A zero-carbon emission new energy coupled coal fractionation conversion device and method

Abstract

This invention discloses a zero-carbon emission new energy coupled coal fractionation conversion device and method, including a circulating reaction unit, a gas-solid separation unit, a recovery and conversion unit, and a gas reuse unit. The circulating reaction unit rapidly converts pulverized coal into tar and semi-coke in stages, and the semi-coke is further converted into hydrogen-rich syngas in a gasifier-reburner. The gas-solid separation unit achieves efficient separation and recycling of dust in high-temperature oil and gas through a multi-stage gas-solid separation device. The recovery and conversion unit obtains full-fraction tar through efficient gas-liquid two-phase separation, and produces coal-based products through enhanced hydrogenation. The gas reuse unit uses carbon dioxide in the syngas as the system's transport gas, fluidizing gas, pressurizing gas, and backflushing gas, thereby realizing the recycling of carbon dioxide gas. This invention recycles carbon dioxide and carbon solid waste, and has the advantages of high energy conversion efficiency, high carbon conversion rate, high oil and gas yield, high effective gas content in syngas, zero carbon emissions, and environmental friendliness.

Description

Technical Field

[0001] This invention relates to the field of coal fractionation technology, specifically to a zero-carbon emission new energy coupled coal fractionation device and method. Background Technology

[0002] Currently, traditional coal resource utilization methods, primarily relying on direct combustion and simple conversion, only utilize the fuel properties of coal, resulting in the waste of valuable components within the coal molecule and environmental pollution. Coal fractionation, through low-energy and low-material consumption methods, efficiently converts coal into clean fuels such as oil and gas, as well as high-value-added chemical products, maximizing overall resource conversion efficiency and thereby improving the social and environmental benefits of the coal conversion process.

[0003] Most existing coal fractionation technologies are still in the industrial verification and upgrading stage, and have not yet achieved a true leap forward. They mainly face industry challenges such as long operating cycles, low carbon conversion rates, failure to meet environmental standards, weak competitiveness of coal-based chemicals, and incomplete industrial chain support, requiring further technological improvement and continuous optimization. Currently, through continuous optimization, upgrading, and coupling of advanced technologies, different coal fractionation technology routes, target products, and supporting technologies have been identified, resulting in various technology and product combination solutions. This is expected to explore new paths for industrial development aimed at reducing carbon dioxide emissions, strengthen efficient integration with new energy or new materials industries such as hydrogen energy and photovoltaics, break down industry barriers, construct a multi-product model for cross-industry coupling development, better adapt to market changes, leverage differentiated characteristics, and simultaneously achieve optimal material and energy consumption, thus building a green and efficient coal chemical technology development and industrial development system. CN114752418A provides a coal fractionation utilization system and process to achieve zero carbon emissions. After pyrolysis of coal, carbon dioxide is separated and extracted from the pyrolysis gas, and then reacted with pyrolysis semi-coke in a redox reaction to produce carbon monoxide. This process only reuses carbon dioxide as a gasifying agent, and the ambient pressure operating conditions are relatively mild. This results in insufficient depth of pyrolysis and reduction reactions under high pressure, leading to a low effective gas component in the syngas. Furthermore, some carbonaceous solids, such as particles, in the pyrolysis tar are not recycled, making it difficult to achieve zero-carbon emissions for coal-based fractional utilization. Summary of the Invention

[0004] In order to overcome the shortcomings of the prior art, the present invention aims to provide a zero-carbon emission new energy coupled coal fractionation conversion device and method, which has the characteristics of high energy conversion efficiency, high syngas content, low carbon emission intensity, low water consumption, flexible product scheme and environmentally friendly zero-carbon emission.

[0005] To achieve the above objectives, the technical solution adopted by the present invention is as follows:

[0006] A zero-carbon emission new energy coupled coal fractionation conversion device includes a new energy hydrogen production unit, a recycling reaction unit, a gas-solid separation unit, a recovery and conversion unit, and a gas reuse unit.

[0007] The new energy hydrogen production unit generates electricity using renewable energy sources, which is then transported to the water electrolysis hydrogen production device. The oxygen and hydrogen produced provide an active atmosphere for the fractional conversion and deep processing of coal.

[0008] The circulating reaction unit completes the rapid segmented conversion of pulverized coal into tar and semi-coke, and the semi-coke is further converted into hydrogen-rich syngas in the gasifier-reburner.

[0009] The gas-solid separation unit achieves efficient separation and recycling of dust in high-temperature oil and gas through a multi-stage gas-solid separation device.

[0010] The recovery and conversion unit obtains full-fraction tar through efficient separation of gas and liquid phases, and produces coal-based products such as special fuels and modified asphalt through enhanced hydrogenation reaction; the gas recycling unit uses carbon dioxide in syngas as the system's transport gas, fluidizing gas, pressurizing gas and backflush gas to realize the recycling of carbon dioxide gas.

[0011] The circulating reaction unit includes a hopper 9 and a pressurized lock hopper 10, a pressurized feed hopper 11, and a first feeder 12 connected thereto in sequence. The outlet of the first feeder 12 is connected to the lower inlet of the pyrolyzer 13, which is connected to the outlet of the hydrogen storage tank 6. The pyrolyzer 13 is connected in sequence to a primary gas-solid separation device 16, a coke powder collector 17, a return material controller 18, and a gasifier 14 to form a middle solid circulation. The lower part of the pyrolyzer 13 is connected to the gasifier 14 to form an internal solid circulation. The primary gas-solid separation device 16 is connected in sequence to a deep gas-solid separation device 19, a multi-stage pressure reducing ash discharge device 20, a fly ash buffer tank 21, and a fly ash collector. 22. The bottom of the reburner 15 and the gasifier 14 are connected to form an external solid circulation; the lower inlet of the gasifier 14 is connected to the outlet of the oxygen storage tank 5, the second feeder 29, and the carbon dioxide pressure regulator 45; the upper part of the reburner 15 is connected to the gasifier 14, the output end of the reburner 15 is connected to the input end of the primary gas-solid separation device 16, the input end of the reburner 15 is connected to the output end of the fly ash collector 22, the output end of the reburner 15 is connected to the input end of the second feeder 29, and the bottom outlet pipeline of the wastewater collection tank 35 goes partly to the reburner 15 as a cooling medium for high-temperature ash and slag, and partly to the multi-effect evaporator 36 as an evaporation medium.

[0012] The gas-solid separation unit includes a coke collector 17 and a deep gas-solid separation device 19 connected to the primary gas-solid separation device 16, an oil-gas enhanced separation device 24 connected to the deep gas-solid separation device 19, and a fly ash pressure relief tank 23 connected to the upper part of the multi-stage pressure reducing and ash discharge device 20. The outlet of the fly ash pressure relief tank 23 is connected to the fly ash buffer tank 21 and the inlet of the oil-gas enhanced separation device 24, respectively.

[0013] The recovery and conversion unit includes a heavy oil buffer tank 25 and a gas purification device 32 connected to the oil-gas enhanced separation device 24. The upper output end of the heavy oil buffer tank 25 is connected to the input end of the primary oil-gas cyclone device 30, and the bottom output end of the heavy oil buffer tank 25 is connected to the input end of the heavy oil collection tank 26. The output end of the heavy oil collection tank 26 is connected to the input end of the liquid-solid enhanced separator 27. The solid phase outlet of the liquid-solid enhanced separator 27 is connected to the solid phase inlet of the solid buffer tank 28. The solid phase outlet of the solid buffer tank 28 is connected to the solid phase inlet of the second feeder 29. The liquid phase outlet of the liquid-solid enhanced separator 27 is connected to the liquid phase inlet of the intermediate oil collection tank 31. The output end of the intermediate oil collection tank 31 is connected to the input end of the multiphase reaction feedstock tank 38. The outlet of the primary oil-gas cyclone device 30 is connected to the intermediate oil collection tank 31. The gas purification device 32 has an inlet; the upper outlet of the gas purification device 32 is connected to the inlet of the deep purification device 39. The bottom of the gas purification device 32 is connected in sequence to the oil-water buffer tank 33, the oil-water enhanced separator 34, the wastewater collection tank 35, and the light oil tank 49. The outlet of the wastewater collection tank 35 is connected to the inlet of the gas purification device 32 and the multi-effect evaporator 36. The outlet of the multi-effect evaporator 36 is connected to the inlet of the second feeder 29. The inlet of the multiphase reaction raw material tank 38 is connected to the outlet of the intermediate oil collection tank 31. The outlet of the multiphase reaction raw material tank 38 is connected to the inlet of the multiphase reactor 41. The bottom outlet of the multiphase reactor 41 is connected to the inlet of the second feeder 29. The inlet of the multiphase reactor 41 is also connected to the outlet of the hydrogen pressure controller 8, the first feeder 12, and the solid buffer tank 28.

