CN111140359A - Solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system - Google Patents
Solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system Download PDFInfo
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- CN111140359A CN111140359A CN201911292851.7A CN201911292851A CN111140359A CN 111140359 A CN111140359 A CN 111140359A CN 201911292851 A CN201911292851 A CN 201911292851A CN 111140359 A CN111140359 A CN 111140359A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 381
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 149
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 149
- 239000003245 coal Substances 0.000 title claims abstract description 91
- 238000002309 gasification Methods 0.000 title claims abstract description 81
- 238000010248 power generation Methods 0.000 title claims abstract description 50
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 210
- 239000007789 gas Substances 0.000 claims abstract description 136
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 106
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 106
- 238000002485 combustion reaction Methods 0.000 claims abstract description 47
- 238000000926 separation method Methods 0.000 claims abstract description 33
- 238000010926 purge Methods 0.000 claims abstract description 25
- 239000001301 oxygen Substances 0.000 claims abstract description 23
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 23
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000001035 drying Methods 0.000 claims abstract description 18
- 238000000746 purification Methods 0.000 claims abstract description 15
- 238000000034 method Methods 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 23
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 239000003546 flue gas Substances 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 6
- 230000005855 radiation Effects 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 claims description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 3
- 239000001760 fusel oil Substances 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 150000003568 thioethers Chemical class 0.000 claims description 2
- 239000002918 waste heat Substances 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 230000005611 electricity Effects 0.000 abstract 1
- 230000002195 synergetic effect Effects 0.000 abstract 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 238000001816 cooling Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
- F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
- C07C29/1518—Multisteps one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/14—Combined heat and power generation [CHP]
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Abstract
The invention discloses a solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system, belonging to the field of clean utilization of coal. The system mainly comprises three subsystems of solar coal gasification, methanol synthesis, zero-emission power generation and the like. And is connected with an oxygen compressor, a synthesis gas compressor and a combustion chamber through an air separation unit and a purification separation device, and the three subsystems are organically connected to form a co-production system. In the system, concentrated solar energy provides energy for the coal gasification process, the generated synthesis gas is sent to a methanol synthesis reactor to synthesize methanol, purge gas at the outlet of the reactor is sent to a combustion chamber to be combusted with oxygen produced by an air separation unit, the purge gas is directly heated to drive supercritical carbon dioxide to generate electricity, and combustion products can be separated from tail gas to realize zero emission; the waste heat in the working process is recycled by heating the circulating working medium, generating steam and drying raw coal. The comprehensive utilization efficiency of energy is improved, and the synergistic development of the graded utilization of coal and clean power generation is realized.
Description
Technical Field
The invention belongs to the field of clean utilization of coal, and particularly relates to a solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system, in particular to a solar-driven coal gasification and methanol synthesis and supercritical carbon dioxide zero-emission power generation integrated cogeneration system.
Background
According to annual data of the national statistical bureau of the people's republic of China, the total energy production amount of China in 2018 is 377000 ten thousand tons of standard coal, wherein the total coal production amount accounts for 69%, the total energy consumption amount is 464000 ten thousand tons of standard coal, wherein the total coal consumption amount accounts for 59%, so that the current energy production and consumption structure in China still takes coal as the main factor, but the coal is directly combusted as fuel for energy supply in power generation and industrial production, the utilization efficiency is low, and the environmental pollution is serious. With the increasing importance on energy safety and environmental protection, clean utilization of coal has become an important research direction at present.
The preparation of methanol by coal gasification is a mature coal clean utilization mode in the coal chemical industry field at present in China. However, the traditional process for preparing methanol by coal gasification has many defects, the energy absorbed in the coal gasification process is supplied by partial coal combustion, the coal conversion rate is reduced, the effective carbon monoxide component in the synthesis gas is consumed in the water gas conversion process, and the waste heat waste material in the coal gasification methanol synthesis process is used for steam cycle power generation with lower parameters, so that the utilization efficiency is low.
