Integrated equipment for coal hot solution liquefaction extraction process

Abstract

The present application belongs to the technical field of coal clean grading conversion, and discloses an integrated equipment for coal hot solution liquefaction extraction process, aiming at solving the problems of low solid-liquid separation efficiency, incomplete flash separation, easy leakage of dynamic seal, easy blockage of discharge and the like of the existing device. The equipment is mainly composed of a reaction flash unit and a condensation collection unit which are sequentially connected. The reaction flash unit adopts a longitudinally integrated hydrogenation liquefaction reactor and a vacuum flash tank, cancels a mechanical agitator, relies on an external circulation and an internal split structure to realize material mixing and heating, and eliminates the leakage risk of high-pressure dynamic seal; a built-in multiple filtering structure and a "self-rotating leaf + hydrogenation blowing description component" combined anti-blocking device cooperate with an external multiple heating mode to ensure the solid-liquid separation effect and continuous and stable operation. The condensation collection unit adopts a two-stage deep condensation and a horizontal gravity oil-water separation structure to improve the purity and efficiency of solvent oil recovery. The equipment can realize continuous production through staggered peak alternating operation of multiple units, and is suitable for efficient hot solution liquefaction extraction of low-rank coal.

Description

Technical Field

[0001] This invention belongs to the field of clean coal classification and conversion technology, and more specifically, it relates to an integrated equipment for a coal thermal solution extraction process. Background Technology

[0002] Low-rank coal (such as lignite and long-flame coal) accounts for more than 50% of my country's total coal reserves. It is characterized by high moisture content, high ash content, low calorific value, and easy spontaneous combustion, resulting in low efficiency and significant environmental pollution from direct combustion. Coal thermal extraction technology, as one of the core pathways for the graded and differentiated conversion of low-rank coal, selectively dissolves organic matter in coal using organic solvents at 300–360℃ under high-pressure hydrogen atmosphere, achieving dehydration, deoxygenation, and deashing to obtain ultra-pure coal with high calorific value and high-value-added raffinate products. This technology has significant economic and environmental value.

[0003] Coal-to-oil technology is mainly divided into two major technical routes: direct liquefaction (DCTL) and indirect liquefaction (ICTL). The two differ significantly in principle, process, and equipment structure. Direct liquefaction units operate under more demanding conditions, but the process is shorter and easier to centralize. Its core units generally include: coal slurry preparation unit, pressurization and heating unit, direct hydrogenation reaction liquefaction unit, solid-liquid separation unit, hydrogenation upgrading unit, and solvent oil recovery unit.

[0004] Existing coal thermal extraction devices have the following technical defects in practical applications: (1) Low solid-liquid separation efficiency: After the reaction is completed, the coal powder in the extract is seriously entrained, which seriously affects the purity of the extract product; (2) Incomplete flash separation: low solvent oil recovery rate, resulting in high operating costs; (3) Poor oil-water separation effect: The purity of the recovered solvent oil is insufficient, and the recycling efficiency is low; (4) Dynamic seal leakage problem: Reactors and flash tanks with agitator structure can only be arranged separately due to structural limitations. Under high pressure conditions, dynamic seal leakage is very likely to occur. (5) Discharge blockage problem: The semi-coke at the bottom of the reactor is prone to deposit and block the discharge port. Conventional filters will become blocked within minutes when processing fine semi-coke, which seriously affects continuous production.

[0005] Therefore, there is an urgent need to develop a new type of coal thermal solidification extraction equipment that can effectively solve the above problems. Summary of the Invention

[0006] The technical problem this invention aims to solve is to overcome the shortcomings of existing technologies and provide an integrated equipment for coal thermal solution extraction, achieving efficient thermal solution extraction of low-rank or high-rank coal. This addresses problems in existing technologies such as low solid-liquid separation efficiency, incomplete flash evaporation, poor oil-water separation, dynamic seal leakage, and discharge blockage. Through a stirless external circulation and internal diversion design, the hydrogenation liquefaction reactor and vacuum flash tank are integrated and centrally arranged. Combined with multiple filtration systems, anti-clogging devices, and precise temperature control, continuous, high-yield, and high-purity extraction production is guaranteed.

[0007] To achieve the above objectives, this invention provides an integrated equipment for a coal thermal liquefaction extraction process, comprising a reaction flash evaporation unit and a condensation collection unit, the two units being connected sequentially by pipelines. The reaction flash evaporation unit consists of a longitudinally integrated hydrogen liquefaction reaction device and a flash evaporation device. The hydrogen liquefaction reaction device is located at the top, and the flash evaporation device is positioned below it, with a connecting pipe fixed between them. An external pipeline filter and a proportional unloading valve are installed in the middle of the connecting pipe. The hydrogen liquefaction reaction device includes a circulating heating device and a hydrogenation liquefaction reactor, with a pipeline connecting the circulating heating device and the hydrogenation liquefaction reactor, forming an external circulating heating loop. The hydrogenation liquefaction reactor is a material pressure reactor, with an internal filtration device. This filtration device, in conjunction with the external pipeline filter, forms a multi-stage filtration structure, achieving two-stage thorough separation of the extract and solid semi-coke, effectively preventing coal powder from being carried into downstream equipment. An anti-clogging device is installed at the bottom inner side of the hydrogenation liquefaction reactor, consisting of a self-rotating blade and a hydrogenation blowing assembly. The hydrogenation liquefaction reactor is surrounded by an auxiliary heating assembly, which works in conjunction with the heating elements of the circulating heating device to form multiple heating modes.