[0014] The gas recycling unit includes a gas purification device 32, a gas shift separator 40, and a light oil tank 49 connected to a deep purification device 39. The outlet of the deep oil-gas cyclone device 37 is connected to the upper inlet of the oil-water enhanced separator 34. The outlet of the gas shift separator 40 is connected to the inlets of the Fischer-Tropsch reactor 42, the gas-fired power generation device 43, and the carbon dioxide buffer tank 44, respectively. The outlet of the carbon dioxide buffer tank 44 is connected to the inlet of the carbon dioxide pressure controller 45. The outlet of the carbon dioxide pressure controller 45 is connected to the inlets of the pressurized lock hopper 10, the pressurized feed hopper 11, the first feeder 12, the gasifier 14, the reburner 15, the return material controller 18, the deep gas-solid separation device 19, the multi-stage pressure reducing and ash removal device 20, the heavy oil buffer tank 25, the second feeder 29, and the oil-water buffer tank 33, respectively. The outlet of the oil-water buffer tank 33 is connected to the inlet of the deep oil-gas cyclone device 37.

[0015] The new energy hydrogen production unit includes a new energy power generation device 1 and a power distribution device 2 and an energy storage device 3 connected thereto in sequence. The output end of the power distribution device 2 is connected to the input end of the water electrolysis hydrogen production device 4. The outlet of the water electrolysis hydrogen production device 4 is connected to the inlet of the oxygen storage tank 5 and the hydrogen storage tank 6 respectively. The outlet of the hydrogen storage tank 6 is connected to the inlet of the hydrogen storage device 7, the hydrogen pressure regulator 8 and the pyrolyzer 13. The output end of the hydrogen pressure regulator 8 is connected to the input end of the multiphase reactor 41.

[0016] The outlet of the hydrogen storage tank 6 is connected to the inlet of the hydrogen storage device 7, which uses pressure hydrogen storage or liquid hydrogen storage.

[0017] The output of the deep gas-solid separation device 19 is connected to the input of the gas sampling device 46. The gas sampling device 46 consists of a high-temperature pre-processor, a primary quench washing tank, a secondary washing and cooling tank, a reflux tank, and a pyrolysis cycle refrigeration system, realizing the two-phase separation of oil and dust in the gas and online analysis of the purified gas. High-temperature dust-laden gas enters the high-temperature pre-processor, where small-particle dust is captured by a ceramic filter with a filter element precision of 1-20μm, suitable for gas dust concentrations ranging from 10-300g / Nm³. 3 The system uses self-produced syngas for pressurized backflushing, collecting powder from the filter element surface online. The high-temperature gas, now free of dust, sequentially enters a primary quench scrubber and a secondary scrubber / cooler containing a solution absorbent. The primary quench scrubber utilizes a quench-type heat exchange, while the secondary scrubber / cooler consists of an upper scrubbing section, a middle cooling section, and a bottom filter element inner cylinder. After the gas is cooled by internal coils and cold walls, the precipitated solution absorbent returns to the primary quench scrubber via a reflux tank. Both the primary quench scrubber and the secondary scrubber / cooler are equipped with a pyrolysis cycle refrigeration system, which dehydrates, removes dust, and performs rotary evaporation on the collected solution to obtain full-fraction coal tar. The high-temperature pre-processor operates at 500-800℃, the primary quench washing tank at 100-500℃, the secondary washing cooling tank at 30-250℃, the pyrolysis cycle refrigeration system at 0-30℃, the heating temperature at >400-450℃, the operating pressure at 0.001-25.0MPa, and the gas flow rate at 10-100Nm³. 3 / h.

[0018] The deep gas-solid separation device 19 has a side-inlet and top-outlet structure. Its interior consists of a large-pore support substrate layer and several small-pore membrane filter rods. The filter element has a pore size of 10-150μm and a porosity of 30-45%.

[0019] Both the primary oil-gas cyclone device 30 and the deep oil-gas cyclone device 37 are integrated multi-stage gas-liquid separators, or multi-stage gas-liquid separators composed of 1-5 single-stage gas-liquid separators connected in series.

[0020] The multiphase reactor 41 comprises 1-5 multiphase flow enhanced hydrogenation reactors connected in series.

[0021] A method for using a zero-carbon emission new energy coupled coal fractionation conversion device includes the following steps:

[0022] Step 1: Electrolysis to produce hydrogen;

[0023] 1.1 Part of the electrical energy generated by the new energy power generation device 1 is transmitted to the power dispatching device 2. Part of the electrical energy generated by the power dispatching device 2 is transmitted to the water electrolysis hydrogen production device 4 through grid connection, and part of the electrical energy is transmitted to the energy storage device 3 for storage and backup.

[0024] 1.2 The water electrolysis hydrogen production device 4 uses electricity to generate oxygen, which is stored in the oxygen storage tank 5 and sent to the gasifier 14 to participate in the gasification reaction. The generated hydrogen is stored in the hydrogen storage tank 6. A portion of the hydrogen is sent to the pyrolyzer 13 to participate in the pyrolysis reaction, and a portion of the hydrogen is sent to the hydrogen pressure controller 8 for pressurization and then enters the multiphase reactor 41 to participate in the enhanced hydrogenation reaction of oil products. The remaining portion of the hydrogen is sent to the hydrogen storage device 7 for storage and backup.

[0025] Step 2: Cyclic reaction;

[0026] Pulverized coal enters the pyrolyzer 13 from the first feeder 12 and is fully mixed with the solid heat carrier. The pyrolysis reaction occurs in the pyrolyzer 13, producing high-temperature oil and gas and semi-coke. Most of the semi-coke is returned to the gasifier 14 through the internal solid circulation return channel. The high-temperature oil and gas containing a small amount of semi-coke and solid particles enters the primary gas-solid separator 16. The semi-coke and solid particles are captured and returned to the gasifier 14 through the pulverized coke collector 17 and the return controller 18. The high-temperature oil and gas carrying fly ash enters the deep gas-solid separator 19. After the fly ash is captured, it passes through the multi-stage pressure reducing and ash discharge device 20, the fly ash buffer tank 21 and the fly ash collector 22 in sequence and is returned to the reburner 15.

[0027] Step 3: Purification and recycling;

[0028] 3.1 The high-temperature oil and gas separated by the deep gas-solid separator 19 enters the oil-gas enhanced separation device 24 for cooling and washing. The resulting oil and gas enters the gas purification device 32, and the resulting liquid enters the heavy oil buffer tank 25 to obtain heavy oil and medium oil respectively. The heavy oil enters the heavy oil collection tank 26 and the liquid-solid enhanced separator 27 in sequence, and the medium oil enters the primary oil-gas cyclone device 30.

[0029] 3.2 The solids separated by the liquid-solid enhanced separator 27 pass through the solid buffer tank 28 and the second feeder 29 in sequence and enter the gasifier 14 for recycling. The liquids separated by the liquid-solid enhanced separator 27 and the medium oils separated by the primary oil-gas cyclone device 30 enter the medium oil collection tank 31 in sequence.

[0030] 3.3 After the oil and gas are purified by the gas purification device 32, the generated gas enters the deep purification device 39, the generated liquid enters the oil-water buffer tank 33, the carried oil and gas enter the deep oil-gas cyclone device 37, and the liquid enters the oil-water enhanced separator 34 to separate light oil and wastewater. The light oil enters the light oil tank 49, and the wastewater enters the wastewater collection tank 35 and the multi-effect evaporator 36 in sequence to generate steam. The steam enters the second feeder 29 and is used as atomizing gas to enter the gasifier 14 for recycling. Part of the liquid in the wastewater collection tank 35 is recycled back into the gas purification device 32.

[0031] Step 4: Oil Conversion;

[0032] 4.1 The medium-grade oil collected in the medium-grade oil collection tank 31 and the light oil separated by the oil-water enhanced separator 34 and the deep purification device 39 enter the multiphase reaction feedstock tank 38 and the multiphase reactor 41 in sequence. The hydrogen in the hydrogen pressure controller 8 enters the multiphase reactor 41 as the hydrogen supply gas. The medium-grade oil from the medium-grade oil collection tank 31 enters the multiphase reaction feedstock tank 38 and the multiphase reactor 41 in sequence, and reacts with the oil-containing solids from the solid buffer tank 28 and the coal powder from the first feeder 12 to produce special fuel oil, modified asphalt and other coal-based products.

