CN117072263A - Hydrogen and electricity combined production system coupling coal partial gasification and semicoke pressurization oxygen-enriched combustion - Google Patents

Hydrogen and electricity combined production system coupling coal partial gasification and semicoke pressurization oxygen-enriched combustion Download PDF

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Publication number
CN117072263A
CN117072263A CN202310632955.8A CN202310632955A CN117072263A CN 117072263 A CN117072263 A CN 117072263A CN 202310632955 A CN202310632955 A CN 202310632955A CN 117072263 A CN117072263 A CN 117072263A
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oxygen
temperature
heat exchanger
gas
pressurized
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张泽祎
邵应娟
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Southeast University
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Southeast University
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/02—Preparation of oxygen
    • C01B13/0229—Purification or separation processes
    • C01B13/0248—Physical processing only
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/50—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K13/00—General layout or general methods of operation of complete plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K13/00—General layout or general methods of operation of complete plants
    • F01K13/006—Auxiliaries or details not otherwise provided for
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
    • F01K17/02—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K21/00—Steam engine plants not otherwise provided for
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B33/00—Steam-generation plants, e.g. comprising steam boilers of different types in mutual association
    • F22B33/18—Combinations of steam boilers with other apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
    • F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2

Abstract

The invention discloses a hydrogen and electricity cogeneration system coupling coal partial gasification and semicoke pressurized oxygen-enriched combustion. Compared with the prior art that normal-pressure air combustion is generally adopted for semicoke combustion, air and steam are generally adopted for the existing gasification atmosphere, the pressurized circulating fluidized bed is adopted as a reactor for coal partial gasification and semicoke pressurized oxygen-enriched combustion, and pure oxygen and circulating flue gas carbon dioxide are adopted as the gasification atmosphere. The semicoke oxygen-enriched combustion can burn semicoke as much as possible, and enrich CO in combustion products 2 So that the system captures CO 2 The system is easier to operate, 0 carbon emission is easier to realize, and the overall operation efficiency of the system is improved. Pure oxygen is provided by the air separation oxygen generation unit, and carbon dioxide is provided by the carbon dioxide capturing unit, so that the reasonable utilization of waste gas in the system is realized.

Description

Hydrogen and electricity combined production system coupling coal partial gasification and semicoke pressurization oxygen-enriched combustion
Technical Field
The invention relates to the field of hydrogen energy preparation, in particular to a hydrogen and electricity cogeneration system coupling coal partial gasification and semicoke pressurized oxygen-enriched combustion.
Background
Compared with the traditional fossil energy, the hydrogen energy has wide application prospect as a green energy. The hydrogen production system is used as an important link for hydrogen energy generation, and plays a vital role in the application and development of the hydrogen energy.
At present, fossil fuel is still used as a main raw material for hydrogen production worldwide, and China is used as a large country of coal, and coal is used as a main hydrogen production raw material. The traditional coal gasification hydrogen production process converts coal into hydrogen and some other gases (such as carbon monoxide, carbon dioxide and the like) through a series of reactions, and chemical energy of the other gases is not utilized. Therefore, the problems of high carbon emission, high energy consumption, pollutant emission and the like of the coal hydrogen production limit the further development and application of the coal hydrogen production.
The current hydrogen production system adopts integral gasification, has high requirement on equipment operation, mainly adopts air and vapor as gasifying agents, adopts air normal pressure combustion in a combustion part, leads to pressure difference between coal gasification and the combustion part, leads to energy loss, leads to pollutant increase and is unfavorable for capturing carbon dioxide due to normal pressure air combustion, is mainly used for power circulation, has lower overall hydrogen and electricity, is mainly used for power generation, and does not use hydrogen as a main product.
Disclosure of Invention
The invention aims to solve the defects in the prior art and provide a hydrogen and oxygen-enriched combustion coupled hydrogen and oxygen-enriched combustion combined system which realizes high-efficiency hydrogen and oxygen combined production of coal and zero emission of pollutants such as sulfur oxides, nitrogen oxides and carbon dioxide greenhouse gases.
In order to solve the technical problems, the invention adopts the technical method that: the invention discloses a hydrogen and electricity cogeneration system coupling coal partial gasification and semicoke pressurized oxygen-enriched combustion, which comprises an air separation oxygen production unit, a coal partial gasification unit, a semicoke pressurized oxygen-enriched combustion unit, a gasification product purification and reforming unit, a pressure swing adsorption unit, a steam Rankine cycle power generation unit and CO 2 A trapping unit;
the air separation oxygen production unit is used for conveying oxygen to the coal partial gasification unit and the semicoke pressurized oxygen-enriched combustion unit;
the coal partial gasification unit performs coal partial gasification reaction, the crude synthesis gas is sent to the gasification product purification and reforming unit, and the semicoke of the solid product is sent to the semicoke combustion unit;
the semicoke pressurized oxygen-enriched combustion unit respectively obtains pure oxygen, semicoke and recirculated flue gas from the air separation oxygen production unit, the coal partial gasification unit and the steam Rankine cycle power generation unit, performs combustion reaction, and performs gas-solid separation on combustion products;
the semicoke pressurized oxygen-enriched combustion unit provides high-temperature water vapor for the steam Rankine cycle power generation unit, and the steam Rankine cycle power generation unit provides low-temperature water vapor for the semicoke pressurized oxygen-enriched combustion unit to realize water vapor circulation;
the gasification product purifying and reforming unit sends clean synthesis gas subjected to reforming reaction and change reaction into the pressure swing adsorption unit;
the pressure swing adsorption unit separates and stores hydrogen in the clean synthesis gas, and sends the synthesis gas waste gas after hydrogen removal into the CO 2 And a trapping unit.
