Coal quality-based utilization device and method based on coupling process

Abstract

The application discloses a coal quality-based utilization device and method based on a coupling process, which comprises a pyrolysis gasification unit, a purification and recovery unit, a separation and utilization unit and an oil product processing unit; the pyrolysis gasification unit completes fast pressurization and hydrogenation of coal powder to realize segmented conversion into pyrolysis oil, semi-coke and synthesis gas; the semi-coke completes an efficient gasification reaction through built-in circulation and external circulation return material channels; the purification and recovery unit realizes collection of the pyrolysis oil and solid residues and graded cyclic utilization of heavy oil and light oil through multi-stage purification, dust removal and washing and recovery of high-temperature oil gas; the separation and utilization unit realizes graded recovery of the light oil and pyrolysis water and separation and cyclic utilization of the synthesis gas through efficient separation and recovery of gas-liquid two phases; and the oil product processing unit realizes cyclic reuse of the solid-containing residues and semi-coke by using heavy components of coal tar and ash and slag. The application has the characteristics of obvious synergistic effect, high energy conversion efficiency, high oil product yield, high synthesis gas content and large processing scale.

Description

Technical Field

[0001] This invention relates to the field of coal fractionation and conversion technology, specifically to a coal fractionation and utilization device and method based on a coupling process. Background Technology

[0002] Clean and efficient coal conversion starts from the characteristics of the resource itself. It utilizes the structural features of low coalification degree, high volatile content, many side chains, and high hydrogen and oxygen content to convert coal into energy states such as coal gas, coal tar, and semi-coke through low-energy and low-material consumption medium- and low-temperature pyrolysis. The above products are further converted to obtain clean fuels such as oil and gas, as well as high-value-added chemical products.

[0003] The technology for the graded utilization of coal has not yet achieved a true leap forward. It requires a considerable period of industrial verification, demonstration, upgrading, and improvement to address issues such as long-term operation, good economic indicators, environmental compliance, and the extension and matching of the industrial chain. It is crucial to leverage the significant characteristics of coal-based oil products and continue research into coal-based specialty fuels, coal-based carbon materials, and coal-based biodegradable materials to achieve breakthroughs in high-performance, high-value-added, and high-end differentiated products. Simultaneously, attention should be paid to the integration and coordinated development of industries such as coal chemical, petrochemical, and hydrogen energy, exploring new paths for industrial development aimed at reducing carbon dioxide emissions. This will allow for leveraging differentiated characteristics to upgrade and optimize coal graded utilization technologies with optimal material and energy consumption, overcoming the technological bottlenecks in producing high-performance, high-value-added, and high-end differentiated products.

[0004] CN110423627A provides a gas-solid heat carrier dual-circulation pyrolysis device, which pyrolyzes carbon-containing materials and uses the resulting coke and crude syngas as heat carriers to carry out a cyclic reaction in a dual-circulation reaction system, so that the carbon-containing materials are fully pyrolyzed and the yield of pyrolysis products is improved. The coal tar yield reaches about 17%, but the coal tar has relatively poor properties and a large content of solid particles, which affects the deep processing and utilization of coal tar and is not conducive to the further extension of the industrial chain.

[0005] CN114381294A discloses an apparatus for producing coal-based special fuels through coal pyrolysis and hydrogenation. A portion of the coal is rapidly pyrolyzed to produce coal tar, while the remaining portion is hydrogenated with the coal tar via a suspended bed to produce fuel oil. However, the key process flows, such as coal pyrolysis and gas-solid dust removal, are not specifically described. In actual operation, the structure of the pyrolysis reactor and gas-solid separation unit determines the pyrolysis depth and product distribution. The relatively mild operating conditions result in insufficient conversion depth, making it difficult to achieve deep pyrolysis under high pressure and produce high-yield, high-quality coal tar, thus hindering the production of sufficient coal tar for the hydrogenation reaction. Furthermore, the hydrogen used in the hydrogenation process needs to be purchased externally, resulting in poor self-sufficiency and low economic efficiency. Summary of the Invention

[0006] In order to overcome the shortcomings of the prior art, the present invention aims to provide a coal fractionation and utilization device and method based on a coupling process, which has the characteristics of significant synergistic effect, high energy conversion efficiency, high oil yield, high syngas content and large processing scale.

[0007] To achieve the above objectives, the technical solution adopted by the present invention is as follows:

[0008] A coal fractionation and utilization device based on a coupled process includes a pyrolysis and gasification unit, a purification and recovery unit, a separation and utilization unit, and an oil processing unit.

[0009] The pyrolysis gasification unit completes the rapid pressurization and hydrogenation of pulverized coal into pyrolysis oil, semi-coke and syngas in stages. The semi-coke completes the efficient gasification reaction through the built-in circulation and external circulation return channels.

[0010] The purification and recovery unit achieves the collection of pyrolysis oil and solid residues and the graded recycling of heavy oil and light oil through multi-stage purification, dust removal and washing recovery of high-temperature oil and gas.

[0011] The separation and utilization unit achieves graded recovery of light oil and pyrolysis water, as well as separation and recycling of syngas through efficient separation and recovery of gas and liquid phases.

[0012] The oil processing unit utilizes heavy components of coal tar and ash residue as feedstock for enhanced hydrogenation to produce coal-based specialty fuel oils, achieving the recycling of solid residues and semi-coke.

[0013] The pyrolysis gasification unit includes a pressurized fluidized feeder 40, a combustion gasifier 2, and a multi-stage gas-solid separator 6, all connected to the pyrolyzer 1. The upper part of the pyrolyzer 1 is connected to the lower inlet of the combustion gasifier 2 to form an upper solid circulation, and the bottom of the pyrolyzer 1 is connected to the upper inlet of the combustion gasifier 2 to form a lower solid circulation. The input end of the combustion gasifier 2 is connected to the output end of the multi-stage gas-solid separator 6 and the atomizing feeder 27. The output end of the combustion gasifier 2 is connected to the input end of the ash cooler 7. The inlet of the atomizing feeder 27 is connected to the output ends of the steam heater 5, the liquid-solid enhanced separator 9, the oil-water enhanced separator 14, and the high-pressure separator 25, respectively.

[0014] The purification and recovery unit includes a pyrolyzer 1 and a circulating gas preheater 19, both connected to the inlet of a multi-stage gas-solid separator 6. The upper outlet of the multi-stage gas-solid separator 6 is connected to the input of a primary washing cooler 8, and the bottom outlet of the multi-stage gas-solid separator 6 is connected to the bottom inlet of a combustion gasifier 2, thus forming a solid external circulation. The inlet of the ash cooler 7 is connected to the outputs of the combustion gasifier 2, the multi-stage gas-solid separator 6, and the oil-water enhanced separator 14. The gas phase outlet of the ash cooler 7 is connected to the gas phase inlet of a steam heater 5, and the solid phase outlet of the ash cooler 7 is connected to the solid phase inlet of an oil-coal slurry tank 22. The inlet of the liquid-solid enhanced separator 9 is connected to the output of the primary washing cooler 8, and the liquid-solid enhanced... The liquid phase outlet of separator 9 is connected to the upper part of primary washing cooler 8 and the liquid phase inlet of oil-coal slurry tank 22, respectively. The solid phase outlet of liquid-solid enhanced separator 9 is connected to atomizing feeder 27 and solid phase inlet of oil-coal slurry tank 22, respectively. The top outlet of primary washing cooler 8 is connected to the inlet of secondary washing cooler 10. The outlet of secondary washing cooler 10 is connected to the input end of primary fractionator 11 and primary gas-liquid condenser 12, respectively. The upper outlet of primary fractionator 11 is connected to the input end of secondary enhanced hydrogenation reactor 24 and phenol extraction device 50. The lower outlet of phenol extraction device 50 is connected to the input end of secondary enhanced hydrogenation reactor 24. The lower output end of primary fractionator 11 is connected to the input end of oil-coal slurry tank 22.