[0008] Furthermore, the anti-clogging device has the following specific structure: a central rotating shaft is fixed to the bottom of the self-rotating blade, which is rotatably connected to the bottom of the hydrogenation liquefaction reactor. This allows the self-rotating blade to rotate freely around the central rotating shaft under the force generated by the fluid flow inside the reactor. The self-rotating blade does not rely on external power for driving, but rotates only by the fluid force. The hydrogenation blowing assembly is fixed below the filter device. Multiple nozzles are provided on the outer wall of the hydrogenation blowing assembly facing the filter device, and each nozzle has an openable cap. When the hydrogenation blowing assembly is not in operation, the cap is closed to prevent impurities from entering the nozzle; when the hydrogenation blowing assembly is in operation, the cap is opened, and the nozzle sprays hydrogenation gas upwards towards the filter device.

[0009] Furthermore, the circulating heating device includes a first external circulation high-pressure pump, an electromagnetic heating coil or a shell-and-tube heat exchanger, and a first circulation pipe. The first circulation pipe is disposed on the outer wall of the hydrogenation liquefaction reactor, with its two ends fixedly connected to the upper and lower parts of the side wall of the hydrogenation liquefaction reactor, respectively. The electromagnetic heating coil or shell-and-tube heat exchanger is disposed on the upper part of the first circulation pipe to heat the circulating material outside the reactor. The first external circulation high-pressure pump is disposed on the lower part of the first circulation pipe to provide driving force for the external circulation. The lower end of the first circulation pipe is obliquely connected to the inner wall of the hydrogenation liquefaction reactor to reduce the frontal impact of the backflow material on the flow field inside the reactor and enhance bottom disturbance.

[0010] The auxiliary heating components are arranged around the outside of the hydrogenation liquefaction reactor and cooperate with the electromagnetic heating coil or shell-and-tube heat exchanger in the first circulation pipe to form multiple heating modes, further improving the heating efficiency and temperature uniformity of the materials in the reactor.

[0011] Furthermore, the filtration device within the hydrogenation liquefaction reactor is fixed obliquely to the inner wall of the reactor. During the hydrogenation liquefaction reaction, the hydrogenation blowing assembly located below the filtration device sprays hydrogenation gas upwards towards the filtration device through a nozzle, achieving reverse flushing of the obliquely fixed filtration device and removing fine powder and semi-coke adhering to the filter surface.

[0012] Furthermore, the flash evaporation device includes a vacuum flash tank, a second external circulation high-pressure pump, a second circulation pipe, and a heating device. The vacuum flash tank is located directly below the hydrogen liquefaction reactor and is connected to the upper hydrogenation liquefaction reactor via the connecting pipe. The second circulation pipe is fixed to the outside of the vacuum flash tank and communicates with the inner wall of the vacuum flash tank. The second external circulation high-pressure pump is located in the middle of the second circulation pipe. The heating device is fixed to the outer wall of the second circulation pipe and can extend to the outlet pipe of the vacuum flash tank to prevent high-viscosity heavy oil from condensing and clogging the pipeline.

[0013] Furthermore, the condensation collection unit includes a water-cooled vacuum condenser, a volumetric separator, a vacuum condenser, and a gas-liquid separator. One end of the water-cooled vacuum condenser is connected to the top gas phase outlet of the vacuum flash tank of the flash evaporator via a pipeline, and the other end is connected to the volumetric separator via a pipeline. The volumetric separator is connected to the vacuum condenser and the gas-liquid separator via pipelines. The above four devices are connected sequentially via pipelines to form a complete condensation recovery process path.

[0014] Furthermore, the integrated equipment is also equipped with a utility system, serving as a known auxiliary condition for the normal operation of the entire system. The utility system mainly includes a vacuum pumping device and a cooling device. The vacuum pumping device provides the necessary negative pressure (vacuum) environment for equipment such as the vacuum flash tank, water-cooled vacuum condenser, volumetric separator, vacuum condenser, and gas-liquid separator; the cooling device provides circulating cooling water for the water-cooled vacuum condenser and low-temperature chilled water for the vacuum condenser, ensuring the normal condensation and cooling functions of each device. The aforementioned utility systems are all facilities known in the art, and their specific configurations can be selected according to actual engineering conditions, and are not considered as the focus of this invention.

[0015] Furthermore, the hydrogenation liquefaction reactor is equipped with a hydrogen feed port, a solvent oil and pulverized coal mixed feed port, and a nitrogen port. Hydrogen serves both as the reactant gas for the hydrogenation liquefaction reaction and as the purge gas source for the hydrogenation purging assembly, achieving dual use of hydrogen. The solvent oil and pulverized coal are pre-mixed and then pumped into the reactor through the mixed feed port via a high-pressure pump. The nitrogen port is used for system inert atmosphere protection and gas purging during start-up and shutdown.

[0016] Furthermore, the hydrogenation liquefaction reactor adopts a stirrer-free structure, replacing traditional mechanical stirring with a material mixing and dispersion system composed of an external circulation structure and an internal diversion structure. The external circulation structure is driven by a first external circulation high-pressure pump to circulate the material inside the reactor, achieving mixing and heating. The internal diversion structure is located inside the hydrogenation liquefaction reactor, and through the rational arrangement of flow guiding components, the material flowing back into the reactor forms multiple diversions within the reactor, enhancing the material dispersion and uniform mixing effect. The bottom of the hydrogenation liquefaction reactor is equipped with self-propelled rotating blades and a hydrogenation blowing assembly to prevent the deposition of solid semi-coke.