Further, the coal partial gasification unit comprises a pressurized circulating fluidized bed gasification furnace, a coal drying and purifying device and a gas-solid separation device;
the pulverized coal is sent into a pressurized circulating fluidized bed gasifier after being dried and purified by a coal drying and purifying device; oxygen is conveyed to the pressurized circulating fluidized bed gasifier by an oxygen heater; the CO 2 The carbon dioxide heat exchanger in the capturing unit is the pressurizing circulationAnnular fluidized bed gasifier for CO supply 2 Partial gasification reaction of coal occurs in the pressurized circulating fluidized bed gasifier;
the reaction product of the pressurized circulating fluidized bed gasifier is sent to the gas-solid separation device for separation treatment; the gas-solid separation device sends the crude synthesis gas into a waste heat recovery heat exchanger in the gasification product purification and reforming unit, and sends the semicoke of the solid product into a pressurized circulating fluidized bed combustion furnace in the semicoke combustion unit for combustion.
Further, the semicoke pressurized oxygen-enriched combustion unit comprises a pressurized circulating fluidized bed combustion furnace and a cyclone separator;
the feed inlet of the pressurized circulating fluidized bed combustion furnace is communicated with an oxygen heater in the air separation oxygen generation unit, a gas-solid separation device in the coal partial gasification unit and an economizer in the steam Rankine cycle power generation unit, so that pure oxygen, semicoke and recirculated flue gas are respectively obtained for combustion reaction;
the pressurized circulating fluidized bed combustion furnace outputs all water vapor to a low-temperature superheater in the steam Rankine cycle power generation unit and outputs all combustion reaction products to a cyclone separator in the semicoke pressurized oxygen-enriched combustion unit;
the cyclone separator carries out gas-solid separation on combustion products in the pressurized circulating fluidized bed combustion furnace to realize separation of gas flue gas and solid waste; the cyclone separator sends the solid waste to a medium-temperature superheater in the steam Rankine cycle power generation unit, and sends the gaseous flue gas to a high-temperature superheater in the steam Rankine cycle power generation unit.
Further, the gasification product purifying and reforming unit comprises a waste heat recovery heat exchanger, a impurity removing device, a reforming reactor and a synthesis gas heat exchanger;
the waste heat recovery heat exchanger is used for carrying out waste heat recovery on the crude gasification product output by the gas-solid separation device, and takes the heat as a heat source of the reforming reactor;
the discharge port of the waste heat recovery heat exchanger is communicated with the feed port of the impurity removing device;
the impurity removing device is used for desulfurizing the gasification product, removing acid gas in the crude synthesis gas and then conveying the crude synthesis gas to the reforming reactor;
the high-temperature heat exchanger in the steam Rankine cycle power generation unit inputs water vapor for the reforming reactor to be used as a reactant of reforming reaction;
the discharge port of the reforming reactor is communicated with a synthesis gas heat exchanger, and the synthesis gas heat exchanger sends clean synthesis gas subjected to reforming reaction and changing reaction to a pressure swing adsorption device in the pressure swing adsorption unit.
Further, the steam Rankine cycle power generation unit comprises a low-temperature superheater, a medium-temperature superheater, a high-pressure steam turbine, a medium-pressure steam turbine, a low-pressure steam turbine, a condenser, a high-temperature heat exchanger, a low-temperature heat exchanger, a water pump, an economizer, a low-temperature reheater and a high-temperature reheater;
the medium-temperature superheater receives high-temperature solid waste output by the cyclone separator and steam discharged by the low-temperature superheater; in the medium-temperature superheater, after the solid waste heats water vapor to overheat the water vapor, the medium-temperature superheater conveys the water vapor to the high-temperature superheater and outputs the solid waste to the low-temperature superheater; the solid waste is sent into the pressurized circulating fluidized bed combustion furnace through the low-temperature superheater;
the high-temperature superheater further superheats high-temperature steam input by the medium-temperature superheater by utilizing high-temperature gaseous flue gas provided by the cyclone separator, outputs the high-temperature steam to the high-pressure steam turbine, and provides gaseous flue gas to the high-temperature reheater;
the high-pressure steam turbine transmits high-temperature steam to the high-temperature heat exchanger and the low-temperature reheater;
the low-temperature reheater further heats high-temperature steam passing through the low-temperature reheater by utilizing the high-temperature gaseous flue gas conveyed by the high-temperature reheater, and conveys the high-temperature steam to the high-temperature reheater;
the high-temperature reheater provides reheated steam for the medium-pressure steam turbine and outputs gaseous smoke to the low-temperature reheater;
the medium-pressure steam turbine is communicated with the low-temperature heat exchanger, the other branch is communicated with the low-pressure steam turbine, and the discharge port of the low-pressure steam turbine is communicated with the feed port of the condenser;
the water vapor is cooled into liquid state in the condenser, and is sent into the low-temperature heat exchanger through the structured water pump to circulate; the water pump can also directly supply water to the low-temperature heat exchanger.
Further, the water vapor expands in the high-pressure steam turbine to do work and output power, and the water vapor state of a discharge port of the high-pressure steam turbine is 4MPa;
in the high-temperature reheater, the gaseous smoke is used for reheating water vapor, and the state of a water vapor discharge hole of the high-temperature reheater is 560 ℃ and 4MPa;
the steam expands in a medium-pressure steam turbine to do work and output power, and the steam state of a discharge port of the medium-pressure steam turbine is 2MPa;
the steam expands in the low-pressure steam turbine to do work and output power, and the steam state of the discharge port is 0.75MPa.
Further, the pressure swing adsorption unit comprises a pressure swing adsorption device, a hydrogen compressor, a hydrogen storage device and an exhaust gas heat exchanger;
the pressure swing adsorption device separates hydrogen in the clean synthesis gas and sends the hydrogen to the hydrogen compressor for pressurization, and the hydrogen compressor sends the pressurized hydrogen to the hydrogen storage device for preservation; and sending the synthesis gas waste gas after hydrogen removal into a waste gas heat exchanger.
