CN114233265A - Coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system and method - Google Patents
Coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system and method Download PDFInfo
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- CN114233265A CN114233265A CN202111679235.4A CN202111679235A CN114233265A CN 114233265 A CN114233265 A CN 114233265A CN 202111679235 A CN202111679235 A CN 202111679235A CN 114233265 A CN114233265 A CN 114233265A
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- pyrolysis
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 212
- 239000003245 coal Substances 0.000 title claims abstract description 191
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 127
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 106
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 106
- 238000011065 in-situ storage Methods 0.000 title claims abstract description 54
- 230000009919 sequestration Effects 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 67
- 239000002918 waste heat Substances 0.000 claims abstract description 49
- 238000012545 processing Methods 0.000 claims abstract description 44
- 238000000926 separation method Methods 0.000 claims abstract description 38
- 238000010248 power generation Methods 0.000 claims abstract description 32
- 238000007789 sealing Methods 0.000 claims abstract description 27
- 238000004064 recycling Methods 0.000 claims abstract description 19
- 238000002347 injection Methods 0.000 claims description 99
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- 238000010521 absorption reaction Methods 0.000 claims description 36
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 239000012716 precipitator Substances 0.000 claims description 19
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- 230000003647 oxidation Effects 0.000 claims description 18
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- 238000009833 condensation Methods 0.000 claims description 17
- 230000005494 condensation Effects 0.000 claims description 17
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- 239000001257 hydrogen Substances 0.000 claims description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims description 15
- 239000011280 coal tar Substances 0.000 claims description 14
- 230000018044 dehydration Effects 0.000 claims description 14
- 238000006297 dehydration reaction Methods 0.000 claims description 14
- 150000001412 amines Chemical class 0.000 claims description 13
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- 230000008569 process Effects 0.000 claims description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 9
- 239000002608 ionic liquid Substances 0.000 claims description 9
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 claims description 8
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 7
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 6
- 230000005611 electricity Effects 0.000 claims description 6
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- RPNUMPOLZDHAAY-UHFFFAOYSA-N Diethylenetriamine Chemical compound NCCNCCN RPNUMPOLZDHAAY-UHFFFAOYSA-N 0.000 claims description 4
- -1 amine cation Chemical class 0.000 claims description 4
- 150000001450 anions Chemical class 0.000 claims description 4
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 claims description 4
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 4
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- PNGLEYLFMHGIQO-UHFFFAOYSA-M sodium;3-(n-ethyl-3-methoxyanilino)-2-hydroxypropane-1-sulfonate;dihydrate Chemical compound O.O.[Na+].[O-]S(=O)(=O)CC(O)CN(CC)C1=CC=CC(OC)=C1 PNGLEYLFMHGIQO-UHFFFAOYSA-M 0.000 claims description 3
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 229910052799 carbon Inorganic materials 0.000 description 10
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
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- KXGFMDJXCMQABM-UHFFFAOYSA-N 2-methoxy-6-methylphenol Chemical compound [CH]OC1=CC=CC([CH])=C1O KXGFMDJXCMQABM-UHFFFAOYSA-N 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
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- 239000000203 mixture Substances 0.000 description 1
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- 229920001568 phenolic resin Polymers 0.000 description 1
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- 230000000135 prohibitive effect Effects 0.000 description 1
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- 239000011435 rock Substances 0.000 description 1
- 238000002390 rotary evaporation Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Images
Classifications
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/295—Gasification of minerals, e.g. for producing mixtures of combustible gases
-
- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/14—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 absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
- B65G5/00—Storing fluids in natural or artificial cavities or chambers in the earth
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/04—Working-up tar by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/20—Refining by chemical means inorganic or organic compounds
- C10C1/205—Refining by chemical means inorganic or organic compounds refining in the presence of hydrogen
-
- 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
-
- 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
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
- E21B43/241—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection combined with solution mining of non-hydrocarbon minerals, e.g. solvent pyrolysis of oil shale
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/30—Specific pattern of wells, e.g. optimising the spacing of wells
- E21B43/305—Specific pattern of wells, e.g. optimising the spacing of wells comprising at least one inclined or horizontal well
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
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- 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
- F01K11/00—Plants characterised by the engines being structurally combined with boilers or condensers
- F01K11/02—Plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F03—MACHINES OR ENGINES FOR LIQUIDS; WIND, SPRING, OR WEIGHT MOTORS; PRODUCING MECHANICAL POWER OR A REACTIVE PROPULSIVE THRUST, NOT OTHERWISE PROVIDED FOR
- F03G—SPRING, WEIGHT, INERTIA OR LIKE MOTORS; MECHANICAL-POWER PRODUCING DEVICES OR MECHANISMS, NOT OTHERWISE PROVIDED FOR OR USING ENERGY SOURCES NOT OTHERWISE PROVIDED FOR
- F03G7/00—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for
- F03G7/04—Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for using pressure differences or thermal differences occurring in nature
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F24—HEATING; RANGES; VENTILATING
- F24T—GEOTHERMAL COLLECTORS; GEOTHERMAL SYSTEMS
- F24T10/00—Geothermal collectors
- F24T10/20—Geothermal collectors using underground water as working fluid; using working fluid injected directly into the ground, e.g. using injection wells and recovery wells
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E10/00—Energy generation through renewable energy sources
- Y02E10/10—Geothermal energy
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P90/00—Enabling technologies with a potential contribution to greenhouse gas [GHG] emissions mitigation
- Y02P90/70—Combining sequestration of CO2 and exploitation of hydrocarbons by injecting CO2 or carbonated water in oil wells
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- Oil, Petroleum & Natural Gas (AREA)
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- Geology (AREA)
- Combustion & Propulsion (AREA)
- Mining & Mineral Resources (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Fluid Mechanics (AREA)
- General Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Geochemistry & Mineralogy (AREA)
- Analytical Chemistry (AREA)
- Hydrology & Water Resources (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention belongs to the technical field of underground coal pyrolysis, and particularly relates to a system and a method for poly-generation and carbon dioxide sequestration by in-situ coal pyrolysis, which comprises a coal in-situ pyrolysis module, a product separation processing module and a product separation processing module, wherein the coal in-situ pyrolysis module starts pyrolysis of a coal bed and sends pyrolysis products into the product separation processing module; the product separation processing module is used for separating, processing and utilizing the pyrolysis product and sending the pyrolysis gas into the power generation module; the waste heat recycling module is used for generating power by waste heat according to heat remained in the pyrolyzed underground coal bed; the power generation module is used for generating power by depending on the pyrolysis gas separated by the product separation processing module; and the carbon dioxide capturing and sealing module is used for capturing, processing and sealing the carbon dioxide generated in the power generation module and the product separation and processing module. According to the invention, the carbon dioxide generated by the product separation processing module and the power generation module is obtained by the carbon dioxide capture and sealing module and is sealed in the coal bed after pyrolysis, so that the safety of carbon dioxide sealing is improved, and the cost is reduced.