Supercritical carbon dioxide power cycle directly heated by oxygen-enriched combustion is a highly-efficient zero-emission power generation technology with great potential in the field of coal power generation. In the power cycle, the gasified clean synthesis gas is combusted with oxygen to heat high-pressure supercritical carbon dioxide, the generated high-temperature and high-pressure flue gas enters a gas turbine to do work to generate power, and the exhaust gas is cooled by a heat regenerator and a cooler to separate moisture in the flue gas. The dehydrated high-concentration carbon dioxide can be conveniently separated from carbon dioxide generated by combustion after being pressurized by a compressor and a pump, and complicated carbon capture equipment is not needed. If solar energy is utilized to supply energy for the coal gasification process and methanol synthesis and supercritical carbon dioxide power cycle deep coupling are adopted, the comprehensive utilization efficiency of energy can be further improved while the coal conversion rate is improved, and more efficient and diversified clean utilization of coal is realized.
In conclusion, the invention provides a solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system, which is expected to further improve the energy utilization efficiency, reduce fossil energy consumption and realize more efficient and diversified clean utilization of coal; the system efficiently couples solar energy gasification, methanol synthesis and supercritical carbon dioxide power generation, abandons the uneconomical water gas conversion process in the traditional methanol synthesis, reasonably and effectively utilizes waste heat and waste materials in the methanol synthesis, realizes the poly-generation of methanol and electric power, and has wide application prospect in the field of clean utilization of coal.
Disclosure of Invention
The invention aims to provide a solar drive coal gasification methanol synthesis and zero-emission power generation cogeneration system, which comprises three subsystems of solar coal gasification, methanol synthesis and zero-emission power generation; it is characterized in that the preparation method is characterized in that,
the solar coal gasification subsystem is connected in series with a solar gasification furnace, a carbon dioxide heater, a steam generator, a synthetic gas cooler and a purification and separation device through a pre-drying device; the steam generator is connected with the solar gasification furnace; the air separation unit is connected with the pre-drying device; solar energy is projected onto the reflecting tower through the heliostat and then condensed to the solar gasification furnace to form a solar coal gasification subsystem;
the methanol synthesis subsystem comprises a synthesis gas compressor, a synthesis gas preheater cold flow section, a methanol synthesis reactor, a synthesis gas preheater hot flow section, a methanol preheater hot flow section, a cooler, a gas-liquid separator liquid outlet, a methanol preheater cold flow section, a methanol rectification device, a methanol cooler and a methanol storage tank which are connected in series; the methanol synthesis reactor is connected with a built-in heat exchanger of the reactor to form a methanol synthesis subsystem;
the zero-emission power generation subsystem is connected with the combustion chamber through a gas outlet of the gas-liquid separator and a purge gas compressor; the combustion chamber is connected with a gas turbine, a heat flow section of a carbon dioxide heat regenerator, a flue gas cooler, a water separator, a carbon dioxide compressor, an intercooler, a carbon dioxide pump, a cold flow section of the carbon dioxide heat regenerator and a carbon dioxide heater in series to form a loop; the reactor is internally provided with a heat exchanger which is connected with a cold flow section of a carbon dioxide heat regenerator, and the gas turbine is connected with a generator; the oxygen compressor is connected with the combustion chamber to form a zero-emission power generation subsystem;
the air separation unit is connected with the combustion chamber through an oxygen compressor; the purification and separation device is connected with the synthesis gas compressor and the gas-liquid separator, and a gas outlet of the gas-liquid separator is connected with the combustion chamber through the purge gas compressor; thereby organically connecting the three subsystems into a co-production system.