[0015] The separation and utilization unit includes a cryogenic purifier 13 connected to the upper outlet of the primary gas-liquid condenser 12. The lower outlets of both the primary gas-liquid condenser 12 and the cryogenic purifier 13 are connected to the inlet of the oil-water enhanced separator 14. The upper outlet of the cryogenic purifier 13 is connected to the inlet of the syngas storage tank 15. The output end of the syngas storage tank 15 is connected to the input end of a multi-stage adsorption tank 16. The output end of the multi-stage adsorption tank 16 is divided into two paths: one path is connected to the input end of the circulating gas separator 17, and the other path is connected to the input end of the hydrogen extraction device 20. The output end of the circulating gas separator 17 is connected to the input end of the carbon dioxide booster 18, and the output end of the carbon dioxide booster 18 is connected to the input end of the circulating gas preheater 19. The output end of the hydrogen extraction device 20 is connected to the input end of the hydrogen booster 21, and the output end of the hydrogen booster 21 is divided into two paths, which are respectively connected to the input ends of the primary enhanced hydrogenation reactor 23 and the secondary enhanced hydrogenation reactor 24.

[0016] The oil processing unit includes a primary enhanced hydrogenation reactor 23 connected to the outlet of the oil-coal slurry tank 22. The outlet of the primary enhanced hydrogenation reactor 23 is connected to the inlet of a high-pressure separator 25, and the output of the high-pressure separator 25 is connected to the input of an atomizing feeder 27. The inlet of the secondary enhanced hydrogenation reactor 24 is connected to the outlets of the high-pressure separator 25 and the phenol extraction unit 50. The outlets of the secondary enhanced hydrogenation reactor 24 and the oil-water enhanced separator 14 are both connected to the inlet of the product fractionator 26.

[0017] The output end of the pyrolyzer 1 is connected to the input end of the pyrolysis sampling device 3. The pyrolysis sampling device 3 includes a high-temperature preprocessor 28. The output end of the high-temperature preprocessor 28 is connected to the input end of the first-stage quench washing tank 29. The output end of the first-stage quench washing tank 29 is connected to the input end of the second-stage washing and cooling tank 30. The output end of the second-stage washing and cooling tank 30 is connected to the input ends of the pyrolysis gas flow meter 33 and the reflux tank 31, respectively. The output end of the reflux tank 31 is connected to the input end of the first-stage quench washing tank 29.

[0018] Both the primary quench washing tank 29 and the secondary washing cooling tank 30 are connected to a pyrolysis cycle refrigeration system 32.

[0019] The output end of the combustion gasifier 2 is connected to the input end of the gasification sampling device 4. The gasification sampling device 4 includes a primary gas cooler 34. The output end of the primary gas cooler 34 is connected to the input end of the depth filter 35. The output end of the depth filter 35 is connected to the input end of the secondary gas cooler 36. The output end of the secondary gas cooler 36 is connected to the input end of the gas-liquid separator 37.

[0020] Both the primary gas cooler 34 and the secondary gas cooler 36 are connected to a vaporization cycle refrigeration system 38; the gas-liquid separator 37 is connected to a vaporization gas flow meter 39.

[0021] The multi-stage gas-solid separator 6 includes a primary gas-solid separator and a secondary gas-solid separator, wherein the secondary gas-solid separator is composed of a large-pore support substrate layer and a small-pore membrane filter layer.

[0022] The primary washing cooler 8 includes an upper porous settling hood, a middle multi-stage nozzle, filter screen and baffle, and a bottom settling cone and baffle.

[0023] Both the primary enhanced hydrogenation reactor 23 and the secondary enhanced hydrogenation reactor 24 include 1-3 reactors in series.

[0024] The pressurized fluidized feeder 40 includes a cylinder 41, inside which are arranged a sleeve 42, a flute 43, a sintered wire mesh 44, a solid distribution plate 45, and a gas distribution pipe 46. A vibrator 47 is connected to the outside of the cylinder 41 to enable feeding of the pyrolyzer 1 under a high pressure of 10.0 MPa at a feed rate of 10-10000 kg / h. The flute 43 is fixedly connected to the top of the sleeve 42 by a flange, and is centrally symmetrically distributed, extending into the sleeve 42, with an insertion length accounting for 1 / 2-2 / 3 of the total sleeve length. The upper part of the sleeve 42 is connected to the top of the cylinder 41 by a flange, extending into the cylinder 41, with an insertion length accounting for 1 / 3-2 / 3 of the total sleeve length. The lower part of the sleeve 42 is connected to the upper part of the solid distribution plate 45. The lower part of the sleeve 42 is provided with an annular filter channel, allowing 10-5 cm diameter coal powder from the annular gap between the sleeve 42 and the flute tube 43 to pass through and enter the cylinder 41. A sintered wire mesh 44 connected to a gas distribution plate 46 is provided at the top of the solid distribution plate 45, and a gas distribution plate 46 connected to a fluidization port is provided at the bottom. The angle of the upper part of the solid distribution plate 45 is 10-70°, and the filtration accuracy of the sintered wire mesh 44 is 0.1-100 μm. A method for using a coal fractionation and utilization device based on a coupled process includes the following steps;

[0025] Step 1: Pyrolysis and Gasification

[0026] Solid particulate heat carriers circulate at a high rate of 50-300 between pyrolyzer 1, combustion gasifier 2, and multi-stage gas-solid separator 6, gradually heating the system to 400-800℃. Powdered coal from pressurized fluidized feeder 40 enters pyrolyzer 1, where it is thoroughly mixed and fluidized with the high-temperature solid particles, undergoing rapid pyrolysis to produce high-temperature oil gas and semi-coke. 50-70% of the semi-coke and heat carrier solid particles are returned to combustion gasifier 2 via an internal solid circulation return channel. The remaining 30-50% of the semi-coke and heat carrier solid particles, along with the high-temperature oil gas, enters multi-stage gas-solid separator 6, where the semi-coke and heat carrier solid particles are captured and returned to combustion gasifier 2. When the material level in the reaction system is high (the material level is determined by the pressure difference in the reaction system (upper pressure point - lower pressure point) P = ρgh (ρ is the particle size distribution)... The pressure difference (particle density, g is the acceleration due to gravity, h is the material level) is used to determine the reaction system. When the pressure difference value of a certain segment fed back by the DCS system is >25-30KPa, it indicates that the material level in the reaction system is too high, which is not conducive to fluidization circulation and online ash discharge is required. The pressure difference (upper pressure point - lower pressure point) in the reaction system is P = ρgh (ρ is particle density, g is the acceleration due to gravity, h is the material level). When the pressure difference value of a certain segment fed back by the system is >25-30KPa, it indicates that the material level in the reaction system is too high, which is not conducive to fluidization circulation and online ash discharge is required. Some of the high-temperature ash and slag produced by the combustion gasifier 2 and the multi-stage gas-solid separator 6 enter the ash and slag cooler 7, where it exchanges heat with the wastewater from the oil-water enhanced separator 14. The by-product medium-pressure steam with a pressure of 2.5-6MPa and a temperature of 350-450℃ enters the steam heater 5, and the ash and slag are discharged from the system.