Further, the CO 2 The trapping unit comprises a flash evaporation reactor, an exhaust gas multi-stage compressor, an exhaust gas purifying device, a carbon dioxide heat exchanger, an exhaust gas distillation tower, a carbon dioxide compressor and a carbon dioxide storage device;
the pressure swing adsorption device separates hydrogen in the clean synthesis gas and sends the hydrogen to the hydrogen compressor for pressurization, and the hydrogen compressor sends the pressurized hydrogen to the hydrogen storage device for preservation; the synthesis gas waste gas after hydrogen removal is sent to a waste gas heat exchanger;
the waste gas heat exchanger sends waste gas into a flash evaporation reactor; after the flash evaporation reactor discharges the moisture in the waste gas, the waste gas is subjected toThe dry waste gas is sent into a waste gas multistage compressor for pressurization and then is sent into a waste gas purifying device, and after washing, NO is converted into HNO in the NOx removal process 3 Separating the carbon dioxide from the remaining acidic solution;
the waste gas purification device sends the waste gas after washing into a carbon dioxide heat exchanger, and the waste gas is conveyed to a waste gas distillation tower through the carbon dioxide heat exchanger; the waste gas distillation tower separates the input waste gas into CO and the rest gas, and then sends the CO and the rest gas into the carbon dioxide heat exchanger.
The carbon dioxide heat exchanger pressurizes a part of carbon dioxide through a carbon dioxide compressor and then sends the pressurized carbon dioxide into a carbon dioxide storage device for storage; and the other part of carbon dioxide is sent into the pressurized circulating fluidized bed gasifier.
Further, the air separation oxygen generation unit comprises an air compressor, an air heat exchanger, an air low-pressure distillation tower, an air high-pressure distillation tower and an oxygen heater;
the air is sent into the air heat exchanger through the air compressor to be cooled, and then is respectively sent into the low-pressure distillation tower and the air high-pressure distillation tower through the air heat exchanger; the air is distilled into O in a distillation tower 2 And N 2 ；
The air high-pressure distillation tower outputs oxygen and nitrogen to the low-pressure distillation tower; the low-pressure distillation tower respectively transmits oxygen and nitrogen to the air heat exchanger;
the air heat exchanger separates nitrogen by utilizing air, cools and separates oxygen, and sends the obtained high-purity oxygen to the oxygen heater; and after the oxygen heater heats the oxygen, the oxygen is respectively sent into the coal partial gasification unit and the semicoke pressurized oxygen-enriched combustion unit.
Further, the operation temperature of the pressurized circulating fluidized bed gasifier is controlled to be 750-1150 ℃ and the operation pressure is controlled to be 1-3MPa.
The beneficial effects are that:
1. compared with the prior art that normal-pressure air combustion is generally adopted for semicoke combustion, air and steam are generally adopted for the existing gasification atmosphere, the pressurized circulating fluidized bed is adopted as a reactor for coal partial gasification and semicoke pressurized oxygen-enriched combustion in the invention, and the method adoptsPure oxygen and recycled flue gas carbon dioxide are used as gasification atmosphere. The semicoke oxygen-enriched combustion can burn semicoke as much as possible, and enrich CO in combustion products 2 So that the system captures CO 2 The system is easier to operate, 0 carbon emission is easier to realize, and the overall operation efficiency of the system is improved. Pure oxygen is provided by the air separation oxygen generation unit, and carbon dioxide is provided by the carbon dioxide capturing unit, so that the reasonable utilization of waste gas in the system is realized.
2. Compared with the prior art, the method has the advantages that the synthetic gas partially gasified by coal is directly fed into the gas turbine for combustion power generation, and a reforming reactor is not adopted for CO change reaction, so that the hydrogen ratio in the product is lower. The invention takes the synthesis gas product of coal partial gasification as the primary purpose of hydrogen production, and improves the hydrogen yield; the gasification product purifying and reforming unit adopts steam methane reforming reaction and CO change reaction to make steam react with methane to generate CO and H 2 And CO 2 And adjusting CO and H in the synthesis gas after reforming reaction 2 Proportion is increased by H 2 The ratio in the synthesis gas increases the hydrogen yield.
3. Compared with the prior art that the water vapor required by the reforming reaction is obtained from the outside, the outlet of the high-temperature heat exchanger in the steam Rankine cycle power generation unit is communicated with the gasification product purifying and reforming reactor in the reforming unit, and the high-temperature heat exchanger does not provide high-temperature water vapor as reaction gas. And the heat source for heating the steam participating in the reforming reaction is the waste heat of the synthesis gas in the waste heat recovery heat exchanger. Realize the high-efficient utilization of vapor and the utilization of heat, improve the thermal efficiency of system.
Drawings
FIG. 1 is a schematic diagram of a combined hydrogen and power generation system coupled with partial gasification of coal and pressurized oxygen-enriched combustion of semicoke.
Detailed Description
The following examples are illustrative, not limiting, and are not intended to limit the scope of the invention.
The invention provides a method for partial gasification of coal by using a pressurized fluidized bed and a pressurized circulating fluidized bed combustion furnaceSemi-pressurized oxygen-enriched combustion adopts circulating flue gas and pure oxygen as hydrogen co-production system of gasification atmosphere, and this co-production system includes: air separation oxygen generation unit, coal partial gasification unit, semicoke pressurized oxygen-enriched combustion unit, gasification product purification and reforming unit, pressure swing adsorption unit, steam Rankine cycle power generation unit and CO 2 And a trapping unit.