[0017] Furthermore, a proportional unloading valve is installed on the connecting pipeline between the hydrogenation liquefaction reactor and the vacuum flash tank to monitor the temperature and pressure within the pipeline in real time. When the pressure exceeds a set value, the valve automatically opens proportionally to release pressure, ensuring safe system operation. A heat tracing structure is installed on the outlet pipeline of the vacuum flash tank to prevent heavy oil from condensing and clogging the pipeline during discharge.

[0018] Furthermore, the vacuum flash evaporator is equipped with pressure and temperature sensors. These sensors monitor the operating pressure and temperature within the vacuum flash evaporator in real time, providing data support for process control.

[0019] Furthermore, the volumetric separator has a horizontal structure with a liquid collection bag at the bottom. Under gravity, the denser aqueous phase naturally settles and collects at the bottom of the collection bag, and is discharged through the bottom drain outlet; the less dense solvent oil phase floats to the top and is discharged and recycled through the upper outlet. Both the volumetric separator and the gas-liquid separator are equipped with pressure and temperature sensors and have low-point venting lines for safe discharge by breaking the vacuum when discharge or maintenance is required.

[0020] Furthermore, to achieve continuous industrial production, at least two sets of the reaction flash evaporation unit are provided. Even further, at least two sets of the integrated equipment are provided as a whole, with multiple sets of integrated equipment coordinated through a unified raw material supply system and solvent oil circulation system, operating alternately in staggered sequences, so that the entire production system achieves uninterrupted continuous operation on a macroscopic level.

[0021] Compared with the prior art, the beneficial effects of the present invention are: 1. Both the reactor and the vacuum flash tank adopt a stirrer-free design. The mechanical stirring is replaced by an external circulation and internal diversion structure, which allows the two vessels to be arranged vertically and centrally. The pipelines are centralized and do not accumulate material, which fundamentally eliminates the high-pressure leakage problem caused by the dynamic seal of the stirrer, and also eliminates the risk of pipe blockage.

[0022] 2. The internal filtration device of the hydrogenation liquefaction reactor and the external pipeline filter form a multi-filtration structure. Combined with the backwashing function of the hydrogenation blowing component, it effectively prevents semi-coke blockage and significantly improves the solid-liquid separation efficiency and the purity of the extracted product.

[0023] 3. The bottom of the hydrogenation liquefaction reactor is equipped with an anti-clogging device consisting of a self-rotating blade and a hydrogenation blowing assembly. The self-rotating blade relies solely on the flow force generated by the fluid flow inside the reactor to continuously rotate and disturb the material at the bottom. The hydrogenation blowing assembly is located below the filter device, and its outer wall facing the filter device has multiple nozzles. When not in operation, the caps at the nozzle openings are closed to prevent debris from entering. When in operation, the caps are opened, and hydrogen is injected through the nozzles toward the filter device to purge the bottom and the filter device. This dual mechanism ensures that the outlet is not blocked by semi-coke, guaranteeing continuous and stable operation.

[0024] 4. The external circulation heating device places the heating unit outside the reactor (outside the vessel). An electromagnetic heating coil or a shell-and-tube heat exchanger is installed on the first circulation pipe. At the same time, auxiliary heating components are installed around the outside of the hydrogenation liquefaction reactor. The two work together to form multiple heating modes, realize precise pre-temperature control of materials, simplify the internal structure of the reactor, and promote material mixing and heat and mass transfer through external circulation, thereby improving reaction efficiency.

[0025] 5. The system employs a two-stage deep condensation process, combining a water-cooled vacuum condenser and a vacuum condenser with a gravity oil-water separation design using a horizontal solvent separator. This achieves efficient condensation of light component oil and gas and high-purity recovery of solvent oil, thereby reducing operating costs.

[0026] 6. By setting up two or more flash evaporation units and operating them alternately, continuous production of the entire extraction process can be achieved, meeting the needs of industrial-scale production.

[0027] 7. The connecting pipeline is equipped with a proportional unloading valve to realize automatic overpressure relief, the outlet pipeline of the vacuum flash tank is equipped with heat tracing to prevent heavy oil condensation and blockage, and each separator is equipped with a low-point venting pipeline to realize safe vacuum breaking and material discharge. Multiple safety measures ensure the safe operation of the system. Attached Figure Description

[0028] Figure 1 This is a schematic diagram showing the distribution of the various units in this invention; Figure 2 This is a flow chart of the coal liquefaction extraction process of the present invention; Figure 3 This is a schematic cross-sectional view of the hydrogenation liquefaction reactor of the present invention.

[0029] In the diagram, 1. Flash reaction unit; 2. Condensation and collection unit; 21. Water-cooled vacuum condenser; 22. Solvent separator; 23. Vacuum condenser; 24. Gas-liquid separator; 3. Coal slurry treatment unit; 31. Coal mill; 32. Mill discharge trough; 33. Low-pressure coal slurry pump; 34. Coal slurry tank; 35. High-pressure coal slurry pump; 36. Shell-and-tube heater; 4. Hydrogen liquefaction reaction device; 41. Connecting pipe; 411. External pipeline filter; 412. Proportional unloading valve; 42. Circulation feeder. Heating device; 421, First external circulation high-pressure pump; 422, Electromagnetic heating coil; 423, First circulation pipe; 43, Hydrogenation liquefaction reactor; 431, Filtration device; 44, Anti-clogging device; 45, Self-propelled rotating blade; 451, Central rotating shaft; 46, Hydrogenation blowing assembly; 461, Nozzle; 462, Cover; 47, Auxiliary heating assembly; 5, Flash evaporation device; 51, Vacuum flash evaporator; 52, Second external circulation high-pressure pump; 53, Second circulation pipe; 54, Heat tracing device. Detailed Implementation