In the co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, in a solar coal gasification subsystem, raw coal enters a pre-drying device for drying treatment, the dried coal enters a solar gasification furnace and is subjected to gasification reaction with steam from a steam generator, after the reaction, crude synthesis gas sequentially passes through a carbon dioxide heater, the steam generator and a synthesis gas cooler, the temperature is reduced to normal temperature, the normal-temperature crude synthesis gas enters a purification and separation device to remove impurity sulfides and water in the crude synthesis gas and then is sent to a methanol synthesis subsystem;
in the methanol synthesis subsystem, purified synthesis gas after impurity removal is pressurized by a synthesis gas compressor, then is heated by a synthesis gas preheater and enters a methanol synthesis reactor to react to generate methanol, and the reacted gas is cooled by the synthesis gas preheater, the methanol preheater and a cooler in sequence and then enters a gas-liquid separator to separate crude methanol and unreacted synthesis gas; the crude methanol is preheated by a methanol preheater and then enters a methanol rectifying device for rectifying to remove water and fusel oil, and the obtained refined methanol is cooled by a methanol cooler and then enters a methanol storage tank for storage; part of unreacted synthesis gas discharged by the gas-liquid separator is used as circulating gas to be converged with synthesis gas from the purification and separation device, and the synthesis gas is pressurized by a synthesis gas compressor and then enters the methanol synthesis reactor again for reaction;
in the zero-emission power generation subsystem, the rest unreacted synthesis gas discharged by the gas-liquid separator is used as purge gas and is compressed by a purge gas compressor and then enters a combustion chamber, the purge gas and high-pressure pure oxygen from an air separation unit are combusted in the combustion chamber to heat supercritical carbon dioxide from a carbon dioxide heater, the generated high-temperature high-pressure gas enters a gas turbine to do work and drive a generator to generate power, the generated high-temperature exhaust gas is sequentially cooled by a carbon dioxide heat regenerator and a flue gas cooler, moisture in the flue gas is condensed and separated by a water separator, the dehydrated high-concentration carbon dioxide is compressed by the carbon dioxide compressor, an intercooler is cooled to form high-density supercritical carbon dioxide, a part of the high-density supercritical carbon dioxide is separated and stored after being boosted by a carbon dioxide pump, and the rest unreacted synthesis; part of carbon dioxide pumped out by the cold flow section of the carbon dioxide heat regenerator enters a built-in heat exchanger of the reactor to absorb heat released by methanol synthesis, and then is pumped into the carbon dioxide heat regenerator to continuously absorb heat, and after the temperature is raised, supercritical carbon dioxide enters a combustion chamber to adjust the combustion temperature after being further heated by a carbon dioxide heater;
air enters an air separation unit to separate high-purity oxygen, the oxygen is pressurized by an oxygen compressor and then enters a combustion chamber to support combustion, and the rest high-temperature nitrogen enters a pre-drying device to dry raw coal; solar radiation energy is projected onto the reflecting tower through the heliostat and is reflected and gathered to the solar gasification furnace through the reflecting tower to drive the gasification reaction of coal.
According to the co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, solar radiation energy is collected to a solar gasification furnace through a heliostat and a reflection tower to provide heat for the gasification reaction of coal, and the gasification temperature is maintained at about 1100 ℃; the high-temperature crude synthesis gas is subjected to heat recovery through a carbon dioxide heater and a steam generator in sequence, and the temperature of the high-temperature crude synthesis gas is reduced to 90 ℃.
According to the co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, the purge gas is compressed by the purge gas compressor and then enters the combustion chamber to be combusted with the high-pressure oxygen from the air separation unit, and the supercritical carbon dioxide is heated to drive the gas turbine to do work.
According to the co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, part of high-pressure carbon dioxide is extracted from the cold flow section of the carbon dioxide heat regenerator, enters the built-in heat exchanger of the reactor to absorb heat released by methanol synthesis, and then is injected into the carbon dioxide heat regenerator to continuously absorb heat, so that the reaction temperature in the methanol synthesis reactor is controlled.
According to the co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, after high-concentration carbon dioxide is pressurized to 30MPa by a carbon dioxide pump, carbon dioxide generated by combustion of synthesis gas is separated, and other carbon capture units are not required to be added.
The invention has the advantages that the overall energy utilization efficiency is improved through the efficient coupling between the solar coal gasification, the methanol synthesis and the supercritical carbon dioxide power generation, the co-production of the methanol preparation from coal and the zero emission power generation in the field of clean utilization of coal is realized, and the process has the following characteristics:
(1) the gathered high-temperature solar energy is used for coal gasification, so that partial combustion of coal can be avoided, the conversion rate of the coal is improved, the ratio of hydrogen to carbon monoxide in the synthesis gas is improved, and the synthesis of methanol is facilitated.