[0033] 4.2 The residue produced by the multiphase reactor 41 is sequentially fed into the second feeder 29 and the gasifier 14, and is recycled as a supplementary carbon source for the gasification reaction.

[0034] Step 5: Gas reuse;

[0035] The gas purified by the deep purification device 39 enters the gas separation and conversion device 40. The separated gas containing carbon monoxide and hydrogen enters the Fischer-Tropsch reactor 42 for the production of clean oil products, or enters the gas-fired power generation device 43 for power generation or heat generation. The separated gas containing carbon dioxide enters the carbon dioxide buffer tank 44 and the carbon dioxide pressure controller 45 in sequence. Among them, a part is used as pressurizing gas and enters the pressurized lock hopper 10, pressurized feed hopper 11, multi-stage pressure reducing ash discharge device 20, heavy oil buffer tank 25 and oil-water buffer tank 33 respectively; a part is used as solid medium conveying gas and enters the first feeder 12, return material controller 18 and second feeder 29 to provide reaction atmosphere; another part enters the gasifier 14 as a gasifying agent to participate in the gasification reaction; the remaining part enters the deep gas-solid separation device 19 as backflushing gas.

[0036] The beneficial effects of this invention are:

[0037] First, this invention utilizes a highly efficient coal fractionation process to obtain high-quality, high-yield tar and syngas, achieving deep conversion and quality improvement of the products. The tar is then coupled with a multiphase enhanced hydrogenation process to produce coal-based products such as special fuels and modified asphalt. The syngas is sent to a gas-fired power plant for ultra-clean power generation, or produced as clean oil through a Fischer-Tropsch reaction. This constructs a new coal-electricity-oil cogeneration model integrating new energy, coal fractionation, green power generation, clean oil, and special fuels, extending the coal fractionation utilization industrial chain, increasing product added value, and reducing pollutant emissions. Second, this production process does not produce semi-coke, sludge, or other residues, achieving deep resource utilization of high-carbon solid waste. In addition to the semi-coke participating in gasification and combustion reactions, the residues generated by the enhanced hydrogenation reaction are returned to the gasifier, supplementing the insufficient carbon source in the gasification reaction. The generated syngas provides reaction heat and an active atmosphere for the pyrolysis reaction, solving the problems of low carbon conversion rate and low effective gas composition in fluidized bed reaction systems. The invention addresses industrial challenges by improving gasification indicators such as carbon conversion rate, cold gas efficiency, and effective gas components in syngas. Furthermore, the process efficiently separates and adaptively regulates carbon dioxide in syngas, using it as transport gas, fluidizing gas, pressurizing gas, and backflushing gas, thus achieving carbon dioxide recycling. This reduces carbon source input in the pyrolysis-gasification reaction while providing an active atmosphere to enhance reaction depth, increase the effective gas content of syngas and oil quality, significantly reduce material consumption, energy consumption, and carbon emissions, and significantly improve overall energy conversion efficiency, achieving zero-carbon emissions in coal fractionation conversion. Finally, the product options of this invention are flexible and versatile. While obtaining high-yield, high-quality tar and syngas, it can also produce coal-based products, clean oils, or be used for ultra-clean power generation, further improving coal conversion rate and clean oil yield, extending the industrial chain of coal fractionation utilization, and enhancing the overall technical and economic efficiency of the process. It is a green, efficient, and economical zero-carbon emission coal fractionation conversion process.

[0038] This invention utilizes renewable energy sources for green power generation and energy storage, achieving efficient utilization of renewable energy. Hydrogen is produced by electrolyzing water using green electricity. Part of the generated hydrogen provides a hydrogen-rich atmosphere and enhanced hydrogenation medium for the fractional conversion of pulverized coal and the deep processing of coal tar, while the other part is used as a hydrogen storage material. The by-product oxygen is used as a gasifying agent for the oxygen enrichment reaction of pulverized coal. This process has the characteristics of wide availability, recyclability, diversified uses, good economic efficiency, low environmental pollution, and high product utilization rate.

[0039] The fluidized bed pyrolyzer-gasifier-reburner integrated circulating fluidized reaction system developed in this invention rapidly converts pulverized coal into tar, semi-coke, and syngas in stages. The semi-coke is deeply converted into hydrogen-rich syngas within the gasifier-reburner. By utilizing internal, central, and external solid circulation return channels, efficient separation and high-rate return of solid particles with different properties are achieved. This circulating fluidized reaction system features high oil and gas yield, high carbon conversion rate, high cold gas efficiency, and high calorific value of syngas components. Attached Figure Description

[0040] Figure 1 : A schematic diagram of the overall process of this invention.

[0041] In the diagram: 1-New energy power generation device; 2-Power dispatching device; 3-Energy storage device; 4-Electrolysis of water to produce hydrogen device; 5-Oxygen storage tank; 6-Hydrogen storage tank; 7-Hydrogen storage device; 8-Hydrogen pressure controller; 9-Hopper; 10-Pressurized lock hopper; 11-Pressurized feed hopper; 12-First feeder; 13-Pyrolysis unit; 14-Gasifier; 15-Reburner; 16-Primary gas-solid separation unit; 17-Powdered coke collector; 18-Return material controller; 19-Deep gas-solid separation unit; 20-Multi-stage pressure reducing ash discharge unit; 21-Fly ash buffer tank; 22-Fly ash collector; 23-Fly ash pressure relief tank; 24-Enhanced oil-gas separation unit; 25-Heavy oil buffer tank; 26-Heavy oil collection tank; 27-Liquid-Solid Enhanced Separator; 28-Solid Buffer Tank; 29-Second Feeder; 30-Primary Oil-Gas Cyclone Device; 31-Middle Oil Collection Tank; 32-Gas Purification Device; 33-Oil-Water Buffer Tank; 34-Oil-Water Enhanced Separator; 35-Wastewater Collection Tank; 36-Multi-Effect Evaporator; 37-Deep Oil-Gas Cyclone Device; 38-Multiphase Reactor Feed Tank; 39-Deep Purification Device; 40-Gas Shift Separator; 41-Multiphase Reactor; 42-Fischer-Tropsch Reactor; 43-Gas-fired Power Generation Unit; 44-Carbon Dioxide Buffer Tank; 45-Carbon Dioxide Pressure Controller; 46-Gas Sampling Device; 47-Vacuum Gas Storage Tank; 48-Vacuum Gas Pressure Controller; 49-Light Oil Tank. Detailed Implementation

[0042] The present invention will be further described in detail below with reference to the embodiments.

[0043] like Figure 1As shown, a zero-carbon emission new energy coupled coal fractionation conversion device includes a new energy hydrogen production unit, a circulating reaction unit, a gas-solid separation unit, a recovery and conversion unit, and a gas reuse unit. The new energy hydrogen production unit generates electricity using renewable energy, which is then transported to an electrolytic water hydrogen production unit. The generated oxygen and hydrogen provide an active atmosphere for the fractionation and deep processing of coal. The circulating reaction unit rapidly converts pulverized coal into tar and semi-coke in stages. The semi-coke is then deeply converted into hydrogen-rich syngas in a gasifier-reburner. The gas-solid separation unit uses a multi-stage gas-solid separation device to efficiently separate and recycle dust from high-temperature oil and gas. The recovery and conversion unit obtains full-fraction tar through efficient gas-liquid two-phase separation, and produces coal-based products such as special fuels and modified asphalt through enhanced hydrogenation reactions. The gas reuse unit uses carbon dioxide from the syngas as the system's transport gas, fluidizing gas, pressurizing gas, and backflushing gas, achieving the recycling of carbon dioxide gas.

[0044] The new energy hydrogen production unit includes a new energy power generation device 1 and a power distribution device 2 connected thereto. The power distribution device 2 is connected to the energy storage device 3 and the water electrolysis hydrogen production device 4. The outlet of the water electrolysis hydrogen production device 4 is connected to the oxygen storage tank 5 and the hydrogen storage tank 6. The outlet of the oxygen storage tank 5 is connected to the lower inlet of the gasifier 14. The outlet of the hydrogen storage tank 6 is connected to the hydrogen storage device 7, the pyrolyzer 13 and the hydrogen pressure controller 8. The hydrogen storage device 7 uses high-pressure hydrogen storage or liquid hydrogen storage. When the load of the water electrolysis hydrogen production device 4 is reduced or it is shut down, the hydrogen storage device 7 provides a continuous and stable supply of hydrogen to the downstream recovery and conversion unit.