The air separation oxygen generation unit comprises an air compressor 1, an air heat exchanger 2, an air low-pressure distillation tower 3, an air high-pressure distillation tower 4 and an oxygen heater 5;
the coal partial gasification unit comprises a pressurized circulating fluidized bed gasification furnace 6, a coal drying and purifying device 7 and a gas-solid separation device 8;
the semicoke pressurized oxygen-enriched combustion unit comprises a pressurized circulating fluidized bed combustion furnace 24 and a cyclone separator 38;
the gasification product purifying and reforming unit comprises a waste heat recovery heat exchanger 9, a impurity removing device 10, a reforming reactor 11 and a synthesis gas heat exchanger 12;
the pressure swing adsorption unit comprises a pressure swing adsorption device 13, a hydrogen compressor 14, a hydrogen storage device 15 and an exhaust gas heat exchanger 16;
CO 2 the trapping unit comprises a flash evaporation reactor 17, an exhaust gas multistage compressor 18, an exhaust gas purifying device 19, a carbon dioxide heat exchanger 20, an exhaust gas distillation tower 21, a carbon dioxide compressor 22 and a carbon dioxide storage device 23;
the steam Rankine cycle power generation unit comprises a low-temperature superheater 25, an intermediate-temperature superheater 26, a high-temperature superheater 27, a high-pressure steam turbine 28, an intermediate-pressure steam turbine 29, a low-pressure steam turbine 30, a condenser 31, a high-temperature heat exchanger 32, a low-temperature heat exchanger 33, a water pump 34, an economizer 35, a low-temperature reheater 36 and a high-temperature reheater 37;
the air is sent into an air heat exchanger 2 through an air compressor 1 to be cooled, and then is respectively sent into a low-pressure distillation tower 3 and a high-pressure distillation tower 4 through the air heat exchanger 2; the air is distilled into O in a distillation tower 2 And N 2 ；
The high-pressure distillation tower 4 outputs oxygen and nitrogen to the low-pressure distillation tower 3; the low-pressure distillation tower 3 respectively transmits oxygen and nitrogen to the air heat exchanger 2;
the air heat exchanger 2 separates nitrogen by utilizing air, cools and separates oxygen, and sends the obtained oxygen with 99% purity to the oxygen heater 5; after oxygen is heated by the oxygen heater 5, the oxygen is respectively sent into a coal partial gasification unit and a semicoke pressurized oxygen-enriched combustion unit;
the oxygen-enriched discharge port of the high-pressure distillation tower 4 is communicated with the feed port of the low-pressure distillation tower 3, the oxygen discharge port of the low-pressure distillation tower 3 is communicated with the oxygen feed port of the air heat exchanger 2, and the nitrogen discharge port of the low-pressure distillation tower 3 is communicated with the nitrogen feed port of the air heat exchanger 2;
wherein the air compressor 1 is pressurized to 1MPa, the pressure of the low-pressure distillation tower 3 and the pressure of the high-pressure distillation tower 4 are respectively 0.25MPa and 1MPa, and the oxygen heater 5 is heated to 400 ℃. .
The pulverized coal is sent into a pressurized circulating fluidized bed gasifier 6 after being dried and purified by a coal drying and purifying device 7; the oxygen heater 5 supplies oxygen to the pressurized circulating fluidized bed gasifier 6; CO 2 The carbon dioxide heat exchanger 20 in the capturing unit supplies CO to the pressurized circulating fluidized bed gasification furnace 6 2 The pressurized circulating fluidized bed gasification furnace 6 is internally provided with a coal partial gasification reaction; wherein, the operation temperature of the pressurized circulating fluidized bed gasifier 6 is controlled between 750 ℃ and 1150 ℃ and the operation pressure is controlled between 1MPa and 3MPa.
The reaction product of the pressurized circulating fluidized bed gasifier 6 is sent into a gas-solid separation device 8 for separation treatment; the gas-solid separation device 8 sends the crude synthesis gas to the waste heat recovery heat exchanger 9 in the gasification product purification and reforming unit, and sends the semicoke of the solid product to the pressurized circulating fluidized bed combustion furnace 24 in the semicoke combustion unit for combustion;
the feed inlet of the pressurized circulating fluidized bed combustion furnace 24 is communicated with an oxygen heater 5 in the air separation oxygen generation unit, a gas-solid separation device 8 in the coal partial gasification unit and an economizer 35 in the steam Rankine cycle power generation unit, so that pure oxygen, semicoke and recirculated flue gas are respectively obtained for combustion reaction;
the pressurized circulating fluidized bed combustor 24 outputs all water vapor to the low temperature superheater 25 and all combustion reaction products to the cyclone 38;
the cyclone separator 38 performs gas-solid separation on combustion products in the pressurized circulating fluidized bed combustion furnace 24 to separate gas flue gas from solid waste; cyclone 38 feeds the solid waste to medium temperature superheater 26 and the gaseous flue gas to high temperature superheater 27;
the waste heat recovery heat exchanger 9 carries out waste heat recovery on the crude gasification product output by the gas-solid separation device 8, and takes the heat as a heat source of the reforming reactor 11;
the discharge port of the waste heat recovery heat exchanger 9 is communicated with the feed port of the impurity removing device 10;
the impurity removing device 10 adopts Selexol technology to desulfurate gasification products, removes acid gas in crude synthesis gas, and then conveys the raw synthesis gas to the reforming reactor 11;
the high-temperature heat exchanger 32 inputs steam into the reforming reactor 11 to be used as a reactant of the reforming reaction;
the discharge port of the reforming reactor 11 is communicated with a synthesis gas heat exchanger 12, and the synthesis gas heat exchanger 12 sends clean synthesis gas subjected to reforming reaction and change reaction into a pressure swing adsorption device 13; the unit is used for cooling the crude synthetic gas product from the coal partial gasification unit, removing acid gas and liquid in the synthetic gas, and sequentially utilizing steam methane reforming reaction and CO change reaction to enable steam to react with methane to generate CO and H 2 And CO 2 And adjusting CO and H in the synthesis gas after reforming reaction 2 Proportion is increased by H 2 Yield.
The reforming reactor was operated at 780℃and at a pressure of 3.69MPa. The pressure swing adsorption unit utilizes the difference of gasifying agents to different gas adsorption rates under different pressures to realize the separation of hydrogen and carbon dioxide, methane and other polluted gases.
The operation temperature and pressure of the pressure swing adsorption device are 35 ℃ and 2MPa respectively, hydrogen with the purity of 99% is obtained, and the hydrogen is pressurized to 6MPa by a hydrogen compressor, so that the pressure swing adsorption device is convenient to store.
The pressure swing adsorption unit comprises a pressure swing adsorption device 13, a hydrogen compressor 14, a hydrogen storage device 15, an exhaust gas heat exchanger 16, a gas product purifying and reforming unit and CO 2 The trapping units are communicated.