[0027] Step 2, purification and recycling

[0028] High-temperature oil and gas are cooled and washed in primary scrubbing cooler 8 and secondary scrubbing cooler 10 to obtain heavy distillate oil and light distillate oil as cooling media, respectively. The liquid product collected in primary scrubbing cooler 8 enters liquid-solid enhanced separator 9, and after separation, heavy distillate oil and solid residue are obtained. The liquid product collected in secondary scrubbing cooler 10 enters primary fractionator 11. The oil and gas washed by secondary scrubbing cooler 10 enters primary gas-liquid condenser 12, cryogenic purifier 13 and oil-water enhanced separator 14 in sequence to recover light oil, pyrolysis water and syngas in stages. The light oil produced enters product fractionator 26. The pyrolysis water produced is mixed with the solid residue produced by high-pressure separator 25 and liquid-solid enhanced separator 9. Under the atomization of steam, it enters combustion gasifier 2 through atomizing feeder 27.

[0029] Step 3, Oil Processing

[0030] The solid residue produced by the liquid-solid separator 9 is partially fed into the combustion gasifier 2 via the atomizing feeder 27 along with the solid residue from the high-pressure separator 25, serving as a supplementary carbon source for regasification. Another portion enters the oil-coal slurry tank 22, sequentially passing through the primary enhanced hydrogenation reactor 23, the high-pressure separator 25, and the secondary enhanced hydrogenation reactor 24. The resulting tail oil is fed into the oil-coal slurry tank 22 as supplementary feedstock for heavy oil production. Hydrogen from the booster unit 21 enters the primary enhanced hydrogenation reactor 23 and the secondary enhanced hydrogenation reactor 24 as hydrogen supply gas for reaction. The hydrogenated oil from the secondary enhanced hydrogenation reactor 24 and the light oil from the oil-water enhanced separator 14 enter the product fractionator 26 for further fractionation to produce naphtha, naphthenic oil, and specialty fuel oils, among other coal-based oil products.

[0031] In step 1, the internal pressure of pyrolyzer 1 and combustion gasifier 2 is 0.001-10.0MPa, and the pyrolysis temperature inside pyrolyzer 1 is 400-800℃, and the gas velocity is 2-20m / s.

[0032] The vaporization temperature inside the combustion vaporizer 2 is 900-1400℃, the gas velocity is 0.1-2m / s, and the solid circulation ratio is 10-300 times.

[0033] The beneficial effects of this invention are:

[0034] 1. This invention uses a pyrolyzer and a combustion gasifier as an integrated coupled circulating fluidized bed reactor to rapidly pressurize and hydrogenate pulverized coal into pyrolysis oil, semi-coke, and syngas in stages. Utilizing built-in and external solid particle circulation return channels, it achieves efficient separation of semi-coke with different properties and particle sizes. The semi-coke is used in the gasification reaction to produce hydrogen-rich and carbon monoxide-rich syngas. Through the synergistic effect of interfacial transfer and enhanced hydrogenation, it achieves hydrogenation stabilization of free radicals from primary coal pyrolysis and suppresses secondary reactions such as cross-linking and polymerization. Therefore, the coal fractionation and utilization process of this invention features high oil and gas yield, high syngas composition and calorific value, and significant lightening of the pyrolysis oil.

[0035] 2. This invention uses the solid oil sludge, heavy coal tar components, and ash generated from pyrolysis-gasification as raw materials for hydrogenation reactions. This solves the problem that the relatively low reaction temperature in fluidized beds leads to high carbon content in the ash and low conversion rate, thus achieving deep resource utilization of high-carbon solid waste. The pyrolysis wastewater, after separation, is used as an additive for coal-water slurry, reducing wastewater treatment costs while improving the stability of the coal-water slurry. The coupled process further improves the coal conversion rate and the yield of clean oil products, extends the industrial chain of coal fractionation utilization, enhances the overall technical and economic efficiency of the process, and achieves breakthroughs in high-performance, high-value-added, and high-end differentiated products.

[0036] 3. The process of this invention ultimately does not produce semi-coke or solid residue, which is reflected in the following aspects: First, the semi-coke produced participates in the gasification reaction; second, the solid residue produced by the enhanced hydrogenation reaction is also returned to the combustion gasifier for gasification reaction to supplement the insufficient carbon source in the gasification reaction; third, the syngas produced provides heat and an active atmosphere for the pyrolysis reaction, realizing an effective combination and flexible control of dry gasification and wet gasification; in addition, the alkali metal / alkaline earth metal in the residue and the catalyst destroy the coking reaction of coal, accelerate the release of volatiles in coal, and improve the yield of pyrolysis oil and the effective gas content of syngas.

[0037] 4. The process of this invention separates and reuses the pyrolysis water recovered from cooling, converting it into steam to participate in the gasification reaction as a gasifying agent. This achieves the goal of reducing steam consumption in the front-end gasification reaction and recycling pyrolysis water at the tail end, significantly reducing steam consumption and saving on equipment operating costs. At the same time, carbon dioxide and hydrogen in the self-produced syngas are efficiently separated and recycled, serving as the carbon source for the front-end pyrolysis reaction and the hydrogen source for the back-end enhanced hydrogenation reaction, respectively. This increases the effective gas content of the syngas and the quality of the oil, significantly reducing the equipment's material consumption, energy consumption, and carbon emissions, and significantly improving the overall energy conversion efficiency.

[0038] 5. The process of this invention is flexible and versatile, capable of producing high-yield, high-quality tar and syngas, as well as coal-based special fuels, achieving oil production at both ends. It features continuous processing of medium and high-rank coals, wide adaptability to raw materials, high conversion efficiency, high pyrolysis oil yield, high effective gas content in syngas, a variety of special fuels, and ease of large-scale and large-scale application. It is a green, efficient, and economical coal fractionation method that improves the overall technical and economic efficiency of the process, achieving breakthroughs in high-performance, high-value-added, and high-end differentiated products.