[0045] The circulating reaction unit includes a hopper 9 and a pressure lock hopper 10 connected thereto. The pressure lock hopper 10 is connected to a pressure feed hopper 11, which is connected to a first feeder 12. The first feeder 12 is connected to the lower inlet of the pyrolyzer 13, which is also connected to a hydrogen storage tank 6. The upper outlet of the pyrolyzer 13 is connected to a primary gas-solid separation device 16, which is connected to a coke powder collector 17. The coke powder collector 17 is connected to a return material controller 18, which is connected to the lower part of the gasifier 14, thus forming a middle solid circulation. The bottom outlet of the pyrolyzer 13... An internal solids circulation is formed by connecting the gasifier 14 to the gasifier 14. The primary gas-solid separation device 16 is connected to a deep gas-solid separation device 19, which is connected to a multi-stage pressure reducing and ash discharge device 20. The multi-stage pressure reducing and ash discharge device 20 is connected to a fly ash buffer tank 21, which is connected to a fly ash collector 22. The fly ash collector 22 is connected to the lower part of the gasifier 14, thus forming an external solids circulation. A reburner 15 is connected to the bottom of the gasifier 14. The upper part of the reburner 15 is connected to the primary gas-solid separation device 16, and the lower part of the reburner 15 is connected to the fly ash collector 22 and the wastewater collection tank 35.

[0046] The gas-solid separation unit includes a deep gas-solid separation device 19 and a coke powder collector 17 connected to the primary gas-solid separation device 16. The coke powder collector 17 is connected to the upper part of the return material controller 18, and the upper part of the return material controller 18 is also connected to the gasifier 14. The deep gas-solid separation device 19 is also connected to the multi-stage pressure reducing and ash discharge device 20, the oil-gas enhanced separation device 24, and the gas sampling device 46. The upper part of the multi-stage pressure reducing and ash discharge device 20 is connected to the fly ash pressure relief tank 23, and the outlet of the fly ash pressure relief tank 23 is connected to the fly ash buffer tank 21 and the oil-gas enhanced separation device 24.

[0047] The recovery and conversion unit includes a heavy oil buffer tank 25 and a gas purification device 32 connected to the oil-gas enhanced separation device 24. The upper part of the heavy oil buffer tank 25 is connected to a primary oil-gas cyclone device 30, and the bottom of the heavy oil buffer tank 25 is connected to a heavy oil collection tank 26. The heavy oil collection tank 26 is connected to a liquid-solid enhanced separator 27, and the solid phase outlet of the liquid-solid enhanced separator 27 is connected to a solid buffer tank 28. The solid buffer tank 28 is connected to a second feeder 29, and the liquid phase outlet of the liquid-solid enhanced separator 27 is connected to a mid-oil collection tank 31. The mid-oil collection tank 31 is connected to the bottom outlet of the primary oil-gas cyclone device 30. The upper outlet of the gas purification device 32 is connected to the inlet of a deep purification device 39, the middle part of the gas purification device 32 is connected to a wastewater collection tank 35, and the bottom of the gas purification device 32 is connected to an oil-water buffer. The outlets of the flushing tank 33 and the oil-water buffer tank 33 are respectively connected to an oil-water enhanced separator 34 and a deep oil-gas cyclone device 37. The bottom of the deep oil-gas cyclone device 37 is connected to the oil-water enhanced separator 34. The oil-water enhanced separator 34 is connected to the wastewater collection tank 35 and the light oil tank 49. The outlet of the wastewater collection tank 35 is connected to the gas purification device 32 and the multi-effect evaporator 36. The multi-effect evaporator 36 is connected to the second feeder 29. The second feeder 29 is connected to the lower inlet of the gasifier 14. The intermediate oil collection tank 31 is connected to the inlet of the multiphase reaction raw material tank 38. The outlet of the multiphase reaction raw material tank 38 is connected to the multiphase reactor 41. The bottom outlet of the multiphase reactor 41 is connected to the second feeder 29. The inlet of the multiphase reactor 41 is connected to the first feeder 12 and the solid buffer tank 28.

[0048] The gas recycling unit includes a gas purification device 32, a gas shift separation device 40, and a light oil tank 49, all connected to a deep purification device 39. The outlet of the gas shift separation device 40 is connected to a Fischer-Tropsch reactor 42, a gas-fired power generation device 43, and a carbon dioxide buffer tank 44, respectively. The inlet of the carbon dioxide pressure controller 45 is connected to the carbon dioxide buffer tank 44, and the outlet of the carbon dioxide pressure controller 45 is connected to a pressure lock hopper 10, a pressure feed hopper 11, a first feeder 12, a gasifier 14, a reburner 15, a return material controller 18, a deep gas-solid separation device 19, a multi-stage pressure reducing and ash removal device 20, a heavy oil buffer tank 25, a second feeder 29, and an oil-water buffer tank 33, respectively.

[0049] Preferably, the new energy power generation device 1 includes, but is not limited to, one or more combinations of photovoltaic power generation devices, wind power generation devices, hydropower generation devices, biomass power generation devices, waste incineration power generation devices, geothermal power generation devices, or devices that have abandoned water, wind, or solar power.

[0050] Preferably, the energy storage device 3 includes, but is not limited to, one or more combinations of lithium-ion battery energy storage, sodium-ion battery energy storage, lead-acid battery energy storage, graphene lithium battery energy storage, lithium-sulfur battery energy storage, aluminum-air battery energy storage, or molten salt thermal energy storage.

[0051] Preferably, the water electrolysis hydrogen production device 4 includes an electrolysis chamber, a gas-liquid processor, a rectifier, a water pump, an alkali tank, a water tank, and a control cabinet, wherein: the number of electrolysis chambers is 1-5, and hydrogen is produced by electrolyzing mine water, and the cathode and anode materials are metal alloys and metal oxides, including but not limited to porous Raney nickel, nickel-copper alloy, nickel-molybdenum alloy, and nickel-iridium alloy.

[0052] Preferably, the first feeder 12 includes a pressurized rotary feeder and a pressurized fluidized feeder. The pressurized rotary feeder includes a sealed rotating shaft, a motor, a spiral cylinder, a screw, a helix, a coupling, a frequency converter, a dynamic shaft seal, a shaft cooler, a feeder, a balancing pipeline, a loosening pipeline, and a conveying pipeline. The motor is located at the top of the spiral cylinder, with a motor speed of 10-90 r / min. The motor drives the rotating shaft to rotate, and the rotating shaft is connected to the screw via a coupling, which is used to fix the rotation angle of the screw. One end of the screw is fixed by the sealed rotating shaft, and the other end is connected to the helix, which is located at the bottom of the screw. The motor drives the sealed rotating shaft, thereby driving the screw to rotate, and the coal powder is fed to the feeder through the helix. The feeder is connected to the spiral cylinder via a flange. The spiral cylinder is externally connected to a shaft cooler, and a frequency converter is provided on the outer wall of the spiral cylinder. The gas inlet of the feeder is cylindrical, and the outlet is conical. The conveying pipeline enters tangentially to the bottom of the feeder. A balancing pipeline is installed at the top inlet of the spiral cylinder and the feeder inlet. The outer wall of the spiral cylinder has 3-6 staggered loose pipelines. A dynamic shaft seal is installed at the top of the pressurized rotary feeder to ensure continuous and stable feeding of pulverized coal under pressure.

[0053] The pressurized fluidized feeder includes an inner cylinder, an outer cylinder, downcomers, looseners, a gas distributor, a metal sintering unit, a drain, and loosening lines, conveying lines, and venting lines. The inner cylinder is connected to the top of the outer cylinder by flanges, and the inner cylinder's depth accounts for 1 / 2 to 2 / 3 of the total length of the outer cylinder. The downcomers are centrally symmetrically distributed and extend into the inner cylinder, connecting to the top of the inner cylinder by flanges. The outer wall surface of the downcomers has several 1-10 μm air ports. The lower part of the inner cylinder is sequentially connected to the metal sintering unit and the gas distributor. The looseners are staggered on the lower outer wall of the outer cylinder. The upper part of the outer cylinder is connected to the loosening lines, conveying lines, and venting lines, and the bottom is connected to the drain. Preferably, the coal powder feeding rate of the first feeder 12 is 10-15000 kg / h, achieving stable feeding under pressure of 0.001-25.0 MPa. The raw coal is required to have a particle size of 10-500 μm, a water content of <20%, a volatile matter content of 10-40%, and an ash content of >20%, and is suitable for coal types with an ash melting point of 1400℃.