(2) The uneconomical water gas conversion process in the traditional methanol synthesis is removed, carbon monoxide gas in the methanol synthesis is excessive, the excessive carbon monoxide after the reaction is used as purge gas to be sent to a combustion chamber for combustion, the zero-emission power generation is driven, the combustion product is directly removed from the circulating cold end, and the zero-emission power generation is realized.
(3) The solar coal gasification, the methanol synthesis and the supercritical carbon dioxide circulating system are deeply coupled, the process waste heat of the air separation unit is used for drying raw coal, the process waste heat of the methanol synthesis and the synthesis gas purification is used for heating the supercritical carbon dioxide and generating steam, the process waste heat is reasonably recovered, and the whole energy utilization efficiency is improved.
(4) The high-efficiency integration of solar coal gasification, methanol synthesis and supercritical carbon dioxide zero-emission power generation is beneficial to realizing the clean utilization of coal in the fields of coal chemical industry and coal power generation, and the utilization way of solar energy is widened.
Drawings
FIG. 1 is a schematic diagram of a solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system.
In the figure: 1-a pre-drying device, 2-a solar gasification furnace, 3-a carbon dioxide heater, 4-a steam generator, 5-a synthesis gas cooler, 6-a purification and separation device, 7-a synthesis gas compressor, 8-a synthesis gas preheater, 9-a methanol synthesis reactor, 10-a reactor built-in heat exchanger, 11-a cooler, 12-a gas-liquid separator, 13-a methanol preheater, 14-a methanol rectification device, 15-a methanol cooler, 16-a methanol storage tank, 17-a purge gas compressor, 18-a combustion chamber, 19-a gas turbine, 20-a generator, 21-a carbon dioxide regenerator, 22-a flue gas cooler, 23-a water separator, 24-a carbon dioxide compressor, 25-an intercooler, 26-carbon dioxide pump, 27-air separation unit, 28-oxygen compressor, 29-heliostat, 30-reflection tower.
Detailed Description
The invention provides a solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system, which is described below by combining with an attached drawing.
The solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system shown in fig. 1 comprises three subsystems of solar coal gasification, methanol synthesis, zero-emission power generation and the like; the system comprises a solar coal gasification subsystem, a pre-drying device 1, a solar gasification furnace 2, a carbon dioxide heater 3, a steam generator 4, a synthesis gas cooler 5 and a purification and separation device 6, wherein the solar coal gasification subsystem is connected in series with the solar gasification furnace; the steam generator 4 is connected with the solar gasification furnace 2; the air separation unit 27 is connected to the pre-drying apparatus 1; solar energy is projected to a reflecting tower 30 through a heliostat 29 and then condensed to a solar gasification furnace 2 to form a solar gasification subsystem;
the methanol synthesis subsystem comprises a synthesis gas compressor 7, a synthesis gas preheater 8 cold flow section, a methanol synthesis reactor 9, a synthesis gas preheater 8 hot flow section, a methanol preheater 13 hot flow section, a cooler 11, a gas-liquid separator 12 liquid outlet, a methanol preheater 13 cold flow section, a methanol rectifying device 14, a methanol cooler 15 and a methanol storage tank 16 which are connected in series to form a loop; the methanol synthesis reactor 9 is connected with a reactor built-in heat exchanger 10 to form a methanol synthesis subsystem;
the zero-emission power generation subsystem comprises a purge gas compressor 17, a combustion chamber 18, a gas turbine 19, a carbon dioxide heat regenerator 21 heat flow section, a flue gas cooler 22, a water separator 23, a carbon dioxide compressor 24, an intercooler 25, a carbon dioxide pump 26, a carbon dioxide heat regenerator 21 cold flow section and a carbon dioxide heater 3 which are connected in series to form a loop; the reactor built-in heat exchanger 10 is connected with a cold flow section of a carbon dioxide heat regenerator 21, and the gas turbine 19 is connected with a generator 20; the oxygen compressor 28 is connected with the combustion chamber 18 to form a zero-emission power generation subsystem;
then connected to the combustor 18 by an air separation unit 27 through an oxygen compressor 28; the purification and separation device 6 is connected with a synthesis gas compressor 7 and a gas-liquid separator 12, and a gas outlet of the gas-liquid separator 12 is connected with a combustion chamber 18 through a purge gas compressor 17; the three subsystems are organically connected to form a solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system.