The pressure swing adsorption device 13 separates hydrogen in the clean synthesis gas and sends the hydrogen to the hydrogen compressor 14 for pressurization, and the hydrogen compressor 14 sends the pressurized hydrogen to the hydrogen storage device 15 for preservation; the synthesis gas waste gas after hydrogen removal is sent to a waste gas heat exchanger 16;
the off-gas heat exchanger 16 feeds off-gas to a flash reactor 17; after the water in the waste gas is discharged from the flash evaporation reactor 17, the dry waste gas is sent to a waste gas multistage compressor 18 for pressurization and then is led into a waste gas purification device 19, and after washing, NO is converted into HNO in the process of removing NOx 3 Separating the carbon dioxide from the remaining acidic solution;
the waste gas purification device 19 sends the waste gas after washing into a carbon dioxide heat exchanger 20, and the waste gas is sent to a waste gas distillation tower 21 through the carbon dioxide heat exchanger 20; the offgas distillation column 21 separates the inputted offgas into CO2 and the remaining gas, and then feeds the CO2 and the remaining gas into the carbon dioxide heat exchanger 20.
The carbon dioxide heat exchanger 20 pressurizes a part of carbon dioxide by the carbon dioxide compressor 22 and then sends the pressurized carbon dioxide to the carbon dioxide storage device 23 for storage; the other part of the carbon dioxide is sent into a pressurized circulating fluidized bed gasifier 6;
the high-temperature steam of the medium-pressure steam turbine 29 exchanges heat with water from the water pump 34 in the low-temperature heat exchanger 33, and then is sent into the high-temperature heat exchanger 32 through the low-temperature heat exchanger 33;
the high temperature heat exchanger 32 receives the steam from the low temperature heat exchanger 33 and the steam from the high pressure steam turbine 28, and after mixing, a part of the steam is sent to the economizer 35, and a part of the steam is sent to the reforming reactor 11;
the economizer 35 exchanges heat between the steam from the high temperature heat exchanger 32 and the high temperature flue gas from the low temperature reheater 36, and the steam is heated to 290 ℃.
The economizer 35 conveys the heat exchanged flue gas to the waste gas heat exchanger 16 and conveys the heat exchanged water vapor to the pressurized circulating fluidized bed combustion furnace 24; and the pressurized circulating fluidized bed combustion furnace 24 outputs water vapor to the low-temperature superheater 25 to realize water vapor circulation.
The medium-temperature superheater 26 receives the high-temperature solid waste output from the cyclone 38 and the steam discharged from the low-temperature superheater 25; in the intermediate-temperature superheater 26, after the solid waste heats the water vapor to superheat the water vapor, the intermediate-temperature superheater 26 sends the water vapor to the high-temperature superheater 27, and outputs the solid waste to the low-temperature superheater 25; the solid waste is sent into a pressurized circulating fluidized bed combustion furnace 24 through a low-temperature superheater 25; specifically, the feeding port of the low-temperature superheater 25 is respectively communicated with the water cooling wall of the pressurized circulating fluidized bed combustion furnace 24 in the semicoke combustion unit to obtain water vapor, and is communicated with the medium-temperature superheater to obtain solid waste, and the discharging port of the low-temperature superheater 25 is communicated with the feeding port of the pressurized circulating fluidized bed combustion furnace 24 to convey the circulating solid waste.
The high-temperature superheater 27 further superheats the high-temperature steam input by the medium-temperature superheater 26 to 560 ℃ and 24.2MPa by using the high-temperature gaseous flue gas provided by the cyclone separator 38, outputs the high-temperature steam to the high-pressure steam turbine 28, and the steam expands in the high-pressure steam turbine to do work to output power, and the steam state of a discharge port is 4MPa. Providing gaseous flue gas to the high temperature reheater 37;
the high pressure steam turbine 28 delivers high temperature steam to the high temperature heat exchanger 32 and the low temperature reheater 36;
the low-temperature reheater 36 further heats the high-temperature steam passing through the low-temperature reheater 36 by using the high-temperature gaseous flue gas conveyed by the high-temperature reheater 37, and conveys the high-temperature steam to the high-temperature reheater 37; in the high temperature reheater 37, the gaseous flue gas reheates the steam, and the steam discharge port state is 560 ℃ and 4MPa.
The high temperature reheater 37 supplies reheated steam to the intermediate pressure steam turbine 29, and outputs gaseous flue gas to the low temperature reheater 36; the steam expands in the medium pressure steam turbine 29 to do work and output power, and the steam state of a discharge port of the medium pressure steam turbine is 2MPa;
the intermediate pressure steam turbine 29 is communicated with the low temperature heat exchanger 33, the other branch is communicated with the low pressure steam turbine 30, and the discharge port of the low pressure steam turbine 30 is communicated with the feed port of the condenser 31; the steam expands in the medium-pressure steam turbine to do work and output power, and the steam state of the discharge port is 2MPa. The steam expands in the low-pressure steam turbine 30 to do work and output electric power, and the steam state of the discharge port is 0.75MPa.
The water vapor is cooled to be liquid in the condenser 31, and is sent to the low-temperature heat exchanger 33 through the water pump 34 to circulate; the water pump 34 may also supply water directly to the cryogenic heat exchanger 33.
Example 1
As shown in fig. 1, coal powder enters a pressurized circulating fluidized bed gasifier 6 through a coal drying and purifying device 7 to undergo partial gasification reaction with a selected gasifying agent (oxygen/circulating flue gas carbon dioxide), and partial gasification products comprise crude synthesis gas and unvaporized semicoke;
the pressurized circulating fluidized bed gasifier 6 products are passed through a gas-solid separation device 8 to separate the gas products from the solid products. The synthesis gas is subjected to sensible heat recovery through a waste heat recovery heat exchanger 9, cooled and enters a impurity removing device 10, and the crude synthesis gas is desulfurized by using a Selexol technology and is used for removing H in the crude synthesis gas 2 S and other acid gases, the subsequent equipment is prevented from being corroded, and clean synthesis gas is obtained;
the post-synthesis gas sequentially passes through a reforming reactor 11, and steam reacts with methane to generate CO and H by reforming reaction and CO change reaction 2 And CO 2 Regulating CO and H in the synthesis gas after reforming reaction 2 Proportion is increased by H 2 Yield.