[0054] Preferably, the pyrolyzer 13, gasifier 14, and reburner 15 are connected by an internal solid recycling return channel, a central solid recycling return channel, and an external solid recycling return channel to form a circulating reaction system. The circulating solid particles include, but are not limited to, one or more combinations of quartz sand, coal powder, ash, semi-coke, petroleum coke, waste tire powder, waste catalyst, carbon black, and other carbon-containing materials. The particle size of the solid particles is 10-300 μm. The reaction temperature and bed material are controlled by adding or discharging solid particles online. The heat source for heating the pyrolyzer 13, gasifier 14, and reburner 15 is provided by a combustion heating furnace, whose fuel is one or more combinations of self-produced syngas or dry gas, associated gas, natural gas, diesel, heavy oil, and pyrolysis oil; the gasifying agent enters the gasifier 14 through three channels: upper, middle, and lower. The gasifying agent type is oxygen, air, or steam, the gasifying agent temperature is 100-300℃, and the pressure is 0.001-25.0MPa; the ratio of the gasifying agent in the upper, middle, and lower channels is 5-20%: 20-50%: 30-75%.

[0055] Preferably, the pyrolyzer 13 has a pressure of 0.001-25.0 MPa, a pyrolysis temperature of 400-800℃, a pyrolysis gas velocity of 5-20 m / s, and a residence time of 2-20 s; the vaporizer 14 has a pressure of 0.001-25.0 MPa, a vaporization temperature of 900-1400℃, a gas velocity of 0.1-5 m / s, a residence time of 2-25 s, and a solid circulation ratio of 10-200 times.

[0056] Preferably, the pressure of the reburner 15 is 0.001-25.0 MPa, the combustion temperature is 700-950℃, the gas velocity is 0.1-5 m / s, and the residence time is 2-25 s. The reburner 15 maintains the circulating fluidization and material level balance of the reaction system by burning the ash and slag from the gasifier 14 and producing medium-pressure steam with a pressure of 2.5-6 MPa and a temperature of 350-450℃.

[0057] Preferably, the oil-gas enhanced separation device 24 is equipped with a demister, nozzle, filter screen, herringbone baffle, and settling hood, as well as a remote and online dual-measurement level gauge and an anti-clogging purging line. The demister is fixed to the top of the oil-gas enhanced separation device 24, and a guide plate is provided on one side of the demister to ensure that the liquid captured by the demister is discharged. The nozzle, filter screen, and herringbone baffle are located in the middle of the oil-gas enhanced separation device 24, and the nozzle is horizontally installed in a ring shape. The filter screen is fixed in the middle of the oil-gas enhanced separation device 24 by flange connection, and the material is one or a combination of metal, nano-metal wire mesh, or high-density packing, with a pore size of 30-50μm, forming a filter cake pressure differential of 50-200kPa. The herringbone baffle is arranged in 10-20 layers in a staggered manner, with a herringbone angle of 100-170°. The online level gauge line is equipped with a purging medium inlet to prevent solids from clogging the level gauge. The settling hood is fixed to the bottom of the oil-gas enhanced separation device 24 to prevent back mixing of the washing medium.

[0058] Preferably, the height-to-diameter ratio of the oil-gas enhanced separation device 24 is 2-5:1, the internal temperature is 250-550℃, the pressure is 0.001-25.0MPa, the operating gas velocity is 0.1-8.0m / s, and the washing medium is heavy oil or medium oil, wherein the heavy oil is a distillate oil with a temperature >350℃, and the medium oil is a distillate oil with a temperature of 250-350℃.

[0059] Preferably, the pressurized lock hopper 10, the multi-stage pressure reducing and ash discharge device 20, the heavy oil buffer tank 25, and the oil-water buffer tank 33 are alternating pressure devices. In addition to the device body, the alternating pressure devices also include pressurizing valves, pressure controlling valves, and pressure relief valves and their pipelines. In this embodiment, circulating carbon dioxide is used as the pressurizing gas to pressurize the alternating pressure devices. The purity of the carbon dioxide is 99-99.9%, and the pressure is 0.001-30.0 MPa.

[0060] Preferably, the deep gas-solid separation device 19 adopts a side-in, top-out structure. Internally, it consists of a large-pore support substrate layer and several small-pore membrane filter rods. The filter element pore size is 10-150μm, the porosity is 30-45%, and the filtration accuracy is 1-30μm. The deep gas-solid separation device 19 is externally connected to multiple staggered backflush ports. The pressure of the backflush air is 2-10 times that of the internal pressure of the deep gas-solid separation device 19. The maximum allowable operating temperature is 1000℃. Compared with existing atmospheric pressure filters, the deep gas-solid separation device 19 of this embodiment has the characteristics of high precision, high dust removal rate, low pressure drop, and high temperature and high pressure resistance.

[0061] Preferably, the multi-stage pressure reducing and ash discharge device 20 includes 1-3 pressure reducing and ash dischargers, including a pressure reducing pipe, a pressure controlling valve, a venting gas shut-off valve, and a venting recovery device. The pressure reducing pipe is used to receive high-pressure powder materials. After separation by the filter element inside the pressure reducing pipe, the powder enters the next stage pressure reducing and ash discharger. The pressure reducing pipe is provided with a gas outlet. The pressure reducing pipe is connected to the pressure controlling valve, the venting gas shut-off valve, and the venting recovery device in sequence. By adjusting the opening degree and gas volume of the powder material pressure controlling valve, the conveying rate of the powder material is controlled. The conveying rate is 10-1000 kg / h.

[0062] Preferably, the particle size of the solid particles in the multi-stage pressure reducing ash discharge device 20 is 10-200μm, the pressure of the first-stage pressure reducing ash discharge device is controlled at 10.0MPa-25.0MPa, the pressure of the second-stage pressure reducing ash discharge device is controlled at 1.0MPa-10.0MPa, and the pressure of the third-stage pressure reducing ash discharge device is controlled at 50KPa-1.0MPa.

[0063] Preferably, the second feeder 29 is provided with a solid feed pipe, a gas feed pipe, a discharge pipe, a buffer chamber, a transition chamber, a mixing chamber, an atomizing chamber, a discharge chamber, and a discharge cylinder. The solid feed pipe is connected to one end of the discharge cylinder, the discharge pipe is connected to the other end of the discharge cylinder, and the gas feed pipe is connected to the upper part of the discharge cylinder. All the above pipes are connected in a threaded, sealed manner. Inside the discharge cylinder, the discharge pipe is connected in sequence to the buffer chamber and the transition chamber. The outlet of the transition chamber is connected to the inlet of the atomizing chamber, and the outlet of the atomizing chamber is connected to the inlet of the discharge chamber. The second feeder 29 can accelerate the mixing, atomization, and flow rate of oily residues, increase the probability of effective collisions between molecules, and improve the conversion rate of oily residues. The gas includes one or more combinations of saturated steam, superheated steam, preheated carbon dioxide, or nitrogen. A heat tracing and insulation layer is provided along the outer wall of the second feeder 29.

[0064] Preferably, the atomizing chamber of the second feeder 29 has a size of DN15-DN60 and an inner diameter of D-2Dmm, and has an internal recess with a length L of D-5Dmm. The included angle α between the inner walls before and after the recess is in the range of 90-180°. The transition chamber has a size of DN15-DN60 and an inner diameter of D-2Dmm.

[0065] Preferably, the raw material suitable for the second feeder 29 has the following properties: high solid content 0-60%, high metal content >300μg / g and high residual carbon content >20%; the feed rate of oily residue is 0.1-1000kg / h, the operating temperature is room temperature-500℃, the operating pressure is 0.001-25.0MPa, the ratio of steam to oily residue is 0.1-0.5; and the residence time is 0.1-3.0s.

[0066] Preferably, the primary oil-gas cyclone device 30 and the deep oil-gas cyclone device 37 are both integrated multi-stage gas-liquid separators or multi-stage gas-liquid separators composed of 1-5 single-stage gas-liquid separators. Both sides of the primary oil-gas cyclone device 30 and the deep oil-gas cyclone device 37 are provided with guide plates for liquid discharge, so that the liquid flows into the intermediate oil collection tank 31 and the oil-water enhanced separator 34 respectively.