Description
Technical Field
The invention belongs to the technical field of underground coal pyrolysis, and particularly relates to a poly-generation and carbon dioxide sequestration system and method for in-situ coal pyrolysis.
Background
The primary energy distribution pattern of rich coal, poor oil and less gas determines the irreplaceable status of coal in energy consumption of China. In 2020, the proportion of coal in the total primary energy consumption is about 58.3%, and the proportion is increased by 0.6%, so that the main energy position of coal is still difficult to change before the goals of 'carbon peak reaching' and 'carbon neutralization' are realized. If the coal tar after coal pyrolysis can be fully utilized to produce products such as coal-based special fuels, chemical raw materials and the like, the problem of high external dependence of oil and gas resources in China can be effectively solved.
At present, the main coal pyrolysis technology is ground pyrolysis, namely, coal is mined and transported underground, washed, selected and processed and then enters ground pyrolysis equipment to be converted into tar, coal gas and semicoke products. But ground pyrolysis has the problem such as area is big, pyrolysis semicoke productivity is surplus, atmospheric pollution and water pollution, compares in ground pyrolysis, and coal underground in situ pyrolysis has that area is little, the carbon discharges the footprint less, can prevent advantages such as ground collapse, remains a large amount of heats in the underground coal seam after coal in situ pyrolysis in addition, and the coal seam waste heat after the rational utilization pyrolysis generates electricity, can effectively reduce the reliance to traditional fossil fuel electricity generation.
At present, the following two methods are mainly adopted for reducing carbon emission: firstly, a low-cost scheme is sought for reducing the emission of carbon dioxide; secondly, the capture, utilization and sequestration (CCUS) of carbon dioxide is carried out.
Currently, the biggest challenge in developing the CCUS is the cost issue, with the cost of carbon capture being relatively prohibitive at high intensity carbon emissions. Under the prior art condition, the installation of the carbon capture device generates additional capital investment, operation and maintenance cost and the like, in addition, in the process of carbon sequestration, the transportation of carbon dioxide mainly takes a tank car at present, the transportation amount of the tank car is small, the transportation risk is high, the investment of pipe network construction is high, the flexibility is poor, and in addition, if leakage occurs in the transportation, injection and sequestration processes, the influence is caused on the ecological environment and the production activities near the accident. Therefore, the system and the method for coal in-situ pyrolysis poly-generation and carbon dioxide sequestration have important significance for energy development.
Disclosure of Invention
The invention aims to provide a coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system and a method, which aim to solve the technical problems of high cost and easy leakage of the existing carbon dioxide sequestration method.
In order to achieve the purpose, the invention adopts the following technical scheme:
according to the first aspect, the system for poly-generation and carbon dioxide sequestration by in-situ coal pyrolysis comprises a coal in-situ pyrolysis module, a product separation processing module, a waste heat recovery and utilization module, a power generation module and a carbon dioxide capture sequestration module;
the coal in-situ pyrolysis module is used for fracturing an underground coal bed, carrying out in-situ pyrolysis production on the underground coal bed by injecting a high-temperature and high-pressure heat carrier and supplying heat through mild oxidation, and sending a pyrolysis product to the product separation processing module;
the product separation processing module is used for separating, processing and utilizing the pyrolysis product and sending pyrolysis gas in the pyrolysis product into the power generation module;
the waste heat recycling module is used for generating power by waste heat according to heat remained in the pyrolyzed underground coal bed;
the power generation module is used for generating power by depending on the pyrolysis gas separated by the product separation processing module;
and the carbon dioxide capturing and sealing module is used for capturing and processing the carbon dioxide generated in the power generation module and the product separation processing module, transporting the processed carbon dioxide to the coal in-situ pyrolysis module, and injecting the processed carbon dioxide into the pyrolyzed coal bed through a production well or an injection well to perform geological sealing.
The invention is further improved in that: the coal in-situ pyrolysis module comprises a coal seam roof, a coal seam bottom plate, a first injection well, a horizontal well, a second injection well, a production well, a mild oxidation heat supply zone, coal seam cracks, an inner member vortex heat exchange device, a sandstone layer, a pressurizing device, a heating device, an ignition device and a heat exchanger;
the pressure device delivery outlet links to each other with the first input port of heating device, the heating device delivery outlet links to each other with first injection well input port and second injection well input port respectively, be equipped with a plurality of horizontal wells between first injection well export and the second injection well export, horizontal well center department is equipped with the producing well, the producing well delivery outlet links to each other with the input port c of first heat exchanger, the input port d input heat carrier of first heat exchanger, the delivery outlet an of heat exchanger links to each other with heating device's second input port, the delivery outlet b of first heat exchanger links to each other with product separation processing module, first heat exchanger input port c links to each other with delivery outlet b, first heat exchanger input port d links to each other with delivery outlet a, ignition device links to each other with first injection well input port and second injection well input port respectively, first injection well, second injection well, first heat exchanger input port, first heat exchanger, second heat exchanger, the heat exchanger is continuous, The second injection well, the production well and the horizontal well are arranged in a coal seam between a coal seam top plate and a coal seam bottom plate, a plurality of coal seam fractures and mild oxidation heat supply zones are arranged in the coal seam, and the inner component vortex heat exchange device is arranged inside the horizontal well and at the bottom of the first injection well and the bottom of the second injection well.