In the co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, in a solar coal gasification subsystem, air enters an air separation unit 27 to separate high-purity oxygen, the oxygen is pressurized by an oxygen compressor 28 and then enters a combustion chamber 18 to support combustion, and the rest high-temperature nitrogen enters a pre-drying device 1 to dry raw coal; solar radiation energy is projected onto the reflecting tower 30 through the heliostat 29, is reflected and gathered to the solar gasification furnace 2 through the reflecting tower 30, drives the gasification reaction of coal, provides heat for the gasification reaction of coal, and maintains the gasification temperature at about 1100 ℃; the high-temperature crude synthesis gas is subjected to heat recovery through a carbon dioxide heater 3 and a steam generator 4 in sequence, and the temperature of the high-temperature crude synthesis gas is reduced to 90 ℃; raw coal enters a pre-drying device 1 for drying treatment, the dried coal enters a solar gasification furnace 2 to perform gasification reaction with steam from a steam generator 4, the temperature of the reacted crude synthesis gas is reduced to normal temperature through a carbon dioxide heater 3, the steam generator 4 and a synthesis gas cooler 5 in sequence, and the normal-temperature crude synthesis gas enters a purification and separation device 6 to remove impurities such as sulfide, water and the like in the crude synthesis gas and then is sent to a methanol synthesis subsystem;
in the methanol synthesis subsystem, purified synthesis gas after impurity removal is pressurized by a synthesis gas compressor 7, then is heated by a synthesis gas preheater 8 and enters a methanol synthesis reactor 9 to react to generate methanol, and the reacted gas is cooled by the synthesis gas preheater 8, a methanol preheater 13 and a cooler 12 in sequence and then enters a gas-liquid separator 12 to separate crude methanol and a large amount of unreacted synthesis gas; the crude methanol is preheated by a methanol preheater 13 and then enters a methanol rectifying device 14 for rectifying to remove water and fusel oil, and the obtained refined methanol is cooled by a methanol cooler 15 and then enters a methanol storage tank 16 for storage; part of unreacted synthesis gas discharged by the gas-liquid separator 12 is used as recycle gas to be merged with the synthesis gas from the purification and separation device 6, and the merged recycle gas is pressurized by a synthesis gas compressor 7 and then enters the methanol synthesis reactor 9 again for reaction;
in the zero-emission power generation subsystem, the rest unreacted synthesis gas of the gas-liquid separator 12 is used as purge gas and is compressed by a purge gas compressor 17 and then enters a combustion chamber 18, the purge gas and high-pressure pure oxygen from an air separation unit 27 are combusted in the combustion chamber 18 to heat supercritical carbon dioxide from a carbon dioxide heater 3, the generated high-temperature high-pressure fuel gas enters a gas turbine 19 to do work to drive a generator 20 to generate power, the generated high-temperature exhaust gas sequentially passes through a carbon dioxide regenerator 21, cooling by a flue gas cooler 22, condensing moisture in the flue gas, separating by a water separator 23, compressing the dehydrated high-concentration carbon dioxide by a carbon dioxide compressor 24, cooling by an intercooler 25 to form high-density supercritical carbon dioxide, boosting by a carbon dioxide pump 26, separating and sealing a part of the high-density supercritical carbon dioxide, and allowing the rest of the high-density supercritical carbon dioxide to enter a carbon dioxide regenerator 21 to absorb high-temperature exhaust heat; and part of the carbon dioxide extracted by the cold flow section of the carbon dioxide heat regenerator 21 enters the built-in heat exchanger 10 of the reactor to absorb the heat released by methanol synthesis, and then enters the carbon dioxide heat regenerator 21 to continuously absorb heat, and after the temperature is raised, the supercritical carbon dioxide enters the combustion chamber 18 to adjust the combustion temperature after being further heated by the carbon dioxide heater 3.
According to the integrated co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, the purge gas is compressed by the purge gas compressor 17 and then enters the combustion chamber 18 to be combusted with the high-pressure oxygen from the air separation unit 27, and the supercritical carbon dioxide is heated to drive the gas turbine 19 to do work.
