to 10 MPa. Specifically, the pressure of the third supernatant can be adjusted to any one of 6 MPa, 7 MPa, 8 MPa, 9 MPa, and 10 MPa, or a range formed between any two values.

[0098] The fourth supernatant is discharged from the upper end of the third separator 304 , and the fourth precipitate is discharged from the lower end of the third separator 304 .

[0099] In this embodiment, the fourth supernatant is carbon dioxide, and the fourth precipitate is saturated hydrocarbon.

[0100] The fourth supernatant is discharged into the second storage tank 601 after being subjected to decompression treatment.

[0101] In this embodiment, the fourth supernatant is discharged from the third separator 304 to the fourth pressure reducing valve 311, and the fourth pressure reducing valve 311 adjusts the pressure of the fourth supernatant to 7 MPa to 8 MPa. Specifically, the pressure of the fourth supernatant can be adjusted to any one of 7 MPa, 7.5 MPa, and 8 MPa or a range formed between any two values.

[0102] In this embodiment, the fourth supernatant is cooled in the second storage tank 601 and then reformed into liquid carbon dioxide, which is then pressurized to form supercritical carbon dioxide and then re-input into the first extractor 301 for reverse extraction.

[0103] The embodiment of the present application adjusts the pressure and temperature conditions of the separation process to adjust the solubility of supercritical carbon dioxide in different light components of coal tar, so that the useful substances in the coal tar are separated one by one. The operation is simple and does not require the addition of a large amount of solvent, thereby improving the product quality of the extracted substances. At the same time, by connecting the third separator 304 with the second storage tank 601, the excess carbon dioxide is recovered and repeatedly cooled and used, thereby reducing production costs.

[0104] See also Figure 1 As shown, in some embodiments, the coal tar extraction equipment also includes a second solution supply device 400 and a second extraction device 500, the input end of the second solution supply device 400 is connected to the output end of one of the separators, the output end of the second solution supply device 400 is connected to the second extraction device 500, and the supercritical carbon dioxide supply device 600 is connected to the second extraction device 500.

[0105] In this embodiment, the second solution supply device 400 and the second extraction device 500 are used to further extract and separate the aromatic hydrocarbons. The input end of the second solution supply device 400 is connected to the output end of the second separator 303 .

[0106] When the coal tar extraction equipment is working, the second separator 303 outputs aromatic hydrocarbons to the second solution supply device 400. The aromatic hydrocarbons are fully mixed with the second solution in the second solution supply device 400 to form a second mixed solution, which is then injected into the second extraction device 500. The supercritical carbon dioxide supply device 600 injects supercritical carbon dioxide into the second extraction device 500 to perform countercurrent extraction on the second mixed solution to obtain a second extraction substance, wherein the second extraction substance includes anthracene, phenanthrene and naphthalene.

[0107] In the embodiment of the present application, a second solution is further added to demulsify and disperse the aromatic hydrocarbons through the second solution, while carrying out light components (such as anthracene, phenanthrene, and naphthalene), thereby avoiding severe emulsification caused by mixing of supercritical carbon dioxide and aromatic hydrocarbons, thereby improving the extraction effect and extraction efficiency of supercritical carbon dioxide.

[0108] See also Figure 1 As shown, in some embodiments, the second solution supply device 400 includes a second liquid storage tank 401, a second dosing pump 402 and a second mixer 403, the second liquid storage tank 401 is connected to the input end of the second dosing pump 402, and the output end of the second dosing pump 402 is connected to the second mixer 403;

[0109] The second liquid storage tank 401 is used to store a second solution, wherein the second solution includes a second drug and toluene, and the second drug and toluene are mixed under normal temperature and pressure conditions.

[0110] The second mixer 403 includes an axially arranged third inlet and a second outlet, and a radially arranged fourth inlet; the output end of the separator is connected to the third inlet, the output end of the second dosing pump 402 is connected to the fourth inlet, and the second outlet is connected to the second extraction device 500;

[0111] When the coal tar pitch extraction equipment is in operation, the first extraction material and the second solution are fully mixed in the second mixer 403 to form a second mixed solution.