[0067] Preferably, the outer wall of the gas purification device 32 is connected from top to bottom via flanges to the gas inlet containing light oil, the washing water return tower inlet, and the washing water return tower inlet. From top to bottom, the outer wall of the cylinder is equipped with a condensate level gauge port, a condensate extraction port, a light oil level gauge port, and a level gauge port inside the tower, all connected by threaded seals. The liquid level is monitored and adjusted using these level gauges. A gas-liquid separator is installed in the upper part of the cylinder; the captured condensate forms a liquid seal through a condensate baffle, ensuring the separator's normal operation. A combination of herringbone and horizontal tower plates is installed in the middle of the cylinder to increase the washing and purification area and improve the washing effect. A liquid separator and an oil separator are installed in the lower part of the cylinder. After washing, the light oil condenses with the water, and at the bottom of the tower, the light oil separates above the water. When the height exceeds the oil separator, it naturally flows to one side of the oil separator and is discharged through the light oil outlet. The washing water is discharged from the other side of the oil separator, and the discharged washing water can be returned in whole or in part to the washing water return tower inlet or the washing water return tower inlet. The process gas has a temperature of 50-200℃, a pressure of 0.001-25.0MPaG, a dust content of <5.0ppm, a dust particle size of 0-5μm, and a light oil that is a distillate oil with a temperature of <200℃.

[0068] Preferably, the syngas generated by the gas separation and conversion device 40 is coupled with clean gas power generation for ultra-clean power generation and heat generation, or coupled with the Fischer-Tropsch synthesis process to produce clean oil products; the multiphase reactor 41 includes 1-5 multiphase flow enhanced hydrogenation reactors, and the products include, but are not limited to, naphtha, naphthenic oil, white oil, aviation fuel, aviation kerosene, military diesel, ultra-low pour point diesel, special lubricating oil base oil, modified asphalt and other special fuels.

[0069] Preferably, the gas sampling device 46 employs an internal structure consisting of bottom washing and absorption, middle condensation and recovery, and upper evaporation azeotropic distillation, along with an external cooling hydrazine structure, to obtain full-fraction tar. The solvent used for bottom washing and absorption is one or more combinations of acetone, dichloromethane, petroleum ether, ammonia, or self-produced medium or light oil; the oil-gas temperature is 200-600℃, and the solvent-to-oil ratio is 2-10:1. The middle section contains a condenser coil for circulating washing solvent, with an oil-gas temperature of 10-200℃. The upper evaporation section has an oil-gas temperature of 10-100℃, and the azeotropic solvent is one or more combinations of benzene and toluene, with a solvent-to-oil ratio of 0.5-5:1. The external cooling hydrazine temperature is 0-30℃, and the cooling medium is one or more combinations of ethylene glycol, ethanol, and water. The density of the obtained full-fraction tar is 1.00-1.10 g / cm³. 3 Solid content 0-0.5%, water content 0-0.5%.

[0070] Preferably, the pure oxygen produced as a byproduct of the water electrolysis hydrogen production process has a purity of 99.5-99.9%. After being thoroughly mixed with the gasifying agent, it enters the gasifier 14 and undergoes a gasification reaction under a pressure of 0.001-25.0 MPa. The resulting syngas contains 30-45% CO, 32-40% H2, 15-30% CO2, and 2-15% CH4.

[0071] Preferably, the multiphase reactor 41 comprises 1-5 enhanced hydrogenation reactors in a multiphase flow mode, with a pressure of 5.0-25.0 MPa, a temperature of 400-550°C, a hydrogen-to-oil ratio of 800-2400, and a space velocity of 0.2-4.0 h⁻¹. -1 With a catalyst addition of 0.1-2%, the tar conversion rate is >90% and the oil yield is >80%.

[0072] Preferred process parameters before carbon dioxide return to vaporizer 14: vapor-to-oxygen ratio 6-10 kg / m³ 3 The syngas contains 30-45% carbon monoxide, 32-40% hydrogen, 15-30% carbon dioxide, and 2-15% methane, with an H2 / CO ratio of 2.5-5:1. The process parameters after carbon dioxide is returned to the gasifier are: gas-oxygen ratio 4-7 kg / m³. 3 The synthesis gas contains 32-48% carbon monoxide, 10-26% hydrogen, 18-32% carbon dioxide, 2-12% methane, and an H2 / CO ratio of 1.2-3.5:1.

[0073] Preferably, carbon dioxide is returned to the gasifier 14 and used as a substitute for steam in the gasification reaction, per 1 Nm 3 The carbon dioxide can save 2-5 kg ​​of steam.

[0074] Preferably, the overall process has a carbon conversion rate >98%, a cold gas efficiency >78%, an effective gas composition of syngas >82%, and a syngas calorific value >2500 kcal / Nm³. 3 .

[0075] A method for using a zero-carbon emission new energy coupled coal fractionation conversion device includes the following steps:

[0076] Step 1: Electrolysis to produce hydrogen

[0077] 1.1 The electrical energy generated by the new energy power generation device 1 is distributed by the power distribution device 2. Part of it is transmitted to the power grid, part of it is connected to the grid and transmitted to the water electrolysis hydrogen production device 4, and the remaining part is transmitted to the energy storage device 3 for storage and backup.

[0078] 1.2 The water electrolysis hydrogen production unit 4 uses electrical energy to generate oxygen and hydrogen, which are stored in oxygen storage tank 5 and hydrogen storage tank 6 respectively. The oxygen in oxygen storage tank 5 is sent to gasifier 14 to participate in the gasification reaction; part of the hydrogen in hydrogen storage tank 6 is sent to pyrolyzer 13 to participate in the pyrolysis reaction, part is sent to hydrogen pressure controller 8 for pressurization and then enters multiphase reactor 41 to participate in the enhanced hydrogenation reaction of oil products, and the remaining part is sent to hydrogen storage unit 7 for storage and backup.

[0079] Step 2: Cyclic Reaction

[0080] 2.1 Using one or more combinations of quartz sand, pulverized coal, ash, semi-coke, petroleum coke, waste tire powder, waste catalyst, carbon black, and other carbon-containing solid particles as the heat carrier, a high-rate circulation return process with a circulation ratio of 50-200 is carried out between the pyrolyzer 13, gasifier 14, primary gas-solid separator 16, pulverized coke collector 17, and return material controller 18. Circulation return occurs through three different channels: internal, middle, and external. The system fluidizes and heats up at a rate of 5-20℃ / h, gradually increasing the temperature to 400-800℃. After the pulverized coal and solid heat carrier are thoroughly mixed, a rapid pyrolysis reaction occurs within the pyrolyzer 13, producing high-temperature oil gas and semi-coke.

[0081] 2.2 In the pyrolysis unit 13, 50-70% of the semi-coke and solid particles are returned to the gasifier 14 through the internal solid circulation return channel. The high-temperature synthesis gas generated by the gasification reaction in the gasifier 14 is returned to the pyrolysis unit 13 to provide reaction heat and an active atmosphere for the pyrolysis reaction; 10-20% of the high-temperature oil gas containing a small amount of semi-coke and solid particles enters the primary gas-solid separator 16, where the semi-coke and solid particles are captured and sequentially passed through the coke powder collector 17 and the return controller 18 before returning to the gasifier 14, forming the middle solid circulation return channel; the high-temperature oil gas carrying 1-10% of semi-coke enters the deep gas-solid separator 19, where the fly ash is captured and sequentially passed through the multi-stage pressure reducing ash discharge device 20, the fly ash buffer tank 21, and the fly ash collector 22 before returning to the reburner 15, forming the external solid circulation return channel;

[0082] Step 3: Purification and Recycling

[0083] 3.1 High-temperature oil and gas enter the enhanced oil-gas separation unit 24 for cooling and washing. The resulting oil and gas then enter the gas purification unit 32. The resulting liquid sequentially passes through the heavy oil buffer tank 25 and the primary oil-gas cyclone device 30. Heavy oil and medium oil are obtained in the heavy oil collection tank 26 and the medium oil collection tank 31, respectively, and used as the cooling medium for the enhanced separation unit 24. The heavy oil enters the liquid-solid enhanced separator 27. The solids produced after separation sequentially pass through the solid buffer tank 28 and the second feeder 29. Part of the solids enter the gasifier 14 for gasification reaction and are then recycled into the reaction system. The other part enters the multiphase reactor 41 for hydrogenation reaction. The liquid produced after separation sequentially passes through the medium oil collection tank 31 and then enters the multiphase reaction feedstock tank 38.