[0039] 6. The designed and developed pyrolysis sampling device and gasification sampling device are specifically designed to handle oil- and dust-containing pyrolysis gases and dust-containing gasification gases under harsh conditions such as high temperature and high pressure. They simultaneously obtain full-fraction coal tar, dust, pyrolysis gas or syngas. By simultaneously analyzing and comparing the ash and carbon content, volatile matter, syngas components and basic physical properties of tar in the pyrolysis and gasification sampling devices, the circulation ratio, operating parameters, feed rate and online ash removal of the pyrolyzer and combustion gasifier can be adjusted. The pyrolysis and gasification reaction processes are coupled and optimized to achieve rapid pyrolysis of coal powder and efficient gasification of semi-coke / solid residue, and obtain high-quality oil and gas products. Attached Figure Description

[0040] Figure 1 This is a schematic diagram of the overall process of the present invention.

[0041] Figure 2 This is a schematic diagram of the working process of the pyrolysis sampling device of the present invention.

[0042] Figure 3This is a schematic diagram of the working process of the gasification sampling device of the present invention.

[0043] Figure 4 This is a schematic diagram of the fluidized pressurized feeder of the present invention.

[0044] In the diagram: 1-Pyrolysis unit; 2-Combustion gasifier; 3-Pyrolysis sampling device; 4-Gasification sampling device; 5-Steam heater; 6-Multi-stage gas-solid separator; 7-Ash cooler; 8-Primary scrubbing cooler; 9-Liquid-solid enhanced separator; 10-Secondary scrubbing cooler; 11-Primary fractionator; 12-Primary gas-liquid condenser; 13-Cryogenic purifier; 14-Oil-water enhanced separator; 15-Synthesis gas storage tank; 16-Multi-stage adsorption tank; 17-Circulating gas separator; 18-Carbon dioxide booster; 19-Circulating gas preheater; 20-Hydrogen extraction unit; 21-Hydrogen booster; 22-Oil-coal slurry tank; 23-Primary enhanced hydrogenation reactor; 24-Secondary enhanced hydrogenation reactor ; 25-High-pressure separator; 26-Product fractionator; 27-Atomizing feeder; 28-High-temperature pre-processor; 29-First-stage quench washing tank; 30-Second-stage washing and cooling tank; 31-Reflux tank; 32-Pyrolysis cycle refrigeration system; 33-Pyrolysis gas flow meter; 34-Primary gas cooler; 35-Depth filter; 36-Secondary gas cooler; 37-Gas-liquid separator; 38-Vaporization cycle refrigeration system; 39-Vaporization gas flow meter; 40-Pressurized fluidized feeder; 41-Cylinder; 42-Shell; 43-Flute tube; 44-Sintered wire mesh; 45-Solid distribution plate; 46-Gas distribution pipe; 47-Vibrator; 48-Fluorization port; 49-Drainage port; 50-Phenol extraction device. Detailed Implementation

[0045] The present invention will be further described in detail below with reference to the embodiments.

[0046] like Figure 1 As shown, a coal fractionation and utilization device based on a coupled process includes a pyrolysis gasification unit, a purification and recovery unit, a separation and utilization unit, and an oil processing unit. The pyrolysis gasification unit rapidly pressurizes and hydrogenates pulverized coal in stages to convert it into pyrolysis oil, semi-coke, and syngas. The semi-coke undergoes efficient gasification through an internal circulation and an external circulation return channel. The purification and recovery unit achieves the collection of pyrolysis oil and solid residues, and the graded recycling of heavy and light oils through multi-stage purification, dust removal, and washing and recovery of high-temperature oil and gas. The separation and utilization unit achieves the graded recovery of light oil and pyrolysis water, and the separation and recycling of syngas through efficient gas-liquid two-phase separation and recovery. The oil processing unit utilizes the heavy components of coal tar and ash residue as feedstock for enhanced hydrogenation to produce coal-based specialty fuel oils, achieving the recycling of solid residues and semi-coke.

[0047] The pyrolysis gasification unit includes a pressurized fluidized feeder 40, a combustion gasifier 2, and a multi-stage gas-solid separator 6 connected to the pyrolyzer 1; a steam heater 5, a multi-stage gas-solid separator 6, an ash cooler 7, and an atomizing feeder 27 connected to the combustion gasifier 2; the upper and lower outlets of the pyrolyzer 1 are respectively connected to the lower inlet of the combustion gasifier 2, thereby forming an internal solid upper circulation and a solid lower circulation; the lower part of the combustion gasifier 2 is connected to the atomizing feeder 27, and the inlet of the atomizing feeder 27 is connected to the liquid-solid separator 9, the oil-water enhanced separator 14, and the high-pressure separator 25; the pyrolysis sampling device 3 is connected to the pyrolyzer 1, and the gasification sampling device 4 is connected to the combustion gasifier 2;

[0048] Preferably, the multi-stage gas-solid separator 6 in this embodiment consists of a primary gas-solid separator and a secondary gas-solid separator. The proportion of particles captured with a diameter of 200-500 μm is 50-70%, and the proportion of particles captured with a diameter of 5-200 μm is 30-50%. The secondary gas-solid separator consists of a large-pore support substrate layer and a small-pore membrane filter layer. The internal operating temperature of the multi-stage gas-solid separator 6 is 400-800℃, the operating pressure is 0.001-10.0 MPa, the filter element pore size is 20-150 μm, the porosity is 30-45%, and the filtration accuracy is 1-30 μm. The backflush gas medium is self-produced syngas, and the backflush gas pressure is 2-5 times the system pressure.

[0049] The pyrolyzer 1 and the combustion gasifier 2 are connected by a built-in solid circulation return channel and an external solid circulation return channel. The solid circulation particles are one or more combinations of coal powder, coal ash, quartz sand, semi-coke, petroleum coke and other carbon-containing materials, with a particle size range of 10-500μm. The bed level is controlled by adding or discharging solid particles online. The pyrolyzer 1 requires the raw coal to have a particle size of 10-500μm, a water content of <20%, a volatile matter content of 10-40%, and an ash content of >18%. It is suitable for medium and high-rank coals with an ash melting point of 1400℃. The coal powder is fed stably under high pressure of 10.0MPa by a fluidized pressurized feeder, with a coal powder feed rate of 10-10000kg / h.

[0050] Preferably, in this embodiment, the pyrolyzer 1 has a pressure of 0.001-10.0 MPa, a pyrolysis temperature of 400-800℃, a pyrolysis gas velocity of 5-18 m / s, and a coal powder residence time of 2-40 s; the combustion gasifier 2 has a pressure of 0.001-10.0 MPa, a gasification temperature of 900-1400℃, a gas velocity of 0.1-2 m / s, a residence time of 2-30 s, a solids circulation ratio of 50-300 times, a carbon conversion rate >98%, an effective gas component of syngas >80%, a cold gas efficiency >75%, and a syngas calorific value >2300 kcal / Nm³. 3 ;

[0051] Preferably, the gasifying agent enters the combustion gasifier 2 through three channels: upper, middle, and lower. The gasifying agent type is oxygen, air, steam, or carbon dioxide. The gasifying agent temperature is 100-350℃, and the pressure is 0.001-10.0MPa. The gasifying agent ratio for the upper, middle, and lower channels is 5-20%: 20-50%: 30-75%. Each channel is equipped with 3-10 gasifying agent nozzles arranged in a staggered ring, with the nozzles angled downwards at 10-60 degrees, the nozzle gas velocity at 5-100m / s, and the oxygen concentration in the gasifying agent at the nozzle at 10-70%.