[0112] In some embodiments, in the second solution, the mass percentage concentration of the second drug is 1% to 30%. Specifically, the mass percentage concentration of the second drug can be set to any value of 1%, 2%, 5%, 10%, 15%, 20%, 25%, 30% or a range formed between any two values.

[0113] In some embodiments, the material of the second drug is selected from at least one of fatty alcohol ether phosphate, carboxylic acid and carboxylate, sulfonic acid and sulfonate, methanol, and acetone.

[0114] In some embodiments, in the second mixed solution, the amount of the second solution added is 1.0% to 1.5% of the liquid coal tar. Specifically, the amount of the first solution added is any one of 1.0%, 1.1%, 1.2%, 1.3%, 1.4%, and 1.5% of the liquid coal tar, or a range formed between any two values.

[0115] In the embodiment of the present application, the aromatic hydrocarbons are fully mixed with the second solution in the second mixer 403 to form a second mixed solution, and the second solution is used to demulsify, strongly disperse and penetrate the aromatic hydrocarbons, while carrying out light components (such as anthracene, phenanthrene, and naphthalene) so as to separate the heavy aromatic hydrocarbons from the aromatic hydrocarbons in a very short time, thereby improving the extraction efficiency of supercritical carbon dioxide and meeting the needs of continuous large-scale industrial production.

[0116] See also Figure 1 As shown, in some embodiments, the second extraction device 500 includes a second extractor 501, at least one second adjustment component and at least one separator, the second extractor 501 has a third input port located at the top, a fourth input port located at the bottom and a second output port arranged near the third input port; the second solution supply device 400 is connected to the third input port, the supercritical carbon dioxide supply device 600 is connected to the fourth input port, and the second output port is connected to the separator.

[0117] When the coal tar extraction equipment is in operation, the second mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the second extractor 501 to perform countercurrent extraction to obtain a supernatant and a precipitate. The supernatant is injected into the separator through the second output port for separation treatment to obtain the second extracted material.

[0118] In the embodiment of the present application, the second mixed solution and the supercritical carbon dioxide are introduced from both ends of the second extractor 501 to accelerate the mixing process of the second mixed solution and the supercritical carbon dioxide, thereby improving the extraction efficiency of the supercritical carbon dioxide to meet the needs of continuous large-scale industrial production.

[0119] In some embodiments, the second regulating component is installed between the second solution supply device 400 and the second extractor 501, and between the second extractor 501 and the separator, and the second regulating component is used to regulate the pressure or temperature of the second mixed solution and the second extraction substance.

[0120] In this embodiment, the second regulating component includes a second booster pump 505, which is connected between the second mixer 403 and the top of the second extractor 501, so as to pressurize the second mixed solution before the second mixed solution and supercritical carbon dioxide are respectively introduced into the two ends of the second extractor 501.

[0121] In this embodiment, the second booster pump 505 performs pressurization processing on the second mixed solution. After the pressurization processing is completed, the pressure of the second mixed solution is 20 MPa to 25 MPa.

[0122] In addition, the boosting component of the supercritical carbon dioxide supply device 600 further includes a fourth boosting pump 605, so as to pressurize the carbon dioxide to form supercritical carbon dioxide before the second mixed solution and supercritical carbon dioxide are respectively introduced into the two ends of the second extractor 501.

[0123] In this embodiment, the fourth booster pump 605 performs pressurization processing on the carbon dioxide. After the pressurization processing is completed, the carbon dioxide is converted into supercritical carbon dioxide, and the pressure of the supercritical carbon dioxide is 25 MPa to 35 MPa.

[0124] In the embodiment of the present application, a third booster pump 604 is provided on the second extraction device 500 and a fourth booster pump 605 is provided on the supercritical carbon dioxide supply device 600 to adjust the pressure of the second mixed solution and the supercritical carbon dioxide, thereby increasing the solubility of the supercritical carbon dioxide in the second mixed solution, so that the heavy aromatics can be separated in a short time, thereby improving the extraction efficiency of the supercritical carbon dioxide.