[0084] 3.2 After purification by the gas purification device 32, the resulting oil and gas enter the deep purification device 39, while the resulting liquid sequentially enters the oil-water buffer tank 33 and the oil-water enhanced separator 34. The oil and gas in the oil-water buffer tank 33 enters the deep oil-gas cyclone device 37, and the captured oil-water mixture enters the oil-water enhanced separator 34. The wastewater generated by the oil-water enhanced separator 34 enters the multi-effect evaporator 36 through the wastewater collection tank 35, and the generated steam enters the second feeder 29, where it is recycled as atomizing gas into the vaporizer 14. A portion of the liquid in the wastewater collection tank 35 is recycled back into the gas purification device 32.

[0085] Step 4: Oil Conversion

[0086] 4.1 Hydrogen from the hydrogen pressure regulator 8 enters the multiphase reactor 41 as a hydrogen supply gas to carry out an enhanced hydrogenation reaction with the distillate oil.

[0087] 4.2 The intermediate oil from the intermediate oil collection tank 31 enters the multiphase reaction feed tank 38 and the multiphase reactor 41 in sequence, and reacts with the oil-containing solids from the solid buffer tank 28 and the coal powder from the first feeder 12 to produce special fuel oil, modified asphalt and other coal-based products. The by-product residue enters the second feeder 29 and is fully mixed with atomized steam to be recycled as a supplementary carbon source for the gasification reaction.

[0088] Step 5: Gas Recycling

[0089] 5.1 The gas from the deep purification unit 39 enters the gas separation and conversion unit 40 to obtain syngas containing carbon monoxide and hydrogen, which enters the Fischer-Tropsch reactor 42 or the gas-fired power generation unit 43 for the production of clean oil products or ultra-clean power generation and heat generation.

[0090] 5.2 The gas separation and conversion device 40 separates carbon dioxide-containing gas, which sequentially enters the carbon dioxide buffer tank 44 and the carbon dioxide pressure controller 45. Among them: part of it enters the pressurized lock hopper 10, pressurized feed hopper 11, multi-stage pressure reducing ash discharge device 20, heavy oil buffer tank 25 and oil-water buffer tank 33 as pressurized gas; part of it enters the first feeder 12, return material controller 18 and second feeder 29 as solid medium conveying gas or fluidizing gas, and provides a reaction atmosphere; part of it enters the gasifier 14 as a gasifying agent to participate in the gasification reaction; the remaining part enters the deep gas-solid separation device 19 as backflushing gas.

Claims

1. A zero-carbon emission new energy coupled coal quality conversion device, characterized in that, The application relates to a coal-based multi-functional conversion system, which comprises a new energy hydrogen production unit, a circulating reaction unit, a gas-solid separation unit, a recovery conversion unit and a gas recycling unit. The new energy hydrogen production unit generates electricity through renewable new energy, and the generated oxygen and hydrogen are delivered to a water electrolysis hydrogen production device to provide an active atmosphere for the quality conversion and deep processing of coal. The circulating reaction unit completes the rapid segmented conversion of coal powder into tar and semicoke, and the semicoke is deeply converted into hydrogen-rich synthesis gas in a gasifier-reburner. The gas-solid separation unit completes the efficient separation and recycling of dust in high-temperature oil gas through a multi-stage gas-solid separation device. The recovery conversion unit obtains full-range tar through the efficient separation of gas and liquid phases, and produces special fuel and modified asphalt coal-based products through intensified hydrogenation reaction; and the gas recycling unit uses carbon dioxide in the synthesis gas as conveying gas, fluidizing gas, pressure charging gas and back flushing gas to realize the recycling of carbon dioxide gas. The circulating reaction unit comprises a hopper (9), a pressurized lock hopper (10) connected with the hopper (9), a pressurized feeding hopper (11) connected with the pressurized lock hopper (10), a first feeder (12) connected with the pressurized feeding hopper (11), an outlet of the first feeder (12) connected with a lower inlet of a pyrolyzer (13), an outlet of the lower inlet of the pyrolyzer (13) connected with an outlet of a hydrogen storage tank (6), the pyrolyzer (13) connected with a primary gas-solid separation device (16), a powder coke collector (17), a return material controller (18) and a gasifier (14) in sequence to form a middle solid circulation, a lower part of the pyrolyzer (13) connected with the gasifier (14) to form an internal solid circulation, the primary gas-solid separation device (16) connected with a deep gas-solid separation device (19), a multi-stage pressure reduction ash discharge device (20), a fly ash buffer tank (21), a fly ash collector (22), a reburner (15) and a bottom of the gasifier (14) in sequence to form an external solid circulation, a lower inlet of the gasifier (14) connected with an outlet of an oxygen storage tank (5), a second feeder (29) and a carbon dioxide pressure controller (45), an upper part of the reburner (15) connected with the gasifier (14), an output end of the reburner (15) connected with an input end of the primary gas-solid separation device (16), an input end of the reburner (15) connected with an output end of the fly ash collector (22), an output end of the reburner (15) connected with an input end of the second feeder (29), a bottom outlet pipeline of a waste water collecting tank (35) connected with a part of the reburner (15) as a cooling medium of high-temperature ash and a part of a multi-effect evaporator (36) as an evaporation medium.

2. The zero-carbon emission new energy coupled coal quality conversion device according to claim 1, characterized in that, The gas-solid separation unit comprises the powder coke collector (17) and the deep gas-solid separation device (19) connected with the primary gas-solid separation device (16), the oil gas intensified separation device (24) connected with the deep gas-solid separation device (19) and the fly ash pressure relief tank (23) connected with the upper part of the multi-stage pressure reduction ash discharge device (20), and the outlet of the fly ash pressure relief tank (23) connected with the inlet of the fly ash buffer tank (21) and the oil gas intensified separation device (24) respectively.

3. The zero-carbon emission new energy coupled coal quality conversion device according to claim 2, characterized in that, The output end of the deep gas-solid separation device (19) is connected with the input end of a gas sampling device (46), which is composed of a high-temperature pretreater, a primary quenching scrubbing tank, a secondary scrubbing cooling tank, a reflux tank and a pyrolysis circulating refrigeration system, realizes two-phase separation of oil and dust in the gas and online analysis of the purified gas; the high-temperature dust-containing gas enters the high-temperature pretreater, captures small-particle-size dust through a ceramic filter with a filter accuracy of 1-20 μm, and is suitable for the dust amount range of 10-300 g / Nm 3 The high-temperature gas from which the dust is removed enters the primary quenching scrubbing tank and the secondary scrubbing cooling tank in which a solution absorbent is filled, the primary quenching scrubbing tank is a quenching heat exchanger, the secondary scrubbing cooling tank is composed of an upper scrubbing section, a middle cooling section and a bottom filter inner cylinder, the gas is cooled by internal coils and cold walls, and the separated solution absorbent is returned to the primary quenching scrubbing tank through the reflux tank; the primary quenching scrubbing tank and the secondary scrubbing cooling tank are both provided with a pyrolysis circulating refrigeration system, the collected solution is dehydrated, dedusted and rotary evaporated to obtain full-range coal tar; the temperature of the high-temperature pretreater is 500-800℃, the temperature of the primary quenching scrubbing tank is 100-500℃, the temperature of the secondary scrubbing cooling tank is 30-250℃, the temperature of the pyrolysis circulating refrigeration system is 0--30℃, the heat tracing temperature is >400-450℃, the operating pressure is 0.001-25.0 MPa, and the gas flow is 10-100 Nm 3 / h. The depth gas-solid separation device (19) is a side-in top-out structure, and is composed of a large-aperture support matrix layer and a plurality of small-aperture membrane filter rods in the inside, the filter core aperture is 10-150 μm, and the porosity is 30-45%.

4. The zero-carbon emission new energy coupled coal quality conversion device according to claim 1, characterized in that, The recovery conversion unit comprises a heavy oil buffer tank (25) connected with the oil-gas enhanced separation device (24) and a gas purification device (32), the upper output end of the heavy oil buffer tank (25) is connected with the input end of a primary oil-gas cyclone device (30), the bottom output end of the heavy oil buffer tank (25) is connected with the input end of a heavy oil collection tank (26), the output end of the heavy oil collection tank (26) is connected with the input end of a liquid-solid enhanced separator (27), the solid phase outlet of the liquid-solid enhanced separator (27) is connected with the solid phase inlet of a solid buffer tank (28), the solid phase outlet of the solid buffer tank (28) is connected with the solid phase inlet of a second feeder (29), the liquid phase outlet of the liquid-solid enhanced separator (27) is connected with the liquid phase inlet of a middle oil collection tank (31), the output end of the middle oil collection tank (31) is connected with the input end of a multi-phase reaction raw material tank (38), and the outlet of the primary oil-gas cyclone device (30) is connected with the inlet of the middle oil collection tank (31); the upper outlet of the gas purification device (32) is connected with the inlet of a deep purification device (39), the bottom of the gas purification device (32) is sequentially connected with an oil-water buffer tank (33), an oil-water enhanced separator (34), a waste water collection tank (35) and a light oil tank (49), the outlet of the waste water collection tank (35) is connected with the inlet of the gas purification device (32) and a multi-effect evaporator (36) respectively, the outlet of the multi-effect evaporator (36) is connected with the inlet of the second feeder (29); the inlet of the multi-phase reaction raw material tank (38) is connected with the outlet of the middle oil collection tank (31), the outlet of the multi-phase reaction raw material tank (38) is connected with the inlet of a multi-phase reactor (41), the bottom outlet of the multi-phase reactor (41) is connected with the inlet of the second feeder (29), and the inlet of the multi-phase reactor (41) is also connected with a hydrogen pressure controller (8), a first feeder (12) and the outlet of the solid buffer tank (28).