[0030] The present invention will be further described below with reference to the accompanying drawings: The directional terms used in the detailed description paragraphs are only for the convenience of those skilled in the art to understand the technical solutions described in this application based on the visual orientation shown in the accompanying drawings. Unless otherwise explicitly specified and limited, the terms "setting," "installation," "connection," etc., should be interpreted broadly, and those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0031] like Figure 1 As shown in the figure, the integrated equipment for a coal thermal solution extraction process provided in this embodiment mainly includes two functional units: a reaction flash evaporation unit 1 and a condensation collection unit 2. The two units are connected sequentially by pipelines to form a complete coal thermal solution extraction process system. The normal operation of the integrated equipment also requires corresponding utility systems, including a vacuum device to provide a negative pressure environment for the system and a cooling device to provide a cooling medium. These utility systems are well-known facilities in the art and can be configured according to actual engineering needs.

[0032] The reaction flash evaporation unit 1 is the core component of the integrated equipment of this invention. It consists of a longitudinally integrated hydrogen liquefaction reaction device 4 and a flash evaporation device 5, which are arranged vertically. The hydrogen liquefaction reaction device 4 is located at the top, and the flash evaporation device 5 is located directly below it. They are fixedly connected in the middle by a connecting pipe 41, forming a compact structure with centralized pipes and no material accumulation.

[0033] The hydrogen liquefaction reactor 4 mainly includes a hydrogen liquefaction reactor 43 and a circulating heating device 42, which are connected by a pipeline to form an external circulating heating loop.

[0034] The hydrogenation liquefaction reactor 43 is a material-pressurized reactor and is the core reaction equipment of this invention. This hydrogenation liquefaction reactor 43 adopts an innovative design without a mechanical stirrer. It replaces the traditional stirring function by setting an external circulation structure outside the reactor 43 and an internal diversion structure inside, achieving efficient dispersion and uniform mixing of the materials within the reactor. By eliminating the stirrer and its through-wall rotating shaft, the potential for high-pressure dynamic seal leakage is fundamentally eliminated, and the hydrogenation liquefaction reactor 43 can be vertically and centrally arranged with the vacuum flash tank 51 below.

[0035] The hydrogenation liquefaction reactor 43 has three feed ports: a hydrogen feed port, a solvent oil and pulverized coal mixed feed port, and a nitrogen feed port, located at the top or upper side. The hydrogen feed port is used to introduce high-pressure hydrogen, which serves a dual function in this unit—it acts as a necessary feed gas for the hydrogenation liquefaction reaction and also serves as a gas source for the hydrogenation purging assembly 46 to purge the bottom of the hydrogenation liquefaction reactor 43 and the filter device 431. The solvent oil and pulverized coal mixed feed port receives coal slurry pre-mixed in the coal slurry tank 34, which is pressurized and fed in by the high-pressure coal slurry pump 35. A heating device (such as a shell-and-tube heat exchanger or an electromagnetic heating coil 422) can be installed on the feed pipe to preheat the incoming coal slurry. The nitrogen feed port is used to establish an inert atmosphere during system start-up and shutdown, as well as for gas replacement and purging before maintenance.

[0036] The circulating heating device 42 includes a first external circulating high-pressure pump 421, an electromagnetic heating coil 422 (or a shell-and-tube heat exchanger), and a first circulating pipe 423. The first circulating pipe 423 is located on the outer wall (outside the vessel) of the hydrogenation liquefaction reactor 43. Its upper end is connected to the upper part of the side wall of the hydrogenation liquefaction reactor 43, serving as the outlet end of the circulating material; its lower end is connected to the lower part of the side wall of the hydrogenation liquefaction reactor 43, serving as the return end of the heated material. The lower end of the first circulating pipe 423 enters the inner wall of the hydrogenation liquefaction reactor 43 at an oblique angle, that is, it is obliquely connected to the inner wall of the hydrogenation liquefaction reactor 43. This oblique entry method helps to reduce the frontal impact interference of the return material on the flow field inside the vessel, and at the same time, the obliquely entering material flow enhances the disturbance in the bottom region inside the vessel.

[0037] An electromagnetic heating coil 422 is wound and fixed to the upper part of the first circulation pipe 423 (or in the form of a shell-and-tube heat exchanger) to heat the circulating material drawn from the upper part of the hydrogenation liquefaction reactor 43. Placing the heating unit on the pipeline outside the reactor simplifies the internal structure of the hydrogenation liquefaction reactor 43, eliminating the need for heating elements inside the reactor; it also avoids localized overheating inside the reactor, achieving uniform and precise pre-temperature control of the material outside the reactor. A first external circulation high-pressure pump 421 is located at the lower part of the first circulation pipe 423, providing driving force for the entire external circulation loop.

[0038] An auxiliary heating component 47 is also provided on the outside of the hydrogenation liquefaction reactor 43. The auxiliary heating component 47 is arranged around the outer wall of the hydrogenation liquefaction reactor 43 and cooperates with the electromagnetic heating coil 422 or the shell-and-tube heat exchanger provided on the first circulation pipe 423 to form a multi-heating mode. The multi-heating mode can further improve the heating efficiency and temperature uniformity of the material in the hydrogenation liquefaction reactor 43, adapt to the different heating power requirements of different working conditions and material characteristics, and effectively ensure that the hydrogenation liquefaction reaction proceeds stably within the target temperature range (300~360℃).