The invention is further improved in that: the product separation processing module comprises a condensation separator, a dehydration tower, a heating furnace, a hydrofining reactor, a hot high-pressure separator, a hot low-pressure separator, a rectifying tower, a gas washing tower, an absorption tower, an electric tar precipitator and a separator;
the output port b of the first heat exchanger is connected with the input port of the condensation separator, the first output port of the condensation separator is connected with the input port of the dehydration tower, the coal tar is sent into the dehydration tower, the output port of the dehydration tower is connected with the first input port of the heating furnace, the output port of the heating furnace is connected with the first input port of the hydrofining reactor, the output port of the hydrorefining reactor is connected with the input port of the hot high-pressure separator, the first output port of the hot high-pressure separator is connected with the input port of the hot low-pressure separator, the second output port of the thermal high-pressure separator is connected with the second input port of the hydrofining reactor, hydrogen generated in the thermal high-pressure separator is sent into the hydrofining reactor, a first output port of the thermal low-pressure separator discharges residual gas, a second output port of the thermal low-pressure separator is connected with an input port of a rectifying tower, and the rectifying tower outputs fuel oil and chemical raw materials;
the second output port of the condensation separator is connected with the input port of the gas washing tower, pyrolysis gas is sent into the gas washing tower, the output port of the gas washing tower is connected with the input port of the absorption tower, the output port of the absorption tower is connected with the input port of the electrical tar precipitator, the first output port of the electrical tar precipitator is connected with the second input port of the heating furnace, tar in the electrical tar precipitator is sent into the heating furnace, the second output port of the electrical tar precipitator is connected with the first separator, the first output port of the first separator is connected with the third input port of the hydrofining reactor, hydrogen in the first separator is sent into the hydrofining reactor, and the second output port of the first separator is connected with the power generation module.
The invention is further improved in that: the waste heat recycling module comprises a pressure pump, a third heat exchanger, a separator, a steam turbine, a generator, a circulating water pump, a third injection well and a production well;
the utility model discloses a steam turbine, including pressure pump, first delivery outlet, second heat exchanger, turbine, steam turbine, pressure pump output port respectively with the third injection well, the production well delivery outlet links to each other with the second heat exchanger input port, the first delivery outlet of second heat exchanger links to each other with the second separator input port, second heat exchanger second delivery outlet links to each other with the turbine input port, sends steam into the steam turbine, the first delivery outlet of steam turbine links to each other with circulating water pump first input port, turbine second delivery outlet links to each other with the generator input port, the second separator delivery outlet links to each other with circulating water pump second input port.
The invention is further improved in that: the carbon dioxide sealing module comprises a booster pump, a heater, a pressure pump and a carbon dioxide concentration monitor;
the output port of the booster pump is connected with the input port of the heater, the output port of the heater is connected with the input port of the pressure pump, and the output port of the pressure pump is respectively connected with the first injection well, the second injection well and the production well;
the carbon dioxide concentration detector is arranged at the wellhead of the production well, the first injection well and the second injection well.
The invention is further improved in that: the carbon dioxide capturing and sealing module comprises absorption liquid, and the absorption liquid is organic amine ionic liquid;
the organic amine ionic liquid comprises an organic amine cation solution and an acid anion solution;
the organic amine cation solution is prepared by mixing one or more of diethanolamine, methyldiethanolamine, piperazine or diethylenetriamine with ethanolamine;
the acid anion solution is one of hexafluorophosphoric acid, tetrafluoroboric acid, sulfuric acid or acetic acid.
In a second aspect, a coal in-situ pyrolysis poly-generation and carbon dioxide sequestration method comprises the following steps:
s1, fracturing the coal seam through the first injection well and the second injection well to generate coal seam fractures and a mild oxidation heat supply zone in the coal seam, and injecting a propping agent into the coal seam fractures through the first injection well and the second injection well;
s2, arranging inner member vortex heat exchange devices towards the interior of the horizontal well and the bottoms of the first injection well and the second injection well; the ignition device controls the mild oxidation heat supply zone to burn, so as to heat up the coal bed to be pyrolyzed;
s3, generating a high-temperature and high-pressure heat carrier through a pressurizing device and a heating device, injecting the high-temperature and high-pressure heat carrier into the coal bed through a first injection well and a second injection well, and starting in-situ pyrolysis of coal underground under the action of the vortex heat exchange device of the inner member and the reinforced heat exchange of a propping agent in the horizontal well;
s4, extracting pyrolysis products through the production well, sending the pyrolysis products into the product separation processing module through the first heat exchanger, and sending heat generated in the pyrolysis process into a heating device through the first heat exchanger to generate high-temperature high-pressure steam to be injected into the coal bed again;
s5, preliminarily separating the pyrolysis product into a coal tar product and a pyrolysis gas product through a condensation separator; the coal tar product is dehydrated by a dehydration tower and then enters a heating furnace for heating, then enters a hydrofining reactor for hydrogenation reaction, the coal tar product leaving the hydrofining reactor firstly enters a thermal high-pressure separator for separating hydrogen and then enters the hydrofining reactor for recycling, then a thermal low-pressure separator is used for separating residual gas, and finally the coal tar product enters a rectifying tower for separation into oil gas products; the pyrolysis gas product is firstly subjected to gas washing absorption treatment through a gas washing tower and an absorption tower, then enters an electric tar precipitator to collect residual tar and is sent into a heating furnace, then the pyrolysis gas product is sent into a first separator to separate hydrogen and residual heat pyrolysis gas, wherein the hydrogen enters a tar hydrofining reactor, and the pyrolysis gas enters a power generation module to generate power;
s6, pumping water into the pyrolyzed coal seam through a third injection well by using a pressure pump, heating by using waste heat of the pyrolyzed coal seam, extracting a waste heat product from a production well, and sending the waste heat product into a second heat exchanger, evaporating the water into high-temperature steam by the second heat exchanger depending on heat in the waste heat product, introducing the high-temperature steam into a steam turbine to drive a generator to generate electricity, introducing the waste heat product in the second heat exchanger into a second separator, separating oil and gas products carried in the waste heat product by the second separator, and introducing the water into a circulating water pump for reuse;
s7, sending carbon dioxide in the power generation module and the product separation module into a carbon dioxide capturing and sealing module, absorbing the carbon dioxide by absorption liquid in the carbon dioxide capturing and sealing module, heating for desorption, collecting carbon dioxide gas, and heating for desorption and recycling the absorption liquid; and processing the collected carbon dioxide gas into a supercritical state by a booster pump and a heater, and injecting the supercritical carbon dioxide into the underground coal seam from the first injection well, the second injection well or the production well through the booster pump for geological sequestration.