5. The zero-carbon emission new energy coupled coal quality conversion device according to claim 4, characterized in that, The primary oil-gas cyclone device (30) and the deep oil-gas cyclone device (37) are all integrated multi-stage gas-liquid separators, or multi-stage gas-liquid separators composed of 1-5 single-stage gas-liquid separators in series. The multi-phase reactor (41) comprises 1-5 multi-phase flow state enhanced hydrogenation reactors in series.

6. The zero-carbon emission new energy coupled coal quality conversion device according to claim 1, characterized in that, The gas recycling unit comprises a gas purification device (32) connected with a deep purification device (39), a gas shift separation device (40) and a light oil tank (49), an outlet of the deep oil gas cyclone device (37) is connected with an upper inlet of the oil-water intensified separator (34), outlets of the gas shift separation device (40) are respectively connected with inlets of the Fischer-Tropsch reactor (42), the gas power generation device (43) and the carbon dioxide buffer tank (44), an outlet of the carbon dioxide buffer tank (44) is connected with an inlet of the carbon dioxide pressure controller (45), an outlet of the carbon dioxide pressure controller (45) is respectively connected with inlets of the pressurized lock hopper (10), the pressurized feeding hopper (11), the first feeder (12), the gasifier (14), the re-burner (15), the return material controller (18), the deep gas-solid separation device (19), the multi-stage pressure-reducing ash discharge device (20), the heavy oil buffer tank (25), the second feeder (29) and the oil-water buffer tank (33), and an outlet of the oil-water buffer tank (33) is connected with an inlet of the deep oil gas cyclone device (37).

7. The zero-carbon emission new energy coupled coal quality conversion device according to claim 1, characterized in that, The new energy hydrogen production unit comprises a new energy power generation device (1), a power allocation device (2) and an energy storage device (3) connected with the new energy power generation device (1) in sequence, an output end of the power allocation device (2) is connected with an input end of the water electrolysis hydrogen production device (4), outlets of the water electrolysis hydrogen production device (4) are respectively connected with inlets of an oxygen storage tank (5) and a hydrogen storage tank (6), an outlet of the hydrogen storage tank (6) is connected with inlets of a hydrogen storage device (7), a hydrogen pressure controller (8) and a pyrolyzer (13), and an output end of the hydrogen pressure controller (8) is connected with an input end of a multi-phase reactor (41). The outlet of the hydrogen storage tank (6) is connected with the inlet of the hydrogen storage device (7), and the hydrogen storage device (7) adopts pressure hydrogen storage or liquid hydrogen storage.

8. A method of using a zero-carbon emission new energy coupled coal quality conversion device according to any one of claims 1-7, characterized in that, The method comprises the following steps: Step one, electrolysis hydrogen production; 1.1) part of the electric energy generated by the new energy power generation device (1) is delivered to the power allocation device (2), part of the electric energy is delivered to the water electrolysis hydrogen production device (4) through power grid, and part of the electric energy is delivered to the energy storage device (3) for storage; 1.2) the oxygen generated by the water electrolysis hydrogen production device (4) by using electric energy is stored in the oxygen storage tank (5) and delivered to the gasifier (14) to participate in the gasification reaction, the hydrogen generated is stored in the hydrogen storage tank (6), part of the hydrogen is delivered to the pyrolyzer (13) to participate in the pyrolysis reaction, part of the hydrogen is delivered to the hydrogen pressure controller (8) to participate in the oil product intensified hydrogenation reaction after being pressurized, and the remaining hydrogen is delivered to the hydrogen storage device (7) for storage; Step two, cyclic reaction; The coal powder enters the pyrolyzer (13) from the first feeder (12) and mixes with the solid heat carrier, and the pyrolysis reaction occurs in the pyrolyzer (13) to produce high-temperature oil gas and semi-coke. Most of the semi-coke returns to the gasifier (14) through the internal solid circulation return channel. The high-temperature oil gas containing a small amount of semi-coke and solid particles enters the primary gas-solid separator (16), and the semi-coke and solid particles are captured and returned to the gasifier (14) through the coke collector (17) and the return controller (18). The high-temperature oil gas carrying fly ash enters the deep gas-solid separator (19), and the fly ash is captured and returned to the reburner (15) in turn through the multi-stage pressure reduction ash removal device (20), the fly ash buffer tank (21), and the fly ash collector (22). Step three: purification and recovery; 3.1) The high-temperature oil gas separated by the deep gas-solid separator (19) enters the oil gas strengthening separation device (24) for cooling and washing, and the generated oil gas enters the gas purification device (32). The generated liquid enters the heavy oil buffer tank (25) to obtain heavy oil and medium oil, respectively. The heavy oil enters the heavy oil collection tank (26) and the liquid-solid strengthening separator (27) in turn, and the medium oil enters the primary oil gas cyclone device (30); 3.2) The solid separated by the liquid-solid strengthening separator (27) enters the gasifier (14) through the solid buffer tank (28) and the second feeder (29) in turn to be recycled and reused. The liquid separated by the liquid-solid strengthening separator (27) and the medium oil separated by the primary oil gas cyclone device (30) enter the medium oil collection tank (31) in turn; 3.3) After the oil gas is purified by the gas purification device (32), the generated gas enters the deep purification device (39), and the generated liquid enters the oil-water buffer tank (33). The oil gas carried enters the deep oil gas cyclone device (37), and the liquid enters the oil-water strengthening separator (34) to separate light oil and waste water. The light oil enters the light oil tank (49), and the waste water enters the waste water collection tank (35) and the multi-effect evaporator (36) in turn to generate steam. The steam enters the second feeder (29) as atomizing gas and is recycled into the gasifier (14). Part of the liquid in the waste water collection tank (35) is recycled into the gas purification device (32); Step four: oil product conversion; 4.1) The medium oil collected in the medium oil collection tank (31) and the light oil separated by the oil-water strengthening separator (34) and the deep purification device (39) enter the multi-phase reaction raw material tank (38) and the multi-phase reactor (41) in turn. The hydrogen gas in the hydrogen gas pressure controller (8) enters the multi-phase reactor (41) as hydrogen supply gas. The medium oil from the medium oil collection tank (31) enters the multi-phase reaction raw material tank (38) and the multi-phase reactor (41) in turn, and reacts with the oil-containing solid from the solid buffer tank (28) and the coal powder from the first feeder (12) to generate special fuel oil and modified asphalt coal-based products; 4.2) The residue generated by the multi-phase reactor (41) enters the second feeder (29) and the gasifier (14) in turn, and is recycled and utilized as a supplementary carbon source for the gasification reaction; Step five: gas recycling; The gas purified by the deep purification device (39) enters a gas separation shift device (40), the separated gas containing carbon monoxide and hydrogen enters a Fischer-Tropsch reactor (42) for producing clean oil products, or enters a gas-fired power generation device (43) for generating electricity or heat energy; the separated gas containing carbon dioxide enters a carbon dioxide buffer tank (44) and a carbon dioxide pressure controller (45) in sequence, wherein: a part thereof serves as pressurizing gas and enters the pressurizing lock hopper (10), the pressurizing feeding hopper (11), the multi-stage pressure-reducing ash discharging device (20), the heavy oil buffer tank (25) and the oil-water buffer tank (33) respectively; a part thereof serves as conveying gas of the solid medium and enters the first feeder (12), the return material controller (18) and the second feeder (29) to provide a reaction atmosphere; another part thereof serves as a gasification agent and enters the gasifier (14) to participate in a gasification reaction; and the remaining part thereof serves as back-blowing gas and enters the deep gas-solid separation device (19).

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