[0125] In some embodiments, after the second mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the second extractor 501, the ratio of the second mixed solution to the supercritical carbon dioxide in the second extractor 501 is 1:(10~60). Specifically, in the second extractor 501, the ratio of the second mixed solution to the supercritical carbon dioxide can be set to any one of 1:10, 1:20, 1:30, 1:40, 1:50, 1:60 or a range formed between any two values.

[0126] In the embodiment of the present application, since the molecular weight, force and polarity of heavy aromatics in aromatics are relatively small compared to asphaltenes, the separation difficulty is low. Therefore, by setting the ratio of the second mixed solution to the supercritical carbon dioxide, the heavy aromatics can be separated in a short time, thereby improving the extraction efficiency of the supercritical carbon dioxide.

[0127] In some embodiments, the second extraction device 500 further includes a third heating coil 703, which is sleeved outside the second extractor 501 and connected to a water vapor supply device 700. The water vapor supply device 700 transmits low-pressure water vapor or medium-pressure water vapor to the third heating coil 703. The third heating coil 703 heats the second extractor 501 to maintain the temperature inside the second extractor 501 above 75°C, so that the aromatic hydrocarbons maintain good fluidity and avoid condensation in the second extractor 501 and blockage.

[0128] In some embodiments, the second mixed solution is melted at the top of the second extractor 501, the supercritical carbon dioxide is introduced from the bottom of the second extractor 501, and the second mixed solution and the supercritical carbon dioxide are continuously countercurrently extracted in the second extractor 501 to obtain a fifth supernatant and a fifth precipitate, wherein the fifth supernatant is discharged from the upper end of the second extractor 501, and the fifth precipitate is discharged from the lower end of the second extractor 501.

[0129] In this embodiment, the fifth precipitate includes heavy aromatic hydrocarbons, and the fifth supernatant includes anthracene, phenanthrene, naphthalene, and supercritical carbon dioxide.

[0130] The embodiment of the present application adjusts the solubility of supercritical carbon dioxide by adjusting the pressure of the second mixed solution and supercritical carbon dioxide, and adjusting the temperature in the second extractor 501, so that the light components in the aromatic hydrocarbons (such as anthracene, phenanthrene, and naphthalene) are fully dissolved in the supercritical carbon dioxide, and the heavy aromatic hydrocarbons in the aromatic hydrocarbons are eliminated; at the same time, the addition of additional solvents is avoided, the purity of the extracted material is improved, and the product quality of the extracted material is improved.

[0131] See also Figure 1 As shown, in some embodiments, the second extraction device 500 includes a fourth separator 502, a fifth separator 503 and a sixth separator 504; the input end of the fourth separator 502 is connected to the second output port of the second extractor 501, the input end of the fifth separator 503 is connected to the output end of the fourth separator 502, the input end of the sixth separator 504 is connected to the output end of the fifth separator 503, and the output end of the sixth separator 504 is connected to the supercritical carbon dioxide supply device 600.

[0132] In some embodiments, the second regulating assembly is installed between two adjacent separators. In this embodiment, the second regulating assembly includes a fifth pressure reducing valve 506 and a third heater 507 connected between the second extractor 501 and the fourth separator 502, a sixth pressure reducing valve 508 and a fourth heater 509 connected between the fourth separator 502 and the fifth separator 503, a seventh pressure reducing valve 510 connected between the fifth separator 503 and the sixth separator 504, and an eighth pressure reducing valve 511 connected between the sixth separator 504 and the second storage tank 601.

[0133] In this embodiment, the fifth supernatant is further separated to obtain a second extract, which specifically includes the following steps:

[0134] The fifth supernatant is passed into the fourth separator 502 .

[0135] The fifth supernatant is subjected to a fourth separation treatment in the fourth separator 502 to obtain a sixth supernatant and a sixth precipitate.