[0039] The external circulation process is as follows: a thin tube on the upper side wall of the hydrogenation liquefaction reactor 43 draws the material out of the reactor, and the material collects and enters the first circulation pipe 423 (loop pipe). The electromagnetic heating coil 422 (or shell-and-tube heat exchanger) on the upper part of the loop pipe heats the material passing through. The heated material enters the first external circulation high-pressure pump 421 for pressurization. An auxiliary heating device can also be installed on the outlet pipe of the high-pressure pump as needed. The material finally returns to the hydrogenation liquefaction reactor 43 through the inclined connecting port at the lower end of the first circulation pipe 423. At the same time, the auxiliary heating component 47 arranged around the outer wall of the reactor heats the outer wall of the reactor. The two work together to maintain and precisely control the reaction temperature inside the reactor.

[0040] The hydrogenation liquefaction reactor 43 is equipped with a filter device 431, which is fixedly installed at an angle on the inner wall of the reactor 43. The angled installation of the filter device 431 causes the semi-coke and coal powder trapped on the filter surface to naturally slide downwards under the influence of gravity, preventing them from accumulating and caking on the filter surface. The filter device 431 is used to intercept and filter coal powder and semi-coke during the reaction process. The intercepted solid materials remain in the hydrogenation liquefaction reactor 43 to continue participating in the reaction or are awaited for subsequent slag discharge.

[0041] An external pipeline filter 411 is installed in the middle of the connecting pipe 41 between the hydrogenation liquefaction reactor 43 and the vacuum flash tank 51. The external pipeline filter 411 works in conjunction with the inclined filter device 431 inside the hydrogenation liquefaction reactor 43 to form a multi-stage filtration structure. After the reaction is completed, the liquefied coal solution is transported to the vacuum flash tank 51 through the connecting pipe 41 under pressure difference. It first undergoes primary filtration through the filter device 431 inside the hydrogenation liquefaction reactor 43, and then undergoes secondary filtration through the external pipeline filter 411 on the connecting pipe 41. This achieves two-stage thorough separation of the extract and solid semi-coke, effectively preventing coal powder from being carried into the downstream flash and condensation equipment.

[0042] A proportional unloading valve 412 is also installed on the connecting pipe 41. The proportional unloading valve 412 monitors the temperature and pressure in the pipeline in real time. When the pipeline pressure exceeds the set safety value, the proportional unloading valve 412 automatically opens proportionally to safely release the overpressure gas or material, prevent the pipeline and equipment from being damaged due to overpressure, and ensure the safe operation of the system.

[0043] An anti-clogging device 44 is installed at the bottom inner side of the hydrogenation liquefaction reactor 43. This anti-clogging device 44 is composed of a self-rotating blade 45 and a hydrogenation blowing assembly 46. The self-rotating blade 45 is a freely rotatable blade component with a central rotating shaft 451 fixed at its bottom. The central rotating shaft 451 cooperates with a bearing seat at the bottom of the hydrogenation liquefaction reactor 43 to form a rotational connection, allowing the self-rotating blade 45 to rotate freely around the central rotating shaft 451 under the push of the fluid inside the reactor. The self-rotating blade 45 does not rely on any external power, but is driven to rotate only by the flow force generated by the fluid flow inside the reactor. During the operation of the hydrogenation liquefaction reactor 43, the first external circulation high-pressure pump 421 drives the material inside the reactor to continuously circulate along the first circulation pipe 423. The fluid impacts the blade surface of the self-rotating blade 45, generating a driving torque that pushes the self-rotating blade 45 to rotate continuously, constantly agitating the bottom area of ​​the hydrogenation liquefaction reactor 43, preventing semi-coke particles from settling and forming caking at the bottom, as the first anti-clogging measure.

[0044] The hydrogenation blowing assembly 46 is fixedly installed below the filter device 431, located below the self-rotating blade 45. Multiple nozzles 461 are provided on the outer wall of the hydrogenation blowing assembly 46 facing the filter device 431. These nozzles 461 are arranged equidistantly in the circumferential direction to ensure uniform spray coverage without dead angles. Each nozzle 461 is oriented towards the area where the filter device 431 is located. An openable cap 462 is provided at the opening edge of each nozzle 461. When the hydrogenation blowing assembly 46 is not in operation, the cap 462 is kept closed by a hinge spring at the hinged position with the nozzle opening edge, preventing debris (such as semi-coke particles, coal dust, etc.) from entering the nozzle 461 and causing blockage. When the hydrogenation blowing assembly 46 is in operation, the cap 462 opens, and the nozzles 461 spray hydrogenated gas upwards towards the filter device 431, producing the following dual anti-blocking and auxiliary effects: First, the bottom of the hydrogen liquefaction reactor 43 is purged to prevent deposition and blockage. The hydrogen jet directly purges the bottom area of ​​the hydrogen liquefaction reactor 43, blowing up the semi-coke particles deposited at the bottom and resuspending them in the liquid phase, preventing the semi-coke from accumulating and blocking near the outlet, and ensuring that the outlet is unobstructed.

[0045] Second, a backwash is performed on the filter device 431. The hydrogen jet sprayed upwards from the nozzle 461 towards the filter device 431 washes against the filter surface (bottom or lower surface) of the obliquely fixed filter device 431, creating a bottom-up backwash effect. This blows off the fine powder and semi-coke adhering to the filter surface and redisperses them in the reactants. This backwash mechanism utilizes the hydrogen present in the hydrogenation reaction itself, requiring no additional rinsing equipment or independent operating procedures. It has the advantages of simple structure, reliable operation, and no need for shutdown maintenance.