The synthesis gas is sent to a pressure swing adsorption device 13 for separating CH 4 、H 2 And CO 2 Isogas, purification of H 2 The H obtained 2 Delivering into a hydrogen compressor 14 for pressurization, and then delivering into a hydrogen storage device 15 for storage to obtain 99% H 2 The method comprises the steps of carrying out a first treatment on the surface of the The waste gas separated by the pressure swing adsorption device 13 is converged with the flue gas from the economizer 35, then water vapor is removed by the flash evaporation reactor 17, the acid solution is removed by the waste gas purification device 19 after being pressurized by the waste gas multistage compressor 18, and then carbon dioxide and other nitrogen oxides are separated by the waste gas heat exchanger 20 and the waste gas distillation tower 21, so that high-purity carbon dioxide is obtained, and the high-purity carbon dioxide is sent to the carbon dioxide storage device 23 after being pressurized by the carbon dioxide compressor 22.
The high-purity oxygen required by the pressurized circulating fluidized bed gasification furnace 6 and the pressurized circulating fluidized bed combustion furnace 24 comes from an air separation oxygen generation unit; the air enters an air compressor 1, passes through an air heat exchanger 2, then respectively enters an air low-pressure distillation tower 3 and an air high-pressure distillation tower 4, separates the oxygen in the air from the rest waste gases such as nitrogen, and respectively enters the air heat exchanger 2 to cool and separate the oxygen, and then passes through an oxygen heater 5 to preheat the oxygen entering a pressurized circulating fluidized bed gasifier 6 and a pressurized circulating fluidized bed combustion furnace 24.
Semi-coke in partial gasified products is separated by a gas-solid separation device and then is sent into a pressurized circulating fluidized bed combustion furnace 24 for pressurized oxygen-enriched combustion, the combustion pressure is consistent with that of the gasification furnace, the generated high-temperature flue gas is separated from combustion waste materials by a cyclone separator 38, and the high-temperature solid waste materials are sent back into the pressurized circulating fluidized bed combustion furnace 24 after being heated by a medium-temperature superheater 26 and a low-temperature superheater 25 in sequence and cooled by high-temperature steam.
The high temperature flue gas is cooled after being heated by the high temperature superheater 27, the high temperature reheater 37, the low temperature reheater 36 and the economizer 35 in sequence, and part of the high temperature flue gas is sent into CO 2 The trap unit is combined with the waste gas separated by pressure swing adsorption to perform carbon trapping, and the other part is returned to the pressurized circulating fluidized bed combustion furnace 24 to perform carbon dioxide circulation.
The coal partial gasification circulating working medium is circulating CO 2 In CO 2 In the trapping unit, the CO is partially purified after the operations of drying, compressing, cleaning, distilling and the like 2 The mixture is sent back to the pressurized circulating fluidized bed gasifier 6 through the carbon dioxide heat exchanger 20 to be used as a circulating reaction working medium to participate in partial gasification reaction;
the water vapor is taken as a circulating working medium of the steam Rankine cycle power generation unit, water is pressurized to 22.4MPa by a water pump 34 under normal temperature and pressure and enters a circulating system, the water is sequentially mixed with exhaust gas from a medium-pressure steam turbine 29 and exhaust gas from a high-pressure steam turbine 28 by a low-temperature heat exchanger 33 and a high-temperature heat exchanger 32 respectively, and is sequentially heated by an economizer 35 and a water cooling wall to become high-temperature high-pressure water vapor, and then sequentially enters a low-temperature superheater 25, a medium-temperature superheater 26 and a high-temperature superheater 27 to become high-pressure superheated water vapor, the high-pressure superheated water vapor enters the high-pressure steam turbine 28 to push turbine blades to do work and generate power, and the exhaust gas sequentially enters a low-temperature reheater 36 and a high-temperature reheater 37 to become superheated water vapor;
the superheated steam sequentially passes through the medium-pressure steam turbine 29 and the low-pressure steam turbine 30 to perform power generation, and the exhausted gas enters the condenser 31 to be cooled into liquid water which is combined with the feed water and then pressurized by the water pump 34 to enter the steam cycle power generation unit.
The steam reactants required by the reforming reactor 11 in the gasification product purification and reforming unit are exhausted from one of the discharge ports of the high temperature heat exchanger 32 in the steam rankine cycle power generation unit.
The invention adopts the pressurized circulating fluidized bed as a reactor for partial gasification of coal and pressurized oxygen-enriched combustion of semicoke, adopts pure oxygen and circulating flue gas carbon dioxide as gasification atmosphere, and has the characteristics of moderate carbon conversion rate in gasification reaction, high system energy utilization efficiency, high hydrogen production efficiency and high hydrogen-electricity ratio. The hydrogen and electricity produced by the system are ideal green energy carriers, and can be directly used for production and living. The pulverized coal is sent into a gasification furnace to be subjected to partial gasification reaction with a gasifying agent to generate synthesis gas and semicoke products, and the synthesis gas and the semicoke products are respectively sent into a gasification product purifying and reforming unit to be purified and reformed and a semicoke pressurized oxygen-enriched combustion unit to be combusted.
Pure oxygen is provided by an air separation oxygen production unit, carbon dioxide is provided by a carbon dioxide capturing unit, a pressurized circulating fluidized bed is adopted for semicoke combustion, a pressurized oxygen-enriched combustion technology is utilized, the carbon dioxide capturing cost generated by semicoke combustion is low, carbon dioxide is separated from hydrogen, high-purity carbon dioxide is obtained, and zero emission of carbon dioxide is easy.
Secondly, the gasification product purifying and reforming unit adopts steam methane reforming reaction and CO change reaction to enable steam and methane to react to generate CO and H 2 And CO 2 And adjusting CO and H in the synthesis gas after reforming reaction 2 Proportion is increased by H 2 Yield.
And finally, a discharge port branch of a high-temperature heat exchanger in the steam Rankine cycle power generation unit is communicated with a gasification product purification and reforming reactor in the reforming unit, high-temperature steam is provided for the gasification product purification and reforming reactor as reaction gas, and waste heat of the synthesis gas is used as a heat source to heat the steam participating in the reforming reaction.
The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof.