[0052] Preferably, the pyrolysis gasification system, the purification and recovery system, and the connecting pipelines are equipped with heat tracing and insulation devices to ensure that the operating temperature is greater than 400°C. The heat tracing and insulation devices ensure that the temperature from the outlet of the pyrolyzer 1 to the inlet of the multi-stage gas-solid separator 6 and the inlet of the pyrolysis sampling device 3, from the outlet of the combustion gasifier 2 to the inlet of the gasification sampling device 4, and the connecting pipelines is greater than 400°C.

[0053] The purification and recovery unit includes a pyrolyzer 1 and a circulating gas preheater 19 connected to the inlet of the multi-stage gas-solid separator 6. The upper outlet of the multi-stage gas-solid separator 6 is connected to a primary washing cooler 8, and the bottom outlet of the multi-stage gas-solid separator 6 is connected to the lower inlet of the combustion gasifier 2 to form a solid external circulation. The inlet of the ash cooler 7 is connected to the combustion gasifier 2, the multi-stage gas-solid separator 6, and the oil-water enhanced separator 14. The gas phase outlet of the ash cooler 7 is connected to a steam heater 5, and the solid phase outlet of the ash cooler 7 is connected to an oil-coal slurry tank 22. The inlet of the liquid-solid enhanced separator 9 is connected to the primary washing cooler 8, and the liquid phase outlet of the liquid-solid enhanced separator 9 is respectively... The upper inlet of the oil-coal slurry tank 22 is connected to the primary washing cooler 8. The solid phase outlet of the liquid-solid enhanced separator 9 is connected to the atomizing feeder 27 and the oil-coal slurry tank 22, respectively. The inlet of the secondary washing cooler 10 is connected to the primary washing cooler 8. The outlet of the secondary washing cooler 10 is connected to the primary fractionator 11 and the primary gas-liquid condenser 12, respectively. The bottom of the secondary washing cooler 10 is also connected to its own upper part. The upper part of the primary fractionator 11 is connected to the secondary enhanced hydrogenation reactor 24 and the phenol extraction device 50. The lower outlet of the phenol extraction device 50 is connected to the secondary enhanced hydrogenation reactor 24. The lower part of the primary fractionator 11 is connected to the oil-coal slurry tank 22.

[0054] Preferably, in this embodiment, the primary washing cooler 8 is provided with a porous settling hood at the top, a multi-stage spray nozzle, filter screen and baffle in the middle, and a settling cone at the bottom. It uses distillate oil with a temperature >350℃ for circulating washing, with an operating gas velocity of 0.1-6.0 m / s, a process gas temperature of 200-400℃, a pressure of 0.001-10.0 MPa, and a dust content of 0-2.0%. The secondary washing cooler 10 is provided with a wire mesh demister and a gas-liquid enhanced separator at the top, a horizontal tray and herringbone baffle in the middle, and a settling cone at the bottom. It uses distillate oil with a temperature <350℃ for circulating washing, with an operating gas velocity of 0.2-5.0 m / s, a process gas temperature of 100-250℃, a pressure of 0.001-10.0 MPa, and a dust content of 0-1.0%.

[0055] Preferably, the raw materials for the oil-coal slurry tank 22 in this embodiment are distillate oil, ash, solid residue and coal powder at >350℃, hydrogenated oil from the secondary enhanced hydrogenation reactor 24 and light oil from the water enhanced separator 14, and coal-based oil products such as naphtha, naphthenic oil, special fuel oil and aerospace kerosene that are fractionated by the product fractionator 26. The tail oil of the secondary enhanced hydrogenation reactor 24 is recycled into the oil-coal slurry tank 22 as a supplementary feedstock for heavy oil. After the solid residue produced by the high-pressure separator 25 and the liquid-solid enhanced separator 9 and the pyrolysis water produced by the primary fractionator 11 are mixed, the mixture is returned to the combustion gasifier 2 through the atomizing feeder 27 for reprocessing.

[0056] The separation and utilization unit includes a primary gas-liquid condenser 12. The upper outlet of the primary gas-liquid condenser 12 is connected to a cryogenic purifier 13, and the lower outlet of the primary gas-liquid condenser 12 is connected to an oil-water enhanced separator 14. The outlet of the cryogenic purifier 13 is connected to the oil-water enhanced separator 14 and a syngas storage tank 15. The syngas storage tank 15 is connected to a multi-stage adsorption tank 16. The multi-stage adsorption tank 16 is connected to a circulating gas separator 17 and a hydrogen extraction device 20. The circulating gas separator 17 is connected to a carbon dioxide booster 18, which is connected to a circulating gas preheater 19. The hydrogen extraction device 20 is connected to a hydrogen... The gas booster 21 and the hydrogen booster 21 are respectively connected to the primary enhanced hydrogenation reactor 23 and the secondary enhanced hydrogenation reactor 24; the gas inside the syngas storage tank 15 is purified and separated by passing through the multi-stage adsorption tank 16 and the circulating gas separator 17 in sequence; the separated carbon dioxide gas enters the pyrolysis unit 1 and the multi-stage gas-solid separator 6 through the carbon dioxide booster 18 and the circulating gas preheater 19, and enters the combustion gasifier 2 through the atomizing feeder 27; the separated hydrogen enters the primary enhanced hydrogenation reactor 23 and the secondary enhanced hydrogenation reactor 24 through the hydrogen extraction unit 20 and the hydrogen booster 21;

[0057] Preferably, the primary enhanced hydrogenation reactor 23 in this embodiment contains 1-3 reactors, with a pressure of 5.0-25.0 MPa, a temperature of 400-550°C, a hydrogen-to-oil ratio of 800-2200, and a space velocity of 0.2-2.0 h⁻¹. -1 The secondary enhanced hydrotreating reactor 24 contains 1-3 reactors, with feedstock being distillate oil at <350℃, pressure 5.0-25.0 MPa, temperature 350-500℃, hydrogen-to-oil ratio 1000-2400, and space velocity 0.5-3.0 h⁻¹. -1 The high-pressure separator 25 operates at a pressure of 5.0-25.0 MPa, a temperature of 400-550℃, a hydrogen-to-oil ratio of 1200-2600, and a space velocity of 0.5-3.0 h⁻¹. -1 .

[0058] The oil processing unit includes a liquid-solid enhanced separator 9 and a primary fractionator 11 connected to the inlet of the oil-coal slurry tank 22; the outlet of the oil-coal slurry tank 22 is connected to a primary enhanced hydrogenation reactor 23; the inlet of the primary enhanced hydrogenation reactor 23 is also connected to a hydrogen booster 21; the outlet of the primary enhanced hydrogenation reactor 23 is connected to a high-pressure separator 25; the inlet of the secondary enhanced hydrogenation reactor 24 is connected to the primary fractionator 11, the high-pressure separator 25, the hydrogen booster 21, and the phenol extraction unit 50; and the inlet of the product fractionator 26 is connected to an oil-water enhanced separator 14 and the secondary enhanced hydrogenation reactor 24.