The invention is further improved in that: and S2, when a high-temperature high-pressure heat carrier is injected, slowly raising the temperature, and when the whole coal bed reaches a preset temperature, raising the temperature.
The invention is further improved in that: when the temperature of the waste heat product is more than or equal to 100 ℃, the waste heat recycling module normally works, and when the temperature of the waste heat product is lower than 100 ℃, the waste heat recycling module stops working.
The invention is further improved in that: and when the absorption liquid absorbs carbon dioxide and then is heated for desorption, the absorption liquid absorbing the carbon dioxide is heated to 150 ℃ to complete desorption to obtain pure absorption liquid.
Compared with the prior art, the invention at least comprises the following beneficial effects:
1. the coal-based special fuel is obtained by in-situ pyrolysis of coal, so that the problems of shortage of oil and gas resources and high external dependence in China are solved, and the coal-based special fuel is generated by utilizing gas through poly-generation, so that the energy utilization efficiency is improved, the energy consumption is reduced, and the method is a powerful way for realizing clean coal-based energy.
2. According to the invention, the carbon dioxide generated by the system is captured by combining the carbon dioxide capturing and sealing module, geological sealing is carried out through the pyrolyzed coal bed, and the semicoke structure and the geological environment generated after pyrolysis provide natural conditions for carbon sealing, so that the safety of carbon dioxide sealing is improved, the sealing cost is reduced, and the method is an effective means for treating carbon dioxide.
3. The invention utilizes the waste heat of the coal bed after in-situ pyrolysis to generate electricity, thereby reducing the energy consumption of the system.
4. According to the invention, the temperature and oxidation heat supply can be controlled, part of coal beds are combusted, and the rest of coal beds are pyrolyzed by heat released by coal combustion, so that the in-situ pyrolysis efficiency of coal is improved, and the purpose of shortening the construction period is achieved.
5. The invention has the advantages that the internal component vortex heat exchange device plays a role in strengthening heat exchange in the pyrolysis stage of injecting a heat carrier, and plays a role of a static mixer in the carbon dioxide storage stage to strengthen the absorption and storage of carbon dioxide.
6. According to the invention, the carbon dioxide in the process is absorbed by the amine ionic liquid, so that the carbon emission of the system can be effectively reduced, and the amine ionic liquid can be desorbed by heating, so that the absorbent can be recycled, and the cost is reduced.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:
FIG. 1 is a system block diagram of a coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system of the present invention;
FIG. 2 is a schematic structural diagram of a coal in-situ pyrolysis module of the coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system of the present invention;
FIG. 3 is a schematic structural diagram of a product separation processing module of the coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system of the present invention;
FIG. 4 is a schematic structural diagram of a waste heat recycling module of the coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system of the present invention;
FIG. 5 is a schematic structural diagram of a carbon dioxide sequestration module of the coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system of the present invention;
FIG. 6 is a schematic diagram of a well arrangement connection mode of a coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system with a sandstone layer.
In the figure, 1, a coal seam roof; 2. a coal seam; 3. a coal seam floor; 4. a first injection well; 5. horizontal wells; 6. a second injection well; 7. a production well; 8. a mild oxidative heating zone; 9. coal seam cracking; 10. the inner component vortex heat exchange device; 11. a sandstone layer; 12. a pressurizing device; 13. a heating device; 14. an ignition device; 15. a first heat exchanger; 16. a second coal seam; 17. a third coal seam; 18. a second sandstone layer; 20. a product separation processing module; 21. a condensation separator; 22. a dehydration tower; 23. heating furnace; 24. a hydrofining reactor; 25. a hot high pressure separator; 26. a hot low pressure separator; 27. a rectifying tower; 28. a scrubber tower; 29. an absorption tower; 30. an electrical tar precipitator; 31. a first separator; 50. a power generation module; 41. a pressure pump; 42. a second heat exchanger; 43. a second separator; 44. a water circulating pump; 45. a steam turbine; 46. a generator; 47. a third injection well; 48. a production well; 50 a power generation module; 51. a booster pump; 52. a heater; 53. a pressure pump; 54. a carbon dioxide concentration detector.
Detailed Description
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The following detailed description is exemplary in nature and is intended to provide further details of the invention. Unless otherwise defined, all technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention.