[0046] The flash evaporation unit 5 mainly includes a vacuum flash tank 51, a second external circulation high-pressure pump 52, a second circulation pipe 53, and a heating device 54. The vacuum flash tank 51 is located directly below the hydrolysis reactor 43, and the two are connected by the connecting pipe 41. After the reaction in the hydrolysis reactor 43 is completed, the liquefied coal solution is transported from top to bottom to the vacuum flash tank 51 through the connecting pipe 41 under the action of pressure difference. Under vacuum, the liquefied coal solution undergoes flash separation in the vacuum flash tank 51. The light components are discharged as gas from the gas phase outlet at the top of the tank and enter the downstream condensation and collection unit 2 for condensation and recovery; the heavy components, the heavy oil product, are discharged from the bottom of the vacuum flash tank 51 and collected.

[0047] The second circulation pipe 53 is fixed to the outside (outside the vessel) of the vacuum flash tank 51, with its upper and lower ends connected to the inner wall of the vacuum flash tank 51, respectively. The second external circulation high-pressure pump 52 is installed in the middle of the second circulation pipe 53, driving the material inside the tank to circulate along the second circulation pipe 53, promoting uniform heating of the material and thorough separation of light and heavy components during flash evaporation, thereby improving flash evaporation efficiency. The heating device 54 is fixed to the outer wall of the second circulation pipe 53 and can extend to each outlet pipeline of the vacuum flash tank 51. The heating device 54 can adopt commonly used heating methods in the field, such as heating cables, steam heating pipes, or electric heating belts. The function of the heating device 54 is to insulate or heat the material in the pipeline, preventing high-viscosity heavy oil components from condensing and precipitating in the circulation and outlet pipelines due to temperature reduction, thus preventing blockage and ensuring unobstructed flow in the external circulation system and discharge pipeline of the flash evaporator 5.

[0048] The vacuum flash evaporator 51 is equipped with a pressure sensor PI and a temperature sensor TI, which are used to monitor the working pressure (vacuum degree) and working temperature inside the tank in real time. Operators or automatic control systems can accurately adjust the operating parameters based on the sensor feedback data to ensure thorough flash separation and stable product quality.

[0049] To achieve continuous industrial production, at least two sets of reaction flash evaporation units 1 are provided in this embodiment. Each set of reaction flash evaporation units 1 operates independently, alternating between the "feed → reaction → discharge → flash evaporation" operation cycles in a staggered sequence. For example, when the first set of reaction flash evaporation units 1 is in the hydrogenation liquefaction reaction stage, the second set of reaction flash evaporation units 1 is discharging and preparing for the next batch of feed; the operating cycles of the two sets of units are staggered, enabling the overall coal thermal solidification extraction process to achieve continuous and uninterrupted operation on a macroscopic level.

[0050] The condensation collection unit 2 mainly includes a water-cooled vacuum condenser 21, a solvent separator 22, a vacuum condenser 23, and a gas-liquid separator 24. The four devices are connected in sequence through pipelines to form a four-stage series condensation recovery process.

[0051] The water-cooled vacuum condenser 21 serves as the first-stage condensation device in the condensation collection unit 2, using circulating water as the cooling medium. The inlet of the water-cooled vacuum condenser 21 is connected to the top gas phase outlet of the vacuum flash tank 51 via a pipe, receiving high-temperature light component gas from the flash evaporation unit 5. In the water-cooled vacuum condenser 21, the high-temperature gas is cooled by the circulating water, with most of the solvent oil components condensing into a liquid phase. The condensed liquid solvent oil (which may contain a small amount of water) flows downstream to the solvent separator 22 for oil-water separation.

[0052] The solvent separator 22 adopts a horizontal structure with a liquid collection bag at the bottom. The solvent separator 22 receives condensate from the water-cooled vacuum condenser 21. Inside the solvent separator 22, the density difference between solvent oil and water allows for natural stratification under gravity: the denser water phase naturally settles and collects in the liquid collection bag at the bottom, and is discharged periodically or continuously through a drain outlet at the bottom of the collection bag; the less dense solvent oil phase floats on top and is discharged through the solvent oil outlet at the top of the solvent separator 22, and can be recycled for the next coal thermal extraction process. Non-condensable gases in the solvent separator 22 are led out from its gas phase outlet and split into two paths: one path enters the vacuum condenser 23 for deep condensation, and the other path enters the gas-liquid separator 24.

[0053] Vacuum condenser 23 serves as the second-stage condensation device in condensation collection unit 2, using low-temperature chilled water as the cooling medium. Since the temperature of the chilled water is significantly lower than that of the circulating water, vacuum condenser 23 can deeply condense the non-condensable gases from solvent separator 22, further condensing the remaining light oil components. The liquid phase condensed in vacuum condenser 23 also flows into gas-liquid separator 24.

[0054] The gas-liquid separator 24 performs the final gas-liquid separation on the gas-liquid two-phase mixture from the solvent separator 22 and the vacuum condenser 23, recovers the liquid solvent, and extracts the non-condensable tail gas through the pipeline by the vacuum pumping device.

[0055] Both solvent separator 22 and gas-liquid separator 24 are equipped with pressure sensor PI and temperature sensor TI to monitor the operating pressure and temperature inside each separator in real time, providing data support for process control and fault diagnosis. Simultaneously, solvent separator 22 and gas-liquid separator 24 are each equipped with a low-point vent line. The low-point vent line is located at the lowest point of each separator. When liquid discharge or equipment maintenance is required, the low-point vent valve is opened to "break the vacuum" (i.e., disrupt the negative pressure environment inside the separator and restore normal pressure), allowing the liquid in the container to be smoothly discharged from the low-point vent by gravity, achieving safe discharge operation.