[0059] Preferably, the distillate oil at <250°C in the primary fractionator 11 enters the phenol extraction unit 50. The upper part of the phenol extraction unit 50 produces coarse powder, while the dephenolized oil in the lower part, together with the distillate oil at 250-380°C in the primary fractionator 11 and the distillate oil at <380°C in the high-pressure separator 25, enters the secondary enhanced hydrogenation reactor 24 for reaction.

[0060] like Figure 2 As shown, the pyrolysis sampling device 3 includes a high-temperature pre-processor 28, a primary quench washing tank 29, a secondary washing and cooling tank 30, a reflux tank 31, a pyrolysis circulating refrigeration system 32, and a pyrolysis gas flow meter 33, realizing the two-phase separation of oil and dust in the pyrolysis gas and online analysis of the purified gas; wherein: the high-temperature pre-processor 28 consists of an upper sintered filter element zone, a middle fluidized loosening zone, and a lower powder collection zone, which uses backflushing air to collect powder on the surface of the filter element online, the filter element accuracy is 1-20μm, suitable for dust content of 10-300g / Nm in the pyrolysis gas. 3The backflush gas medium is self-produced syngas, and the backflush gas pressure is 2-5 times the system pressure. The secondary washing and cooling tank 30 consists of an upper washing section, a middle cooling section, and a bottom filter inner cylinder. After the gas is cooled by the internal coils and cold walls, the precipitated solution absorbent returns to the primary quench washing tank 29 via the reflux tank 31. Both the primary quench washing tank 29 and the secondary washing and cooling tank 30 are equipped with a pyrolysis cycle refrigeration system 32, which dehydrates, removes dust, and evaporates the collected solution to obtain full-fraction coal tar. The internal temperature of the high-temperature pre-processor 28 is 500-800℃, the temperature of the primary quench washing tank 29 is 100-500℃, the temperature of the secondary washing and cooling tank 30 is 30-250℃, the temperature of the pyrolysis cycle refrigeration system 32 is 0-30℃, the heating temperature is >400-450℃, the operating pressure is 0.001-10.0MPa, and the pyrolysis gas volume is 10-100Nm³. 3 / h.

[0061] like Figure 3 As shown, the gasification sampling device 4 includes a primary gas cooler 34, a depth filter 35, a secondary gas cooler 36, a gas-liquid separator 37, and a heating system. The gasified gas first enters the primary gas cooler 34 for preliminary cooling, raising its temperature above the water vapor dew point temperature. The cooled gas then enters the parallel-connected depth filter 35, which consists of an upper sintered filter element zone, a middle backfluidization zone, and a lower powder collection zone, removing all dust from the gasified gas. The dust-free gas is further cooled in the secondary gas cooler 36, and the condensed water vapor is separated and collected in the gas-liquid separator 37. The purified gas is then metered by a gasified gas flow meter 39 for online gas component analysis. The depth filter 35 can be switched online to achieve continuous operation, enabling the collection of fly ash in the crude syngas and online gas analysis. Backflushing air is used to purge and collect powder from the filter element surface. The filter element accuracy is 1-30 μm, suitable for syngas with dust concentrations of 20-300 g / Nm³. 3 The backflush gas medium is self-produced syngas, and the backflush gas pressure is 2-5 times the system pressure. The temperature of the primary gas cooler 34 is 500-1100℃, the temperature of the depth filter 35 is 200-500℃, the temperature of the secondary gas cooler 36 is 50-200℃, the operating pressure is 0.001-10.0MPa, and the syngas flow rate is 10-80Nm³. 3 / h.

[0062] like Figure 4As shown, the fluidized pressurized feeder 40 includes a cylinder 41. The upper part of the cylinder 41 is provided with a sleeve 42 and a flute 43, while the lower part is provided with a sintered wire mesh 44, a solid distribution plate 45, and a gas distribution pipe 46. A vibrator 47 is connected to the outside of the cylinder 41. Under the action of fluidizing gas, qualified coal powder enters the sleeve 42. Under the purging and fluidizing action of the flute 43 and the gas distribution plate 46, the coal powder is discharged from the bottom of the sleeve 42 into the lower cylinder. Under the dual action of gas fluidization of the solid distribution plate 45 and vibration of the vibrator 47, the coal powder is discharged from the upper part of the cylinder 41, achieving feeding of the pyrolyzer 1 under a high pressure of 10.0 MPa at a feeding rate of 10-10000 kg / h.

[0063] A method for using a coal fractionation and utilization device based on a coupling process includes the following steps:

[0064] Step 1: Pyrolysis and Gasification

[0065] 1. Using solid particles as the heat carrier, a high-rate circulation return process with a circulation ratio of 50-300 is carried out between the pyrolyzer 1, the combustion gasifier 2, and the multi-stage gas-solid separator 5. Under the condition that one or more combinations of quartz sand, ash, semi-coke, carbon black, and other carbon-containing solid particles are used as the heat carrier, the system gradually heats up to 400-800℃ at a heating rate of 5-30℃ / h.

[0066] 2. Powdered coal from the pressurized fluidized feeder 40 enters the pyrolyzer 1, where it is thoroughly mixed and fluidized with high-temperature solid particles, undergoing a rapid pyrolysis reaction to produce high-temperature oil gas and semi-coke. 50-70% of the semi-coke and heat carrier solid particles in the pyrolyzer 1 are returned to the combustion gasifier 2 through the internal solid circulation return channel. The remaining high-temperature oil gas, containing 30-50% semi-coke and heat carrier solid particles, enters the multi-stage gas-solid separator 6, where the semi-coke and heat carrier solid particles are captured and returned to the combustion gasifier 2. When the material level in the reaction system is high, some of the high-temperature ash produced by the combustion gasifier 2 and the multi-stage gas-solid separator 6 enters the ash cooler 7, where it exchanges heat with wastewater from the oil-water enhanced separator 14, producing medium-pressure steam at a pressure of 2.5-6 MPa and a temperature of 350-450℃, which then enters the steam heater 5. The ash is then discharged from the system.

[0067] Step 2, purification and recycling

[0068] 1. High-temperature oil and gas are sequentially cooled and washed in a primary scrubbing cooler 8 and a secondary scrubbing cooler 10 to obtain heavy distillate oil (>350℃) and light distillate oil (<350℃) as circulating cooling media, respectively. The liquid product collected in the primary scrubbing cooler 8 enters a liquid-solid enhanced separator 9, where it is separated to obtain heavy distillate oil and solid residue; the liquid product collected in the secondary scrubbing cooler 10 enters a primary fractionator 11.

[0069] 2. After being washed by the secondary scrubber 10, the oil and gas sequentially enter the primary gas-liquid condenser 12, the cryogenic purifier 13 and the oil-water enhanced separator 14 to recover light oil, pyrolysis water and syngas in stages. The light oil produced enters the product fractionator 26. The pyrolysis water produced is mixed with the solid residue produced by the high-pressure separator 25 and the liquid-solid enhanced separator 9. Under the atomization of steam, it enters the combustion gasifier 2 through the atomizing feeder 27.