Example 1
As shown in fig. 1, a coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system comprises a coal in-situ pyrolysis module, a product separation processing module 20, a waste heat recovery and utilization module, a power generation module 50 and a carbon dioxide capture sequestration module;
the coal in-situ pyrolysis module is used for a production part and is used for fracturing an underground coal bed, the underground coal bed is pyrolyzed in situ by injecting a high-temperature and high-pressure heat carrier and supplying heat through mild oxidation, pyrolysis volatile components generated by coal pyrolysis are extracted to the ground and introduced into the product separation and processing module 20 after being subjected to catalytic regulation and quality improvement in a production well;
the product separation processing module 20 is used for separating, processing and utilizing oil gas products, condensing and separating the oil gas products, carrying out secondary purification processing on tar products, and recycling one part after the gas products are separated and introducing the other part into the power generation module;
the waste heat recycling module is used for generating power by using a large amount of waste heat of the pyrolyzed underground coal bed and supplying energy consumption to the system;
a power generation module 50 for generating power by means of the fuel gas separated by the product separation processing module 20 to supply energy consumption of the whole system;
the carbon dioxide capturing and sealing module comprises a carbon dioxide capturing process flow, a carbon dioxide processing process flow, a pipeline transportation process flow and a carbon dioxide sealing and sealing process flow. The coal pyrolysis device is used for capturing carbon dioxide generated in the power generation module 50, transporting the carbon dioxide to the coal in-situ pyrolysis module through a pipeline after processing, and injecting the carbon dioxide into the coal bed after pyrolysis through a production well or an injection well for geological storage.
As shown in fig. 2, the coal in-situ pyrolysis module comprises a coal seam roof 1, a coal seam 2, a coal seam floor 3, a first injection well 4, a horizontal well 5, a second injection well 6, a production well 7, a mild oxidation heat supply zone 8, coal seam cracks 9, an inner member vortex heat exchange device 10, a sandstone layer 11, a pressurizing device 12, a heating device 13, an ignition device 14 and a heat exchanger 15;
an output port of the pressurizing device 12 is connected with a first input port of a heating device 13, an output port of the heating device 13 is respectively connected with an input port of a first injection well 4 and an input port of a second injection well 6, a horizontal well 5 is arranged between an output port of the first injection well 4 and an output port of the second injection well 6, a production well 7 is arranged at the center of the horizontal well 5, an output port of the production well 7 is connected with an input port c of a first heat exchanger 15, a heat carrier is input into an input port d of the first heat exchanger 15, the heat carrier is water, nitrogen or air, etc., an output port a of the heat exchanger is connected with a second input port of the heating device 13, an output port b of the first heat exchanger 15 is connected with a product separation processing module 20, an input port c of the first heat exchanger is connected with an output port b, an input port d of the first heat exchanger is connected with an output port a, and an ignition device 14 is respectively connected with the input port of the first injection well 4 and the input port of the second injection well 6, the first injection well 4, the second injection well 6, the production well 7 and the horizontal well 5 are arranged in a coal seam between the coal seam roof 1 and the coal seam floor 3, a plurality of coal seam fractures 9 and mild oxidation heat supply zones 8 are arranged in the coal seam 2, and an inner member vortex heat exchange device 10 is arranged inside the horizontal well 5 and at the bottom of the first injection well 4 and the second injection well 6;
the production well 7 is provided with a heat-insulating sleeve device, so that the temperature inside the production well can be ensured to be higher than 360 ℃, and the blockage caused by condensation and adhesion of pyrolysis products on the pipe wall in the product extraction process is prevented.
The inner member vortex heat exchange device 10 is arranged in the first injection well 4, the second injection well 6 and the horizontal well 5, and can strengthen heat carrier heat exchange in a heat carrier injection stage; the static mixer is used in the carbon dioxide sealing stage to strengthen the absorption and sealing of the carbon dioxide.
The energy consumption required by the heating device 13 is provided by clean energy sources such as solar energy, wind energy and the like.
As shown in fig. 3, the product separation processing module 20 includes a condensation separator 21, a dehydration tower 22, a heating furnace 23, a hydrofining reactor 24, a hot high-pressure separator 25, a hot low-pressure separator 26, a rectifying tower 27, a scrubber tower 28, an absorption tower 29, an electrical tar precipitator 30 and a separator 31;
an output port b of the first heat exchanger 42 is connected with an input port of the condensation separator 21, a first output port of the condensation separator 21 is connected with an input port of the dehydration tower 22, coal tar is sent into the dehydration tower 22, an output port of the dehydration tower 22 is connected with a first input port of the heating furnace 23, an output port of the heating furnace 23 is connected with a first input port of the hydrofining reactor 24, an output port of the hydrofining reactor 24 is connected with an input port of the hot high-pressure separator 25, a first output port of the hot high-pressure separator 25 is connected with an input port of the hot low-pressure separator 26, a second output port of the hot high-pressure separator 25 is connected with a second input port of the hydrofining reactor 25, hydrogen generated in the hot high-pressure separator 25 is sent into the hydrofining reactor 25, the first output port of the hot low-pressure separator 26 discharges residual gas, the second output port of the hot low-pressure separator 26 is connected with an input port of the rectifying tower 27, and the rectifying tower 27 outputs fuel oil and chemical raw materials;
a second output port of the condensation separator 21 is connected with an input port of a gas washing tower, pyrolysis gas is sent into the gas washing tower 28, an output port of the gas washing tower 28 is connected with an input port of an absorption tower 29, an output port of the absorption tower 29 is connected with an input port of an electric tar precipitator 30, a first output port of the electric tar precipitator 30 is connected with a second input port of the heating furnace 23, tar in the electric tar precipitator 30 is sent into the heating furnace 23, a second output port of the electric tar precipitator 30 is connected with a first separator 31, a first output port of the first separator 31 is connected with a third input port of the hydrofining reactor 24, hydrogen in the first separator 31 is sent into the hydrofining reactor 24, a second output port of the first separator 31 is connected with a power generation module 50, and the pyrolysis gas is sent into the power generation module 50 for power generation;
as shown in fig. 4, the waste heat recycling module includes a pressure pump 41, a third heat exchanger 42, a separator 43, a steam turbine 45, a generator 46 and a circulating water pump 44;
an output port of the pressure pump 41 is connected with a third injection well 47, an output port of a production well 48 is connected with an input port of a second heat exchanger 42, a first output port of the second heat exchanger 42 is connected with an input port of a second separator 43, a second output port of the second heat exchanger 42 is connected with an input port of a steam turbine 45, secondary steam is sent to the steam turbine 45, a first output port of the steam turbine 45 is connected with a first input port of a circulating water pump 44, a second output port of the steam turbine 45 is connected with an input port of a generator 46, and an output port of the second separator 43 is connected with a second input port of the circulating water pump 44.