[0136] In this embodiment, the fifth supernatant is discharged from the second extractor 501 to the fifth pressure reducing valve 506, and the fifth pressure reducing valve 506 adjusts the pressure of the fifth supernatant to 15 MPa~20 MPa. Specifically, the pressure of the fifth supernatant can be adjusted to any one of 15 MPa, 16 MPa, 17 MPa, 18 MPa, 19 MPa, 20 MPa or a range formed between any two values.

[0137] The fifth supernatant passes through the fifth pressure reducing valve 506 and enters the third heater 507. The third heater 507 adjusts the temperature of the fifth supernatant to 85°C to 100°C. Specifically, the temperature of the fifth supernatant can be adjusted to any one of 85°C, 90°C, 95°C, and 100°C, or a range formed between any two values.

[0138] The sixth supernatant is discharged from the upper end of the fourth separator 502 and passed into the fifth separator 503 , and the sixth precipitate is discharged from the lower end of the fourth separator 502 .

[0139] In this embodiment, the sixth precipitate is anthracene.

[0140] The sixth supernatant is subjected to a fifth separation process in the fifth separator 503 to obtain a seventh supernatant and a seventh precipitate.

[0141] In this embodiment, the sixth supernatant is discharged from the fifth separator 503 to the sixth pressure reducing valve 508, and the sixth pressure reducing valve 508 adjusts the pressure of the sixth supernatant to 10MPa~15MPa. Specifically, the pressure of the sixth supernatant can be adjusted to any one of 10Mpa, 11Mpa, 12Mpa, 13Mpa, 14Mpa, 25Mpa or a range formed between any two values.

[0142] The sixth supernatant passes through the sixth pressure reducing valve 508 and enters the fourth heater 509. The fourth heater 509 adjusts the temperature of the sixth supernatant to 95°C to 110°C. Specifically, the temperature of the sixth supernatant can be adjusted to any one of 95°C, 100°C, 1055°C, and 110°C, or a range formed between any two values.

[0143] The seventh supernatant is discharged from the upper end of the fifth separator 503 and passed into the sixth separator 504 , and the seventh precipitate is discharged from the lower end of the fifth separator 503 .

[0144] In this embodiment, the seventh precipitate is phenanthrene.

[0145] The seventh supernatant is subjected to a sixth separation treatment in the sixth separator 504 to obtain an eighth supernatant and an eighth precipitate.

[0146] In this embodiment, the seventh supernatant is discharged from the fifth separator 503 to the seventh pressure reducing valve 510, and the seventh pressure reducing valve 510 adjusts the pressure of the seventh supernatant to 6 MPa to 10 MPa. Specifically, the pressure of the seventh supernatant can be adjusted to any one of 6 MPa, 7 MPa, 8 MPa, 9 MPa, and 10 MPa, or a range formed between any two values.

[0147] The eighth supernatant is discharged from the upper end of the sixth separator 504 , and the eighth precipitate is discharged from the lower end of the sixth separator 504 .

[0148] In this embodiment, the eighth supernatant is carbon dioxide, and the eighth precipitate is naphthalene.

[0149] The eighth supernatant is discharged into the second storage tank 601 after being subjected to decompression treatment.

[0150] In this embodiment, the eighth supernatant is discharged from the sixth separator 504 to the eighth pressure reducing valve 511, and the eighth pressure reducing valve 511 adjusts the pressure of the eighth supernatant to 7Mpa~8Mpa. Specifically, the pressure of the eighth supernatant can be adjusted to any one of 7Mpa, 7.5Mpa, 8Mpa or a range formed between any two values.

[0151] In this embodiment, the eighth supernatant is cooled in the second storage tank 601 to form liquid carbon dioxide, which is then pressurized to form supercritical carbon dioxide and then re-input into the second extractor 501 for reverse extraction.