[0070] Step 3, Oil Processing

[0071] The solid residue produced by the liquid-solid separator 9 is partially fed into the combustion gasifier 2 via the atomizing feeder 27 along with the solid residue from the high-pressure separator 25, serving as a supplementary carbon source for regasification. The remaining portion enters the oil-coal slurry tank 22, and then sequentially enters the primary enhanced hydrogenation reactor 23, the high-pressure separator 25, and the secondary enhanced hydrogenation reactor 24. The resulting tail oil is fed into the oil-coal slurry tank 22 as a supplementary feedstock for heavy oil.

[0072] 2. Hydrogen from the booster unit 21 enters the primary enhanced hydrogenation reactor 23 and the secondary enhanced hydrogenation reactor 24 as hydrogen supply gas for reaction. The hydrogenated oil from the secondary enhanced hydrogenation reactor 24 and the light oil produced by the oil-water enhanced separator 14 enter the product fractionator 26 for further fractionation to obtain coal-based oil products such as naphtha, naphthenic oil, and special fuel oil.

Claims

1. A coal quality-based utilization device based on a coupling process, characterized by, It includes a pyrolysis and gasification unit, a purification and recovery unit, a separation and utilization unit, and an oil processing unit; The pyrolysis gasification unit completes the rapid pressurization and hydrogenation of pulverized coal into pyrolysis oil, semi-coke and syngas in stages. The semi-coke completes the efficient gasification reaction through the built-in circulation and external circulation return channels. The purification and recovery unit achieves the collection of pyrolysis oil and solid residues and the graded recycling of heavy oil and light oil through multi-stage purification, dust removal and washing recovery of high-temperature oil and gas. The separation and utilization unit achieves graded recovery of light oil and pyrolysis water, as well as separation and recycling of syngas through efficient separation and recovery of gas and liquid phases. The oil processing unit utilizes heavy components of coal tar and ash residue as feedstock for enhanced hydrogenation to produce coal-based specialty fuel oil, thereby achieving the recycling of solid residue and semi-coke. The purification and recovery unit includes a pyrolyzer (1) and a circulating gas preheater (19) connected to the inlet of a multi-stage gas-solid separator (6). The upper outlet of the multi-stage gas-solid separator (6) is connected to the input end of the primary washing cooler (8), and the bottom outlet of the multi-stage gas-solid separator (6) is connected to the bottom inlet of the combustion gasifier (2) to form a solid external circulation. The inlet of the ash cooler (7) is connected to the output ends of the combustion gasifier (2), the multi-stage gas-solid separator (6), and the oil-water enhanced separator (14). The gas phase outlet of the ash cooler (7) is connected to the gas phase inlet of the steam heater (5), and the solid phase outlet of the ash cooler (7) is connected to the solid phase inlet of the oil-coal slurry tank (22). The inlet of the liquid-solid enhanced separator (9) is connected to the output end of the primary washing cooler (8), and the liquid-solid enhanced separator... The liquid phase outlet of (9) is connected to the upper part of the primary washing cooler (8) and the liquid phase inlet of the oil-coal slurry tank (22), respectively. The solid phase outlet of the liquid-solid enhanced separator (9) is connected to the atomizing feeder (27) and the solid phase inlet of the oil-coal slurry tank (22), respectively. The top outlet of the primary washing cooler (8) is connected to the inlet of the secondary washing cooler (10), and the outlet of the secondary washing cooler (10) is connected to the input end of the primary fractionator (11) and the primary gas-liquid condenser (12), respectively. The upper outlet of the primary fractionator (11) is connected to the input end of the secondary enhanced hydrogenation reactor (24) and the phenol extraction device (50), and the lower outlet of the phenol extraction device (50) is connected to the input end of the secondary enhanced hydrogenation reactor (24). The lower output end of the primary fractionator (11) is connected to the input end of the oil-coal slurry tank (22).

2. The coal quality-based utilization device based on coupling process according to claim 1, characterized in that, The pyrolysis gasification unit includes a pressurized fluidized feeder (40), a combustion gasifier (2), and a multi-stage gas-solid separator (6) connected to the pyrolyzer (1). The upper part of the pyrolyzer (1) is connected to the lower inlet of the combustion gasifier (2) to form an upper solid circulation, and the bottom of the pyrolyzer (1) is connected to the upper inlet of the combustion gasifier (2) to form a lower solid circulation. The input end of the combustion gasifier (2) is connected to the output end of the multi-stage gas-solid separator (6) and the atomizing feeder (27). The output end of the combustion gasifier (2) is connected to the input end of the ash cooler (7). The inlet of the atomizing feeder (27) is connected to the output of the steam heater (5), the liquid-solid enhanced separator (9), and the oil-water enhanced separator (14), respectively.

3. A coal fractionation and utilization device based on a coupling process according to claim 2, characterized in that, The output end of the pyrolyzer (1) is connected to the input end of the pyrolysis sampling device (3). The pyrolysis sampling device (3) includes a high temperature preprocessor (28). The output end of the high temperature preprocessor (28) is connected to the input end of the first-stage quench washing tank (29). The output end of the first-stage quench washing tank (29) is connected to the input end of the second-stage washing and cooling tank (30). The output end of the second-stage washing and cooling tank (30) is connected to the input ends of the pyrolysis gas flow meter (33) and the reflux tank (31) respectively. The output end of the reflux tank (31) is connected to the input end of the first-stage quench washing tank (29). Both the primary quench washing tank (29) and the secondary washing cooling tank (30) are connected to a pyrolysis cycle refrigeration system (32).

4. A coal fractionation and utilization device based on a coupling process according to claim 2, characterized in that, The output end of the combustion gasifier (2) is connected to the input end of the gasification sampling device (4). The gasification sampling device (4) includes a primary gas cooler (34). The output end of the primary gas cooler (34) is connected to the input end of the depth filter (35). The output end of the depth filter (35) is connected to the input end of the secondary gas cooler (36). The output end of the secondary gas cooler (36) is connected to the input end of the gas-liquid separator (37). The primary gas cooler (34) and the secondary gas cooler (36) are both connected to a vaporization cycle refrigeration system (38); the gas-liquid separator (37) is connected to a vaporization gas flow meter (39). The multi-stage gas-solid separator (6) includes a primary gas-solid separator and a secondary gas-solid separator, wherein the secondary gas-solid separator is composed of a large-pore support substrate layer and a small-pore membrane filter layer. The primary washing cooler (8) includes an upper porous settling hood, a middle multi-stage nozzle, filter and baffle, and a bottom settling cone and baffle.