The power generation module comprises a gas turbine and a steam turbine.
As shown in fig. 5, the carbon dioxide sequestration module includes a booster pump 51, a heater 52, a pressure pump 53, and a carbon dioxide concentration detector 54;
the output port of the booster pump 51 is connected with the input port of the heater 52, the output port of the heater 52 is connected with the input port of the pressure pump 53, the output port of the pressure pump 53 is connected with the injection well, and the carbon dioxide concentration detector 54 is arranged at each well head.
Example 2
A coal in-situ pyrolysis poly-generation and carbon dioxide sequestration method comprises the following steps:
s1, fracturing the coal seam 2 through the first injection well 4 and the second injection well 6 to generate coal seam fractures 9 and a mild oxidation heat zone 8 in the coal seam 2, and injecting a proppant into the coal seam fractures 9 through the first injection well 4 and the second injection well 6;
s2, arranging an inner member vortex heat exchange device 10 towards the interior of the horizontal well 5 and the bottoms of the first injection well 4 and the second injection well 6; the ignition device 14 controls the mild oxidation heat supply zone to burn, and the coal bed to be pyrolyzed is heated;
s3, generating a high-temperature and high-pressure heat carrier through the pressurizing device 12 and the heating device 13, injecting the high-temperature and high-pressure heat carrier into the coal seam 2 through the first injection well 4 and the second injection well 6, and starting in-situ pyrolysis of coal underground under the action of the internal member vortex heat exchange device 10 and the supporting agent enhanced heat exchange in the horizontal well 5;
s4, extracting pyrolysis products through the production well 7, and sending the pyrolysis products into the product separation processing module 20 through the first heat exchanger 15, wherein the first heat exchanger 15 sends heat generated in the pyrolysis process into the heating device 13 to generate high-temperature high-pressure steam to be injected into the coal seam 2 again;
s5, primarily separating the pyrolysis product into a coal tar product and a pyrolysis gas product through the condensation separator 21; the coal tar product is dehydrated by a dehydrating tower 22 and then enters a heating furnace 23 for heating, then enters a hydrofining reactor 24 for hydrogenation reaction, the coal tar product leaving the hydrofining reactor 24 enters a thermal high-pressure separator 25 for separating hydrogen and then is sent to the hydrofining reactor 24 for recycling, then the residual gas is separated by a thermal low-pressure separator 25, and finally the residual gas enters a rectifying tower 27 for separation into oil gas products; the pyrolysis gas product is firstly subjected to gas washing absorption treatment through a gas washing tower 28 and an absorption tower 29, then enters an electric tar precipitator 30 to collect residual tar and is sent to a heating furnace 23, then the pyrolysis gas product is sent to a first separator 31 to separate hydrogen and residual heat pyrolysis gas, wherein the hydrogen enters a tar hydrofining reactor 24, and the pyrolysis gas enters a power generation module 50 to generate power;
s6, pumping water into the pyrolyzed coal seam 2 through a third injection well 47 by using a pressure pump 41, heating by using waste heat of the pyrolyzed coal seam, extracting a waste heat product from a production well 48, and sending the waste heat product into a second heat exchanger 42, evaporating the water into high-temperature steam by the second heat exchanger 42 depending on heat in the waste heat product, sending the high-temperature steam into a steam turbine 45 to drive a generator 46 to generate electricity, sending the waste heat product in the second heat exchanger 42 into a second separator 43, separating oil and gas products carried in the waste heat product by the second separator 43, and sending the water into a circulating water pump 44 for reuse;
s7, sending carbon dioxide in the power generation module 50 and the product separation module 20 into a carbon dioxide capturing and sealing module, absorbing the carbon dioxide by absorption liquid in the carbon dioxide capturing and sealing module, heating for desorption, collecting carbon dioxide gas, and heating for desorption and recycling the absorption liquid; the collected carbon dioxide gas is processed into a supercritical state by a booster pump 51 and a heater 52, and the supercritical carbon dioxide is injected into the underground coal seam 2 from the first injection well 4, the second injection well 6 or the production well 7 through a pressure pump 53 for geological sequestration.
The preparation method of the proppant comprises the following steps: mixing and grinding a carrier material and red mud, and then carrying out homogenization and refinement treatment to obtain mixed powder, wherein the particle size range of the mixed powder is 0.4-2.0 mm; uniformly mixing the mixed powder with an adhesive, and then feeding the mixture into a granulator for granulation to obtain spherical particles; and drying the pellets and then calcining at the temperature of 1000-1200 ℃ to obtain the proppant for underground in-situ pyrolysis of coal.
The carrier material in the mixed material accounts for 35-60 wt% of the mass of the mixed powder; the red mud accounts for 40 to 65 weight percent of the mass of the mixed powder. The carrier material is one or more of ceramsite, metal aluminum ball and resin coated sand, and the adhesive is one or more of phenolic resin, polyurethane and sodium silicate.