[0152] The embodiment of the present application adjusts the pressure and temperature conditions of the separation process to adjust the solubility of supercritical carbon dioxide in different light components of aromatic hydrocarbons, so that useful substances of aromatic hydrocarbons are separated one by one. The operation is simple and does not require the addition of a large amount of solvent, thereby improving the product quality of the extracted substances. At the same time, by connecting the sixth separator 504 with the second storage tank 601, excess carbon dioxide is recovered and repeatedly cooled and used, thereby reducing production costs.

[0153] Please continue reading Figure 1 As shown, in some embodiments, the supercritical carbon dioxide supply device 600 further includes a second storage tank 601 and a cooling assembly.

[0154] The second storage tank 601 is used to store carbon dioxide, wherein the concentration of the carbon dioxide is 90% to 99.9% and the pressure is 7.35 MPa.

[0155] The cooling component includes a cooling coil 603 and a cooling medium supplier 602. The cooling coil 603 is installed on the outside of the second storage tank 601. The cooling medium supplier 602 is connected to the cooling coil 603. The cooling medium supplier 602 is used to provide cooling medium into the cooling coil 603. The cooling coil 603 is used to cool the second storage tank 601 so that the gaseous carbon dioxide is converted into liquid carbon dioxide.

[0156] The booster assembly is connected to the bottom of the second storage tank 601 and is used to pressurize the carbon dioxide output from the second storage tank 601 to produce supercritical carbon dioxide, so as to improve the extraction efficiency of supercritical carbon dioxide on coal tar and aromatics.

[0157] Obviously, the embodiments described above are only some of the embodiments of the present application, rather than all of the embodiments. The preferred embodiments of the present application are given in the accompanying drawings, but they do not limit the patent scope of the present application. The present application can be implemented in many different forms. On the contrary, the purpose of providing these embodiments is to make the understanding of the disclosure of the present application more thorough and comprehensive. Although the present application has been described in detail with reference to the aforementioned embodiments, for those skilled in the art, it is still possible to modify the technical solutions described in the aforementioned specific embodiments, or to make equivalent replacements for some of the technical features therein. Any equivalent structure made using the contents of the present application specification and the accompanying drawings, directly or indirectly used in other related technical fields, is also within the scope of patent protection of the present application.

Claims

1. A coal tar extraction device, characterized in that: It includes a liquid coal tar pitch output device, a first solution supply device, a first extraction device and a supercritical carbon dioxide supply device, wherein the liquid coal tar pitch output device, the first solution supply device and the first extraction device are connected in sequence, and the supercritical carbon dioxide supply device is connected to the first extraction device; The liquid coal tar output device includes a first storage tank, a heating device, and a coal tar extraction pump; the heating device is installed outside the first storage tank and is used to heat the first storage tank to maintain the fluidity of the liquid coal tar in the first storage tank; the input end of the coal tar extraction pump is connected to the first storage tank; The first solution supply device includes a first liquid storage tank, a first dosing pump and a first mixer, the first liquid storage tank is connected to the input end of the first dosing pump, and the output end of the first dosing pump is connected to the first mixer; The first extraction device comprises a first extractor, at least one first adjustment assembly and at least one separator, wherein the first extractor has a first input port located at the top, a second input port located at the bottom and a first output port disposed near the first input port; The first solution supply device is connected to the first input port, the supercritical carbon dioxide supply device is connected to the second input port, and the first output port is connected to the separator; During operation, the liquid coal tar output device outputs liquid coal tar to the first solution supply device. The liquid coal tar is fully mixed with the first solution in the first solution supply device to form a first mixed solution, which is then injected into the first extraction device. The supercritical carbon dioxide supply device injects supercritical carbon dioxide into the first extraction device to perform countercurrent extraction on the first mixed solution to obtain a first extraction substance.

2. The coal tar extraction equipment according to claim 1, characterized in that: The first mixer includes an axially arranged first inlet and a first outlet, and a radially arranged second inlet; the liquid coal tar pitch output device is connected to the first inlet, the output end of the first dosing pump is connected to the second inlet, and the first outlet is connected to the first extraction device; The liquid coal tar pitch and the first solution are fully mixed in the first mixer to form a first mixed solution.