According to the integrated co-production method of the solar-driven coal gasification methanol synthesis and zero-emission power generation co-production system, part of high-pressure carbon dioxide is extracted from the cold flow section of the carbon dioxide heat regenerator 21, enters the built-in heat exchanger 10 of the reactor to absorb heat released by methanol synthesis, and then is pumped into the carbon dioxide heat regenerator 21 to continuously absorb heat, so that the reaction temperature in the methanol synthesis reactor 9 is controlled; after the high-concentration carbon dioxide is pressurized to 30MPa by the carbon dioxide pump 26, the carbon dioxide generated by the combustion of the synthesis gas is separated, and other carbon capturing units are not required to be added.
Claims (6)
1. A solar-driven coal gasification methanol synthesis and zero-emission power generation cogeneration system comprises three subsystems of solar coal gasification, methanol synthesis and zero-emission power generation; it is characterized in that the preparation method is characterized in that,
the solar coal gasification subsystem is connected in series with a solar gasification furnace (2), a carbon dioxide heater (3), a steam generator (4), a synthesis gas cooler (5) and a purification and separation device (6) through a pre-drying device (1); the steam generator (4) is connected with the solar gasification furnace (2); the air separation unit (27) is connected with the pre-drying device (1); solar energy is projected to a reflecting tower (30) through a heliostat (29) and then condensed to a solar gasification furnace (2) to form a solar coal gasification subsystem;
the methanol synthesis subsystem comprises a synthesis gas compressor (7), a synthesis gas preheater (8), a cold flow section, a methanol synthesis reactor (9), a synthesis gas preheater (8) heat flow section, a methanol preheater (13) heat flow section, a cooler (11), a gas-liquid separator (12), a methanol preheater (13) cold flow section, a methanol rectifying device (14), a methanol cooler (15) and a methanol storage tank (16) which are connected in series; the methanol synthesis reactor (9) is connected with a reactor built-in heat exchanger (10) to form a methanol synthesis subsystem;
the zero emission power generation subsystem comprises a gas outlet of a gas-liquid separator (12) and a combustor (18) which are connected through a purge gas compressor (17); the combustion chamber (18), the gas turbine (19), the heat flow section of the carbon dioxide regenerator (21), the flue gas cooler (22), the water separator (23), the carbon dioxide compressor (24), the intercooler (25), the carbon dioxide pump (26), the cold flow section of the carbon dioxide regenerator (21) and the carbon dioxide heater (3) are connected in series to form a loop; the heat exchanger (10) arranged in the reactor is connected with the cold flow section of the carbon dioxide heat regenerator (21), and the gas turbine (19) is connected with the generator (20); the oxygen compressor (28) is connected with the combustion chamber (18) to form a zero-emission power generation subsystem;
the air separation unit (27) is in turn connected to the combustion chamber (18) via an oxygen compressor (28); the purification and separation device (6) is also connected with a synthesis gas compressor (7) and a gas-liquid separator (12), and a gas outlet of the gas-liquid separator (12) is connected with a combustion chamber (18) through a purge gas compressor (17); thereby organically connecting the three subsystems into a co-production system.