5. A coal fractionation and utilization device based on a coupling process according to claim 2, characterized in that, The pressurized fluidized feeder (40) includes a cylinder (41), inside which are provided a sleeve (42), a flute (43), a sintered wire mesh (44), a solid distribution plate (45), and a gas distribution pipe (46). A vibrator (47) is connected to the outside of the cylinder (41) to enable feeding of the pyrolyzer (1) under a high pressure of 10.0 MPa at a feed rate of 10-10000 kg / h. The flute (43) is fixedly connected to the top of the sleeve (42) by a flange and is centrally symmetrically distributed into the sleeve (42), with a penetration length accounting for 1 / 2-2 / 3 of the total length of the sleeve (42). The upper part of the sleeve (42) is connected to the top of the cylinder (41) by a flange and penetrates into the cylinder (41), with a penetration length accounting for 1 / 3-2 / 3 of the total length of the sleeve. The lower part of the sleeve (42) is connected to the upper part of the solid distribution plate (45). An annular filtration channel is provided to allow 10-5cm coal powder from the annular gap between the sleeve (42) and the flute (43) to enter the cylinder (41). The top of the solid distribution plate (45) is provided with a sintered wire mesh (44) connected to the gas distribution pipe (46), and the bottom is provided with a gas distribution pipe (46) connected to the fluidization port. The angle of the upper part of the solid distribution plate (45) is 10-70°, and the filtration accuracy of the sintered wire mesh (44) is 0.1-100μm.

6. A coal fractionation and utilization device based on a coupling process according to claim 1, characterized in that, The separation and utilization unit includes a cryogenic purifier (13) connected to the upper outlet of the primary gas-liquid condenser (12). The lower outlets of both the primary gas-liquid condenser (12) and the cryogenic purifier (13) are connected to the inlet of the oil-water enhanced separator (14). The upper outlet of the cryogenic purifier (13) is connected to the inlet of the syngas storage tank (15). The output end of the syngas storage tank (15) is connected to the input end of a multi-stage adsorption tank (16). The output end of the multi-stage adsorption tank (16) is divided into two paths, one of which is connected to the circulating gas separator (17). The output of the circulating gas separator (17) is connected to the input of the carbon dioxide booster (18), and the output of the carbon dioxide booster (18) is connected to the input of the circulating gas preheater (19). The output of the hydrogen extraction device (20) is connected to the input of the hydrogen booster (21), and the output of the hydrogen booster (21) is divided into two paths, which are connected to the inputs of the primary enhanced hydrogenation reactor (23) and the secondary enhanced hydrogenation reactor (24), respectively.

7. A coal fractionation and utilization device based on a coupling process according to claim 1, characterized in that, The oil processing unit includes a primary enhanced hydrogenation reactor (23) connected to the outlet of an oil-coal slurry tank (22). The outlet of the primary enhanced hydrogenation reactor (23) is connected to the inlet of a high-pressure separator (25). The output of the high-pressure separator (25) is connected to the input of an atomizing feeder (27). The inlet of the secondary enhanced hydrogenation reactor (24) is connected to the outlet of the high-pressure separator (25) and the phenol extraction unit (50). The outlets of the secondary enhanced hydrogenation reactor (24) and the oil-water enhanced separator (14) are both connected to the inlet of a product fractionator (26). The primary enhanced hydrogenation reactor (23) and the secondary enhanced hydrogenation reactor (24) each include 1-3 reactors in series.

8. A coal fractionation and utilization device based on a coupling process according to claim 7, characterized in that, The output ends of the atomizing feeder (27) and the high-pressure separator (25) are connected.

9. A method of using a coal fractionation and utilization device based on a coupling process as described in any one of claims 1-8, characterized in that, Includes the following steps; Step 1: Pyrolysis and Gasification The solid particulate heat carrier is circulated at a high rate of 50-300 between the pyrolyzer (1), the combustion gasifier (2), and the multi-stage gas-solid separator (6), and the system gradually heats up to 400-800℃. After the pulverized coal from the pressurized fluidized feeder (40) enters the pyrolyzer (1), it is fully mixed and fluidized with the high-temperature solid particles and undergoes a rapid pyrolysis reaction to produce high-temperature oil gas and semi-coke. The semi-coke and heat carrier solid particles with a mass of 50-70% are returned to the combustion gasifier (2) through the internal solid circulation return channel. The remaining high-temperature oil gas with a mass of 30-50% semi-coke and heat carrier solid particles enters the multi-stage gas-solid separator. The semi-coke and heat carrier solid particles are captured and returned to the combustion gasifier (2) in the separator (6); when the material level of the reaction system is high, it is judged by the pressure difference P=ρgh in the reaction system. When the pressure difference value of a certain section of the system feedback is >25-30KPa, it indicates that the material level in the reaction system is high, which is not conducive to fluidization circulation and requires online ash discharge. Some of the high-temperature ash generated by the combustion gasifier (2) and the multi-stage gas-solid separator (6) enters the ash cooler (7) and exchanges heat with the wastewater from the oil-water enhanced separator (14). After producing medium-pressure steam with a pressure of 2.5-6MPa and a temperature of 350-450℃, it enters the steam heater (5) and the ash is discharged from the system. Step 2, purification and recycling High-temperature oil and gas are cooled and washed in the primary washing cooler (8) and the secondary washing cooler (10) to obtain heavy distillate oil and light distillate oil as cooling media, respectively. The liquid product collected in the primary washing cooler (8) enters the liquid-solid enhanced separator (9) and is separated to obtain heavy distillate oil and solid residue. The liquid product collected in the secondary washing cooler (10) enters the primary fractionator (11). The oil and gas washed by the secondary washing cooler (10) enter the primary gas-liquid condenser (12), the cryogenic purifier (13) and the oil-water enhanced separator (14) in sequence to recover light oil, pyrolysis water and syngas in stages. The light oil produced enters the product fractionator (26). The pyrolysis water produced is mixed with the solid residue produced by the high-pressure separator (25) and the liquid-solid enhanced separator (9). Under the atomization of steam, it enters the combustion gasifier (2) through the atomizing feeder (27). Step 3, Oil Processing The solid residue produced by the liquid-solid separator (9) is partially fed into the combustion gasifier (2) via the atomizing feeder (27) along with the solid residue from the high-pressure separator (25) to serve as a supplementary carbon source for the combustion gasifier (2) for regasification reaction; the remaining portion enters the oil-coal slurry tank (22) and then sequentially enters the primary enhanced hydrogenation reactor (23), the high-pressure separator (25), and the secondary enhanced hydrogenation reactor (24). The resulting tail oil is fed into the oil-coal slurry tank (22) as a supplementary feedstock for heavy oil. The hydrogen from the booster (21) enters the primary enhanced hydrogenation reactor (23) and the secondary enhanced hydrogenation reactor (24) as hydrogen supply gas for reaction. The hydrogenated oil from the secondary enhanced hydrogenation reactor (24) and the light oil produced by the oil-water enhanced separator (14) enter the product fractionator (26) for further fractionation to obtain naphtha, naphthenic oil, and special fuel oil.

10. The method of using a coal fractionation and utilization device based on a coupling process according to claim 9, characterized in that, In step 1, the internal pressure of the pyrolyzer (1) and the combustion gasifier (2) is 0.001-10.0 MPa, and the pyrolysis temperature inside the pyrolyzer (1) is 400-800℃, and the gas velocity is 2-20 m / s. The gasification temperature inside the combustion gasifier (2) is 900-1400℃, the gas velocity is 0.1-2 m / s, and the solid circulation ratio is 10-300 times.

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