[0056] The coal slurry treatment unit 3 includes a coal mill 31, a mill discharge trough 32, a low-pressure coal slurry pump 33, a coal slurry tank 34, a high-pressure coal slurry pump 35, and a shell-and-tube heater 36. The coal mill 31, mill discharge trough 32, low-pressure coal slurry pump 33, coal slurry tank 34, and high-pressure coal slurry pump 35 are connected sequentially by pipelines, and the high-pressure coal slurry pump 35 is connected to the hydrogenation liquefaction reactor 43. The shell-and-tube heater 36 is installed outside the pipeline between the high-pressure coal slurry pump 35 and the hydrogenation liquefaction reactor 43.

[0057] Combined with appendix Figure 1 The overall process of the integrated equipment in this embodiment will be fully described below.

[0058] (1) Raw material preparation. The raw coal is pulverized to the required particle size by the coal mill 31 and then enters the mill discharge trough 32. The pulverized coal is transported to the coal slurry tank 34 by the low-pressure coal slurry pump 33. In the coal slurry tank 34, the pulverized coal and solvent oil are mixed in a predetermined ratio and stirred to form a uniform coal slurry.

[0059] (2) Hydrogenation liquefaction reaction. The coal slurry is pressurized to the required reaction pressure by the high-pressure coal slurry pump 35 and then fed into the hydrogenation liquefaction reactor 43 through the solvent oil and pulverized coal mixing inlet. At the same time, high-pressure hydrogen gas is introduced into the hydrogenation liquefaction reactor 43 through the hydrogen gas feed inlet. Under the temperature range of 300-360℃ and the high-pressure hydrogen atmosphere, the solvent oil selectively dissolves and extracts the organic matter in the coal, resulting in a hydrogenation liquefaction reaction.

[0060] During the reaction, the first external circulation high-pressure pump 421 operates continuously, driving the material to circulate outside the reactor along the first circulation pipe 423. As the circulating material flows through the upper part of the first circulation pipe 423, it is heated by the electromagnetic heating coil 422 (or a shell-and-tube heat exchanger), and upon returning to the hydrogenation liquefaction reactor 43, it replenishes the heat for the reaction inside the reactor, while simultaneously circulating and stirring the material within. At the same time, the auxiliary heating components 47 surrounding the outer wall of the hydrogenation liquefaction reactor 43 work in conjunction with the external circulation heating to form multiple heating modes, jointly maintaining and precisely controlling the reaction temperature inside the reactor. The inclined filter device 431 inside the hydrogenation liquefaction reactor 43 continuously intercepts and filters pulverized coal and semi-coke. The self-propelled rotating blades 45 rotate continuously under the flow force generated by the fluid flow inside the reactor, constantly agitating the material at the bottom to prevent sedimentation. During the hydrogenation process, the cover 462 of the hydrogenation blowing assembly 46 is opened, and hydrogen gas is sprayed toward the filter device 431 through the nozzle 461. On the one hand, it blows away the bottom material to prevent sedimentation and blockage, and on the other hand, it performs reverse flushing of the filter device 431 to prevent blockage, ensuring the normal operation of the hydrogenation liquefaction reactor 43. In the non-operation state, the cover 462 is closed to prevent impurities from entering the nozzle 461.

[0061] (3) Flash Separation. After the hydrogenation liquefaction reaction reaches the predetermined time, the liquefied coal solution that has completed the reaction undergoes primary filtration through the filter device 431 inside the hydrogenation liquefaction reactor 43 under the action of pressure difference, and then secondary filtration through the external pipeline filter 411 on the connecting pipe 41, before entering the vacuum flash tank 51. Inside the vacuum flash tank 51, under the negative pressure environment provided by the vacuum pumping device, the liquefied coal solution undergoes flash separation. The light component gas (mainly solvent oil vapor and a small amount of light oil gas) is discharged from the top gas phase outlet of the vacuum flash tank 51 and enters the downstream condensation and collection unit 2. The heavy component heavy oil product is discharged and collected from the bottom of the vacuum flash tank 51. During the flash process, the second external circulation high-pressure pump 52 drives the material in the tank to circulate externally along the second circulation pipe 53 to promote the flash separation efficiency; the heating device 54 insulates and heats the pipeline to prevent the heavy oil from condensing and clogging.

[0062] (4) Condensation and Recovery. The high-temperature light component gas discharged from the top of the vacuum flash tank 51 first enters the water-cooled vacuum condenser 21, where it is cooled by circulating cooling water. Most of the solvent oil is condensed into a liquid phase here and flows into the solvent separator 22. In the solvent separator 22, gravity is used to achieve natural oil-water separation. The water phase is discharged from the bottom drain, and the solvent oil is discharged from the top outlet for recycling. The non-condensable gas from the outlet of the water-cooled vacuum condenser 21 enters the vacuum condenser 23, where it is deeply cooled by low-temperature cold water. The remaining light component oil gas is further condensed, and the liquid phase flows into the gas-liquid separator 24 for final gas-liquid separation. The non-condensable tail gas is extracted by a vacuum pump and then processed.