3. The coal tar extraction equipment according to claim 1, characterized in that: The first regulating component is installed between the first solution supply device and the first extractor, and between the first extractor and the separator, and is used to regulate the pressure or temperature of the first mixed solution and the first extraction substance; During operation, the first mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the first extractor to perform countercurrent extraction to obtain a supernatant and a precipitate. The supernatant is injected into the separator through the first output port for separation treatment to obtain the first extract material.

4. The coal tar extraction equipment according to claim 3, characterized in that: The first extraction device includes a first separator, a second separator, and a third separator; the input end of the first separator is connected to the first output port of the first extractor, the input end of the second separator is connected to the output end of the first separator, the input end of the third separator is connected to the output end of the second separator, and the output end of the third separator is connected to the supercritical carbon dioxide supply device; The first adjusting component is installed between two adjacent separators.

5. The coal tar extraction equipment according to claim 4, characterized in that: The coal tar extraction equipment further includes a second solution supply device and a second extraction device, wherein the input end of the second solution supply device is connected to the output end of one of the separators, the output end of the second solution supply device is connected to the second extraction device, and the supercritical carbon dioxide supply device is connected to the second extraction device; During operation, the separator outputs the first extraction substance to the second solution supply device. The first extraction substance is fully mixed with the second solution in the second solution supply device to form a second mixed solution, which is then injected into the second extraction device. The supercritical carbon dioxide supply device injects supercritical carbon dioxide into the second extraction device to perform countercurrent extraction on the second mixed solution to obtain the second extraction substance.

6. The coal tar extraction equipment according to claim 5, characterized in that: The second solution supply device includes a second liquid storage tank, a second dosing pump and a second mixer, the second liquid storage tank is connected to the input end of the second dosing pump, and the output end of the second dosing pump is connected to the second mixer; The second mixer includes an axially arranged third inlet and a second outlet, and a radially arranged fourth inlet; the output end of the separator is connected to the third inlet, the output end of the second dosing pump is connected to the fourth inlet, and the second outlet is connected to the second extraction device; The first extraction material and the second solution are fully mixed in the second mixer to form a second mixed solution.

7. The coal tar extraction equipment according to claim 6, characterized in that: The second extraction device includes a second extractor, at least one second adjustment component, and at least one separator. The second extractor has a third input port located at the top, a fourth input port located at the bottom, and a second output port located near the third input port. The second solution supply device is connected to the third input port, the supercritical carbon dioxide supply device is connected to the fourth input port, and the second output port is connected to the separator. The second regulating component is installed between the second solution supply device and the second extractor, and between the second extractor and the separator, and is used to regulate the pressure or temperature of the second mixed solution and the second extraction substance; During operation, the second mixed solution and the supercritical carbon dioxide are respectively introduced into both ends of the second extractor to perform countercurrent extraction to obtain a supernatant and a precipitate. The supernatant is injected into the separator through the second output port for separation treatment to obtain the second extract material.

8. The coal tar extraction equipment according to claim 7, characterized in that: The second extraction device includes a fourth separator, a fifth separator, and a sixth separator; the input end of the fourth separator is connected to the second output port of the second extractor, the input end of the fifth separator is connected to the output end of the fourth separator, the input end of the sixth separator is connected to the output end of the fifth separator, and the output end of the sixth separator is connected to the supercritical carbon dioxide supply device; The second adjusting assembly is installed between two adjacent separators.

9. The coal tar pitch extraction equipment according to any one of claims 1 to 8, characterized in that: The supercritical carbon dioxide supply device includes a second storage tank, a cooling component and a pressurizing component; The second storage tank is used to store carbon dioxide; The cooling assembly includes a cooling coil and a cooling medium supplier, wherein the cooling coil is installed outside the second storage tank, and the cooling medium supplier is connected to the cooling coil; The pressurizing component is connected to the bottom of the second storage tank and is used for pressurizing the carbon dioxide output from the second storage tank.

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