Claims (10)

1. A hydrogen and electricity combined production system coupling coal partial gasification and semicoke pressurized oxygen-enriched combustion is characterized by comprising an air separation oxygen production unit, a coal partial gasification unit, a semicoke pressurized oxygen-enriched combustion unit, a gasification product purification and reforming unit, a pressure swing adsorption unit, a steam Rankine cycle power generation unit and CO 2 A trapping unit;
the air separation oxygen production unit is used for conveying oxygen to the coal partial gasification unit and the semicoke pressurized oxygen-enriched combustion unit;
the coal partial gasification unit performs coal partial gasification reaction, the crude synthesis gas is sent to the gasification product purification and reforming unit, and the semicoke of the solid product is sent to the semicoke combustion unit;
the semicoke pressurized oxygen-enriched combustion unit respectively obtains pure oxygen, semicoke and recirculated flue gas from the air separation oxygen production unit, the coal partial gasification unit and the steam Rankine cycle power generation unit, performs combustion reaction, and performs gas-solid separation on combustion products;
the semicoke pressurized oxygen-enriched combustion unit provides high-temperature water vapor for the steam Rankine cycle power generation unit, and the steam Rankine cycle power generation unit provides low-temperature water vapor for the semicoke pressurized oxygen-enriched combustion unit to realize water vapor circulation;
the gasification product purifying and reforming unit sends clean synthesis gas subjected to reforming reaction and change reaction into the pressure swing adsorption unit;
the pressure swing adsorption unit separates and stores hydrogen in the clean synthesis gas, and sends the synthesis gas waste gas after hydrogen removal into the CO 2 And a trapping unit.
2. The combined hydrogen and electricity production system for coupling coal partial gasification and semicoke pressurized oxygen-enriched combustion according to claim 1, wherein the coal partial gasification unit comprises a pressurized circulating fluidized bed gasification furnace (6), a coal drying and purifying device (7) and a gas-solid separation device (8);
the pulverized coal is dried and purified by a coal drying and purifying device (7) and then is sent into a pressurized circulating fluidized bed gasifier (6); oxygen is conveyed to the pressurized circulating fluidized bed gasifier (6) by an oxygen heater (5); the CO 2 A carbon dioxide heat exchanger (20) in the capturing unit provides CO for the pressurized circulating fluidized bed gasifier (6) 2 Partial gasification reaction of coal occurs in the pressurized circulating fluidized bed gasifier (6);
the reaction product of the pressurized circulating fluidized bed gasifier (6) is sent to the gas-solid separation device (8) for separation treatment; the gas-solid separation device (8) sends the crude synthesis gas into a waste heat recovery heat exchanger (9) in the gasification product purification and reforming unit, and sends the semicoke of the solid product into a pressurized circulating fluidized bed combustion furnace (24) in the semicoke combustion unit for combustion.
3. The combined hydrogen and power system coupled with partial gasification of coal and pressurized oxyfuel combustion of claim 1, wherein the pressurized oxyfuel combustion unit comprises a pressurized circulating fluidized bed combustion furnace (24) and a cyclone separator (38);
the feed inlet of the pressurized circulating fluidized bed combustion furnace (24) is communicated with an oxygen heater (5) in the air separation oxygen generation unit, a gas-solid separation device (8) in the coal partial gasification unit and an economizer (35) in the steam Rankine cycle power generation unit, so that pure oxygen, semicoke and recirculated flue gas are respectively obtained for combustion reaction;
the pressurized circulating fluidized bed combustion furnace (24) outputs all water vapor to a low-temperature superheater (25) in the steam Rankine cycle power generation unit and outputs all combustion reaction products to a cyclone separator (38) in the semicoke pressurized oxygen-enriched combustion unit;
the cyclone separator (38) carries out gas-solid separation on combustion products in the pressurized circulating fluidized bed combustion furnace (24) to realize separation of gas flue gas and solid waste; the cyclone (38) feeds solid waste to a medium temperature superheater (26) in the steam rankine cycle power unit and gaseous flue gas to a high temperature superheater (27) in the steam rankine cycle power unit.
4. The combined hydrogen and power generation system coupled with partial gasification of coal and pressurized oxygen-enriched combustion of semicoke according to claim 3, wherein the gasification product purification and reforming unit comprises a waste heat recovery heat exchanger (9), a impurity removal device (10), a reforming reactor (11) and a synthesis gas heat exchanger (12);
the waste heat recovery heat exchanger (9) is used for carrying out waste heat recovery on the crude gasification product output by the gas-solid separation device (8) and taking the heat as a heat source of the reforming reactor (11);
the discharge port of the waste heat recovery heat exchanger (9) is communicated with the feed port of the impurity removing device (10);
the impurity removing device (10) is used for desulfurizing gasification products, removing acid gas in the crude synthesis gas and then conveying the crude synthesis gas to the reforming reactor (11);
a high-temperature heat exchanger (32) in the steam Rankine cycle power generation unit inputs water vapor for the reforming reactor (11) to be used as a reactant of a reforming reaction;
the discharge port of the reforming reactor (11) is communicated with a synthesis gas heat exchanger (12), and the synthesis gas heat exchanger (12) sends clean synthesis gas subjected to reforming reaction and change reaction into a pressure swing adsorption device (13) in the pressure swing adsorption unit.