[0063] (5) Continuous operation. By setting up at least two sets of reaction flash evaporation units 1 (or at least two sets of complete integrated equipment), each unit operates alternately in a staggered sequence. Taking two sets of reaction flash evaporation units 1 as an example: when the first unit is in the hydrogenation liquefaction reaction stage, the second unit is performing the discharge, slag discharge and feeding of the next batch of materials; the operating cycles of the two units are staggered, so that from the macroscopic level of the whole system, the feeding of coal slurry, the discharge of liquefied coal solution, flash separation and solvent condensation recovery and other links are carried out without interruption, realizing continuous production of the whole process.

[0064] Finally, although this specification describes embodiments, not every embodiment contains only one independent technical solution. This way of describing the specification is only for clarity. Those skilled in the art should regard the specification as a whole. The technical solutions in each embodiment can also be appropriately combined to form other embodiments that can be understood by those skilled in the art.

Claims

1. An integrated equipment for a coal thermal solution extraction process, comprising a reaction flash evaporation unit (1) and a condensation collection unit (2), the two units being connected sequentially via pipelines, characterized in that: The reaction flash unit (1) consists of a longitudinally integrated hydrogen liquefaction reaction device (4) and a flash evaporation device (5), with a connecting pipe (41) fixed between them. An external pipeline filter (411) and a proportional unloading valve (412) are provided in the middle of the connecting pipe (41). The hydrogen liquefaction reaction device (4) includes a circulating heating device (42) and a hydrogenation liquefaction reactor (43), with a pipeline connecting them. A filter device (431) is provided in the hydrogenation liquefaction reactor (43), which, together with the external pipeline filter (411), forms a multi-filter device (431) structure. A poison protection device (44) consisting of a self-rotating blade (45) and a hydrogenation blowing assembly (46) is provided at the bottom of the inner side of the hydrogenation liquefaction reactor (43). The self-rotating blade (45) is driven to rotate only by the fluid inside the reactor. An auxiliary heating assembly (47) is provided around the hydrogenation liquefaction reactor (43) on the outer side.

2. The integrated equipment for a coal thermal solution extraction process according to claim 1, characterized in that: The anti-toxic device (44) includes a self-rotating blade (45) and a hydrogenation blowing assembly (46). The self-rotating blade (45) has a central rotating shaft (451) fixed at its bottom and is rotatably connected to the bottom of the hydrogenation liquefaction reactor (43) through the central rotating shaft (451). The self-rotating blade (45) is driven to rotate by the flow force generated by the fluid flow in the reactor. The hydrogenation blowing assembly (46) is fixed below the filter device (431). Multiple nozzles (461) are provided on the side of its outer wall facing the filter device (431), and an openable cap (462) is provided at the mouth edge of the nozzle (461).

3. The integrated equipment for a coal thermal solution extraction process according to claim 2, characterized in that: The nozzles (461) of the hydrogenation blowing assembly (46) are arranged equidistantly in the circumferential direction, and each nozzle (461) is positioned facing the filter device (431); the cover (462) is opened when the hydrogenation blowing assembly (46) is running and closed when it is not running, in order to prevent debris from entering the nozzle (461).

4. The integrated equipment for a coal thermal solution extraction process according to claim 1, characterized in that: The circulating heating device (42) includes a first external circulation high-pressure pump (421), an electromagnetic heating coil (422) or a shell-and-tube heat exchanger, and a first circulation pipe (423). The first circulation pipe (423) is disposed on the outer wall of the hydrogenation liquefaction reactor (43), and its two ends are fixedly connected to the upper and lower parts of the side wall of the hydrogenation liquefaction reactor (43), respectively. The electromagnetic heating coil (422) or the shell-and-tube heat exchanger is disposed on the upper part of the first circulation pipe (423). The first external circulation high-pressure pump (421) is disposed on the lower part of the first circulation pipe (423). The lower end of the first circulation pipe (423) is obliquely connected to the inner wall of the hydrogenation liquefaction reactor (43). The auxiliary heating component (47) is disposed around the outside of the hydrogenation liquefaction reactor (43) and cooperates with the electromagnetic heating coil (422) or the shell-and-tube heat exchanger disposed on the first circulation pipe (423) to form multiple heating modes.

5. The integrated equipment for a coal thermal solution extraction process according to claim 1, characterized in that: The filter device (431) is fixed obliquely inside the hydrogenation liquefaction reactor (43), and the hydrogenation blowing assembly (46) performs reverse flushing of the filter device (431) during the hydrogenation process.

6. The integrated equipment for a coal thermal solution extraction process according to claim 1, characterized in that: The flash evaporation device (5) includes a vacuum flash tank (51), a second external circulation high-pressure pump (52), a second circulation pipe (53), and a heat tracing device (54). The vacuum flash tank (51) is located below the hydrogen liquefaction reaction device (4) and is connected through a connecting pipe (41). The second circulation pipe (53) is fixed to the outside of the vacuum flash tank (51) and is connected to the inner wall of the vacuum flash tank (51). The second external circulation high-pressure pump (52) is located in the middle of the second circulation pipe (53). The heat tracing device (54) is fixed to the outer wall of the second circulation pipe (53).

7. The integrated equipment for a coal thermal solution extraction process according to claim 1, characterized in that: The condensation collection unit (2) includes a water-cooled vacuum condenser (21), a solvent separator (22), a vacuum condenser (23), and a gas-liquid separator (24). One end of the water-cooled vacuum condenser (21) is connected to the flash evaporation device (5) through a pipe, and the other end is connected to the solvent separator (22) through a pipe. The solvent separator (22) is connected to the vacuum condenser (23) and the gas-liquid separator (24) through pipes respectively.

8. The integrated equipment for a coal thermal solution extraction process according to claim 1, characterized in that: The reaction flash unit (1) is provided in at least two sets.

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