2. A co-production method of a solar-driven coal gasification methanol synthesis and zero emission power generation co-production system according to claim 1, characterized in that in a solar coal gasification subsystem, raw coal enters a pre-drying device (1) for drying treatment, the dried coal enters a solar gasification furnace (2) to perform gasification reaction with steam from a steam generator (4), after the reaction, the raw synthesis gas passes through a carbon dioxide heater (3), the steam generator (4) and a synthesis gas cooler (5) in sequence, the temperature is reduced to normal temperature, and the normal temperature raw synthesis gas enters a purification and separation device (6) to remove impurity sulfides and water in the raw synthesis gas and then is sent to the methanol synthesis subsystem;
in a methanol synthesis subsystem, purified synthesis gas after impurity removal is pressurized by a synthesis gas compressor (7), heated by a synthesis gas preheater (8) and enters a methanol synthesis reactor (9) to react to generate methanol, and the gas after reaction is cooled by the synthesis gas preheater (8), a methanol preheater (13) and a cooler (12) in sequence and then enters a gas-liquid separator (12) to separate crude methanol and unreacted synthesis gas; the crude methanol is preheated by a methanol preheater (13), enters a methanol rectifying device (14) for rectifying to remove water and fusel oil, and the obtained refined methanol is cooled by a methanol cooler (15) and enters a methanol storage tank (16) for storage; part of unreacted synthesis gas discharged by the gas-liquid separator (12) is used as recycle gas to be merged with synthesis gas from the purification and separation device (6), and the merged recycle gas is pressurized by a synthesis gas compressor (7) and then enters the methanol synthesis reactor (9) again for reaction;
in the zero-emission power generation subsystem, the rest unreacted synthesis gas discharged by the gas-liquid separator (12) is used as purge gas and is compressed by a purge gas compressor (17) and then enters a combustion chamber (18), the purge gas and high-pressure pure oxygen from an air separation unit (27) are combusted in the combustion chamber (18) to heat supercritical carbon dioxide from a carbon dioxide heater (3), the generated high-temperature and high-pressure gas enters a gas turbine (19) to do work and drive a generator (20) to generate power, the generated high-temperature exhaust gas is sequentially cooled by a carbon dioxide regenerator (21) and a flue gas cooler (22), moisture in the flue gas is condensed and separated by a water separator (23), the dehydrated high-concentration carbon dioxide is compressed by a carbon dioxide compressor (24), an intercooler (25) is cooled to form high-density supercritical carbon dioxide, and a part of the high-density supercritical carbon dioxide is separated and sealed after the pressure is increased by a carbon dioxide pump, the rest enters a carbon dioxide regenerator (21) to absorb the heat of high-temperature exhaust; part of carbon dioxide extracted by a cold flow section of the carbon dioxide heat regenerator (21) enters a heat exchanger (10) arranged in the reactor to absorb heat released by methanol synthesis, then the carbon dioxide heat regenerator (21) is driven to continuously absorb heat, and after the temperature is raised, supercritical carbon dioxide enters a combustion chamber (18) to adjust the combustion temperature after being further heated by a carbon dioxide heater (3);
air enters an air separation unit (27) to separate high-purity oxygen, the oxygen is pressurized by an oxygen compressor (28) and then enters a combustion chamber (18) to support combustion, and the rest high-temperature nitrogen enters a pre-drying device (1) to dry raw coal; solar radiation energy is projected to the reflecting tower (30) through the heliostat (29), is reflected and gathered to the solar gasification furnace (2) through the reflecting tower (30), and drives the gasification reaction of coal.
3. The cogeneration method of a solar-driven coal gasification methanol synthesis and zero emission power generation cogeneration system according to claim 2, wherein the solar radiation energy is concentrated to the solar gasification furnace (2) through the heliostat (29) and the reflection tower (30) to provide heat for the gasification reaction of coal, and the gasification temperature is maintained at about 1100 ℃; the high-temperature crude synthesis gas passes through the carbon dioxide heater (3) and the steam generator (4) in sequence for heat recovery, and the temperature of the high-temperature crude synthesis gas is reduced to 90 ℃.
4. The co-production method of the solar-driven coal gasification methanol synthesis and zero emission power generation co-production system according to claim 2, characterized in that the purge gas is compressed by a purge gas compressor (17) and then enters a combustion chamber (18) to be combusted with high-pressure oxygen from an air separation unit (27), and the supercritical carbon dioxide is heated to drive a gas turbine (19) to do work.
5. The co-production method of the solar-driven coal gasification methanol synthesis and zero emission power generation co-production system according to claim 2, characterized in that part of the high-pressure carbon dioxide extracted from the cold flow section of the carbon dioxide regenerator (21) enters the built-in heat exchanger (10) of the reactor to absorb the heat released by methanol synthesis, and then enters the carbon dioxide regenerator (21) to continuously absorb heat, so as to control the reaction temperature in the methanol synthesis reactor (9).
6. The cogeneration method of a solar driven coal gasification methanol synthesis and zero emission power generation cogeneration system according to claim 2, wherein the carbon dioxide generated by the combustion of the synthesis gas is separated after the high concentration carbon dioxide is pressurized to 30MPa by the carbon dioxide pump (26) without adding other carbon capture units.
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