The preparation method of the organic amine ionic liquid comprises the following steps: weighing organic amine and acid with equal molar weight, respectively placing the organic amine and the acid into ice water, stirring and dissolving, slowly adding the acid solution into the organic amine solution after stirring uniformly, then uniformly stirring and reacting, continuously carrying out rotary evaporation at the temperature of 80-100 ℃, and finally drying for 24 hours at the temperature of 60-80 ℃.
The organic amine solution is prepared by mixing one or More of Ethanolamine (MEA), Diethanolamine (DEA), Methyldiethanolamine (MDEA), Piperazine (PZ) and Diethylenetriamine (DETA); the acid solution is one of hexafluorophosphoric acid, tetrafluoroboric acid, sulfuric acid and acetic acid.
When injecting first injection well 4 and second injection well 6 with high temperature high pressure heat carrier, the low-speed intensification earlier, when the temperature of coal seam 2 reached 200 ℃, the heating of beginning rapid heating up improves the initial pyrolysis rate in coal seam, increases pyrolysis tar yield.
The waste heat recycling module generates power by using a large amount of waste heat generated after in-situ pyrolysis of coal, and effectively utilizes energy.
The waste heat recycling module utilizes coal bed waste heat after pyrolysis to heat steam, and the waste heat product can be normally used when the temperature is more than 100 ℃, and can be stopped to be used when the temperature is lower than 100 ℃.
Absorbing carbon dioxide in the power generation module 50 and the product separation processing module by using organic amine ionic liquid as absorption liquid;
the absorbed mixed solution can be desorbed when heated to 150 ℃, and the obtained organic amine ionic liquid absorption liquid can be reused.
And carrying out geological sequestration of supercritical carbon dioxide by utilizing the coal bed after underground pyrolysis, wherein the coal bed after pyrolysis provides natural conditions for sequestration of the carbon dioxide.
And the injection well and the production well in the coal in-situ pyrolysis module are used for injecting supercritical carbon dioxide, so that the construction cost is reduced.
By injecting carbon dioxide, residual pyrolytic gas adsorbed in coal rock and semicoke is removed, the pyrolytic gas is further recovered, and the recovery ratio is improved.
The waste heat of the geological environment after the underground coal pyrolysis is utilized to stabilize the state of the supercritical carbon dioxide and reduce the leakage risk of the carbon dioxide.
Example 3
As shown in fig. 6, a well arrangement mode of a coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system comprises a coal seam roof 1, a coal seam 2, a sandstone layer 11, a second coal seam 16, a second sandstone layer 18, a third coal seam 17, a first injection well 4, a second injection well 6, a horizontal well 5, a production well 7, a coal seam floor 3, a mild oxidation heat supply zone 8 and an inner member vortex heat exchange device 10, wherein the coal seam 2 is arranged below the coal seam roof 1, the sandstone layer 11 is arranged below the coal seam 2, the second coal seam 16 is arranged below the sandstone layer 11, the second sandstone layer 18 is arranged below the second coal seam 16, the third coal seam 17 is arranged below the second sandstone layer 18, the coal seam floor 3 is arranged below the third coal seam 17, the coal seam 5 is arranged in the first coal seam roof 1, the coal seam 2, the sandstone layer 11, the second coal seam 16, the second sandstone layer 18, the third coal seam 17, the production well 7 sequentially pass through the coal seam roof 1, the coal seam 2, the second coal seam 6 and the third coal seam 17, the second coal seam 16 is provided with a mild oxidative heating zone 8, and the sandstone layer 11 and the second sandstone layer 18 are provided with cracks.
The mild oxidation heat supply zone 8 is used for burning part of underground coal seams, controlling the coal burning to generate heat, strengthening the pyrolysis of the rest coal seams, reducing the pyrolysis energy consumption and improving the pyrolysis efficiency;
controlling the middle part of the burning coal bed to heat the rest coal bed aiming at the underground thick coal bed and the thick sandstone layer; and aiming at multiple coal seams and thin sandstone layers, the middle coal seam is controlled to be burnt, and the pyrolysis efficiency of the upper coal seam and the lower coal seam is enhanced.
It will be appreciated by those skilled in the art that the invention may be embodied in other specific forms without departing from the spirit or essential characteristics thereof. The embodiments disclosed above are therefore to be considered in all respects as illustrative and not restrictive. All changes which come within the scope of or equivalence to the invention are intended to be embraced therein.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solutions of the present invention and not for limiting the same, and although the present invention is described in detail with reference to the above embodiments, those of ordinary skill in the art should understand that: modifications and equivalents may be made to the embodiments of the invention without departing from the spirit and scope of the invention, which is to be covered by the claims.
Claims (10)
1. The system is characterized by comprising a coal in-situ pyrolysis module, a product separation processing module (20), a waste heat recycling module, a power generation module (50) and a carbon dioxide capturing and sealing module;
the coal in-situ pyrolysis module is used for fracturing an underground coal bed, carrying out in-situ pyrolysis production on the underground coal bed by injecting a high-temperature and high-pressure heat carrier and supplying heat through mild oxidation, and sending a pyrolysis product into the product separation processing module (20);
the product separation and processing module (20) is used for separating, processing and utilizing the pyrolysis products and sending pyrolysis gas in the pyrolysis products into the power generation module (50);
the waste heat recycling module is used for generating power by waste heat according to heat remained in the pyrolyzed underground coal bed;
the power generation module (50) is used for generating power by means of the pyrolysis gas separated by the product separation processing module (20);
and the carbon dioxide capturing and sealing module is used for capturing and processing the carbon dioxide generated in the power generation module (50) and the product separation processing module (20), transporting the processed carbon dioxide to the coal in-situ pyrolysis module, and injecting the processed carbon dioxide into the pyrolyzed coal bed through a production well or an injection well to carry out geological sealing.