5. The combined hydrogen and power generation system coupled with partial gasification of coal and pressurized oxyfuel combustion of claim 3, wherein the steam rankine cycle power generation unit comprises a low temperature superheater (25), a medium temperature superheater (26), a high temperature superheater (27), a high pressure steam turbine (28), a medium pressure steam turbine (29), a low pressure steam turbine (30), a condenser (31), a high temperature heat exchanger (32), a low temperature heat exchanger (33), a water pump (34), an economizer (35), a low temperature reheater (36) and a high temperature reheater (37);
the medium-temperature superheater (26) receives high-temperature solid waste output by the cyclone separator (38) and steam discharged by the low-temperature superheater (25); in the medium-temperature superheater (26), after the solid waste heats the water vapor to overheat the water vapor, the medium-temperature superheater (26) transmits the water vapor to the high-temperature superheater (27) and outputs the solid waste to the low-temperature superheater (25); feeding solid waste material through said low temperature superheater (25) into said pressurized circulating fluidized bed combustion furnace (24);
the high-temperature superheater (27) further superheats high-temperature steam input by the medium-temperature superheater (26) by utilizing high-temperature gaseous flue gas provided by the cyclone separator (38), outputs the high-temperature steam to the high-pressure steam turbine (28), and provides gaseous flue gas to the high-temperature reheater (37);
the high-pressure steam turbine (28) delivers high-temperature steam to the high-temperature heat exchanger (32) and the low-temperature reheater (36);
the low-temperature reheater (36) further heats high-temperature steam passing through the low-temperature reheater (36) by utilizing high-temperature gaseous flue gas conveyed by the high-temperature reheater (37), and conveys the high-temperature steam to the high-temperature reheater (37);
the high temperature reheater (37) provides reheat steam for the intermediate pressure steam turbine (29) and outputs gaseous flue gas to the low temperature reheater (36);
the medium-pressure steam turbine (29) is communicated with the low-temperature heat exchanger (33), the other branch is communicated with the low-pressure steam turbine (30), and a discharge port of the low-pressure steam turbine (30) is communicated with a feed port of the condenser (31);
the water vapor is cooled into liquid state in a condenser (31), and is sent into a low-temperature heat exchanger (33) through a water pump (34) to form water vapor circulation; the water pump (34) can also supply water directly to the cryogenic heat exchanger (33).
6. The combined hydrogen and electricity generation system coupled with partial gasification of coal and semi-coke pressurized oxygen-enriched combustion according to claim 5, wherein water vapor expands in the high-pressure steam turbine (28) to do work and output power, and the water vapor state of a discharge port of the high-pressure steam turbine (28) is 4MPa;
in the high-temperature reheater (37), the gaseous smoke is used for reheating water vapor, and the state of a water vapor discharge hole of the high-temperature reheater (37) is 560 ℃ and 4MPa;
the steam expands in a medium-pressure steam turbine (29) to do work and output power, and the steam state of a discharge port of the medium-pressure steam turbine (29) is 2MPa;
the steam expands in the low-pressure steam turbine (30) to do work and output power, and the steam state of the discharge port is 0.75MPa.
7. The combined hydrogen and electricity generation system coupled with partial gasification of coal and semi-coke pressurized oxygen-enriched combustion according to claim 4, wherein the pressure swing adsorption unit comprises a pressure swing adsorption device (13), a hydrogen compressor (14), a hydrogen storage device (15) and an exhaust gas heat exchanger (16);
the pressure swing adsorption device (13) separates hydrogen in the clean synthesis gas and sends the hydrogen to the hydrogen compressor (14) for pressurization, and the hydrogen compressor (14) sends the pressurized hydrogen to the hydrogen storage device (15) for preservation; the synthesis gas exhaust after removal of hydrogen is fed to an exhaust gas heat exchanger (16).
8. The combined hydrogen and power generation system coupled with partial gasification of coal and pressurized oxyfuel combustion of claim 7, wherein the CO 2 The trapping unit comprises a flash evaporation reactor (17), an exhaust gas multistage compressor (18), an exhaust gas purifying device (19), a carbon dioxide heat exchanger (20), an exhaust gas distillation tower (21), a carbon dioxide compressor (22) and a carbon dioxide storage device (23);
the pressure swing adsorption device (13) separates hydrogen in the clean synthesis gas and sends the hydrogen to the hydrogen compressor (14) for pressurization, and the hydrogen compressor (14) sends the pressurized hydrogen to the hydrogen storage device (15) for preservation; the synthesis gas waste gas after hydrogen removal is sent to a waste gas heat exchanger (16);
the waste gas heat exchanger (16) sends waste gas into a flash evaporation reactor (17); after the flash evaporation reactor (17) discharges the moisture in the waste gas, the dry waste gas is sent into a waste gas multistage compressor (18) for pressurization and then is led into a waste gas purification device (19), and after washing, NO is converted into HNO in the NOx removal process 3 Separating the carbon dioxide from the remaining acidic solution;
the waste gas purification device (19) sends the waste gas after washing into a carbon dioxide heat exchanger (20), and the waste gas is sent to a waste gas distillation tower (21) through the carbon dioxide heat exchanger (20); the waste gas distillation tower (21) separates the input waste gas into CO 2 And the rest gas are sent into a carbon dioxide heat exchanger (20);
the carbon dioxide heat exchanger (20) pressurizes a part of carbon dioxide through the carbon dioxide compressor (22) and then sends the pressurized carbon dioxide into the carbon dioxide storage device (23) for storage; and the other part of carbon dioxide is sent into the pressurized circulating fluidized bed gasifier (6).
9. The combined hydrogen and electricity generation system coupled with the partial gasification of coal and the pressurized oxygen-enriched combustion of semicoke according to claim 1, wherein the air separation oxygen generation unit comprises an air compressor (1), an air heat exchanger (2), an air low-pressure distillation tower (3), an air high-pressure distillation tower (4) and an oxygen heater (5);
after the air is sent into the air heat exchanger (2) through the air compressor (1) for cooling, the air is respectively conveyed to the low-pressure distillation tower (3) and the air high-pressure distillation tower (4) through the air heat exchanger (2); the air is distilled into O in a distillation tower 2 And N 2 ；
The air high-pressure distillation tower (4) outputs oxygen and nitrogen to the low-pressure distillation tower (3); the low-pressure distillation tower (3) respectively transmits oxygen and nitrogen to the air heat exchanger (2);
the air heat exchanger (2) separates nitrogen by utilizing air, cools and separates oxygen, and sends the obtained high-purity oxygen to the oxygen heater (5); and after the oxygen heater (5) heats the oxygen, the oxygen is respectively sent into the coal partial gasification unit and the semicoke pressurized oxygen-enriched combustion unit.
10. The combined hydrogen and electricity production system for coupling coal partial gasification and semicoke pressurized oxygen-enriched combustion according to claim 2, wherein the operation temperature of the pressurized circulating fluidized bed gasifier (6) is controlled to be 750-1150 ℃, and the operation pressure is controlled to be 1-3MPa.
CN202310632955.8A 2023-05-31 2023-05-31 Hydrogen and electricity combined production system coupling coal partial gasification and semicoke pressurization oxygen-enriched combustion Pending CN117072263A (en)

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