2. The system for poly-generation and carbon dioxide sequestration through in-situ coal pyrolysis as claimed in claim 1, characterized in that the in-situ coal pyrolysis module comprises a coal seam roof (1), a coal seam (2), a coal seam floor (3), a first injection well (4), a horizontal well (5), a second injection well (6), a production well (7), a mild oxidation heat supply zone (8), coal seam fractures (9), an inner member vortex heat exchange device (10), a sand stratum (11), a pressurizing device (12), a heating device (13), an ignition device (14) and a heat exchanger (15);
the pressure device (12) delivery outlet is connected with the first input port of the heating device (13), the delivery outlet of the heating device (13) is respectively connected with the first input port of the first injection well (4) and the second input port of the second injection well (6), a plurality of horizontal wells (5) are arranged between the outlet of the first injection well (4) and the outlet of the second injection well (6), a production well (7) is arranged at the center of the horizontal well (5), the delivery outlet of the production well (7) is connected with the input port c of the first heat exchanger (15), a heat carrier is input into the input port d of the first heat exchanger (15), the delivery outlet a of the heat exchanger is connected with the second input port of the heating device (13), the delivery outlet b of the first heat exchanger (15) is connected with the product separation processing module (20), the input port c of the first heat exchanger is connected with the delivery outlet b, and the input port d of the first heat exchanger is connected with the delivery outlet a, ignition device (14) link to each other with first injection well (4) input port and second injection well (6) input port respectively, first injection well (4), second injection well (6), production well (7) and horizontal well (5) set up in the coal seam between coal seam roof (1) and coal seam bottom plate (3), have a plurality of coal seam fissures (9) and mild oxidation heat supply area (8) in coal seam (2), horizontal well (5) inside and first injection well (4), second injection well (6) bottom are equipped with interior component vortex heat transfer device (10).
3. The coal in-situ pyrolysis poly-generation and carbon dioxide sequestration system according to claim 1, wherein the product separation processing module (20) comprises a condensation separator (21), a dehydration tower (22), a heating furnace (23), a hydrofining reactor (24), a hot high pressure separator (25), a hot low pressure separator (26), a rectifying tower (27), a scrubbing tower (28), an absorption tower (29), an electric tar precipitator (30) and a separator (31);
the output port b of the first heat exchanger (42) is connected with the input port of the condensation separator (21), the first output port of the condensation separator (21) is connected with the input port of the dehydration tower (22), coal tar is sent into the dehydration tower (22), the output port of the dehydration tower (22) is connected with the first input port of the heating furnace (23), the output port of the heating furnace (23) is connected with the first input port of the hydrofining reactor (24), the output port of the hydrofining reactor (24) is connected with the input port of the hot high-pressure separator (25), the first output port of the hot high-pressure separator (25) is connected with the input port of the hot low-pressure separator (26), the second output port of the hot high-pressure separator (25) is connected with the second input port of the hydrofining reactor (25), hydrogen generated in the hot high-pressure separator (25) is sent into the hydrofining reactor (25), and residual gas is discharged from the first output port of the hot low-pressure separator (26), a second output port of the thermal low-pressure separator (26) is connected with an input port of a rectifying tower (27), and the rectifying tower (27) outputs fuel oil and chemical raw materials;
the second output port of the condensation separator (21) is connected with the input port of the scrubber tower (28) to send pyrolysis gas into the scrubber tower (28), the outlet of the scrubber tower (28) is connected with the inlet of the absorption tower (29), the outlet of the absorption tower (29) is connected with the inlet of the electrical tar precipitator (30), the first output port of the electrical tar precipitator (30) is connected with the second input port of the heating furnace (23) to send tar in the electrical tar precipitator (30) into the heating furnace (23), the second output port of the electrical tar precipitator (30) is connected with the first separator (31), a first output port of the first separator (31) is connected with a third input port of the hydrofining reactor (24), hydrogen in the first separator (31) is sent into the hydrofining reactor (24), and a second output port of the first separator (31) is connected with the power generation module (50).
4. The system for coal in-situ pyrolysis poly-generation and carbon dioxide sequestration as claimed in claim 2, wherein the waste heat recovery and utilization module comprises a pressure pump (41), a third heat exchanger (42), a separator (43), a steam turbine (45), a generator (46), a circulating water pump (44), a third injection well (47) and a production well (48);
the delivery outlet of pressure pump (41) respectively with third injection well (47), it links to each other with second heat exchanger (42) input port to adopt well (48) delivery outlet, the first delivery outlet of second heat exchanger (42) links to each other with second separator (43) input port, second heat exchanger (42) second delivery outlet links to each other with steam turbine (45) input port, sends steam into steam turbine (45), the first delivery outlet of steam turbine (45) links to each other with circulating water pump (44) first input port, steam turbine (45) second delivery outlet links to each other with generator (46) input port, second separator (43) delivery outlet links to each other with circulating water pump (44) second input port.
5. The system for poly-generation and carbon dioxide sequestration by in-situ coal pyrolysis according to claim 1, wherein the carbon dioxide sequestration module comprises a booster pump (51), a heater (52), a pressure pump (53) and a carbon dioxide concentration monitor (54);
the output port of the booster pump (51) is connected with the input port of the heater (52), the output port of the heater (52) is connected with the input port of the pressure pump (53), and the output port of the pressure pump (53) is respectively connected with the first injection well (4), the second injection well (6) and the production well (7);
the carbon dioxide concentration detector (54) is arranged at the wellhead of the production well (7), the first injection well (4) and the second injection well (6).
6. The system for poly-generation and carbon dioxide sequestration by in-situ coal pyrolysis according to claim 1, wherein the carbon dioxide capture sequestration module comprises an absorption liquid, and the absorption liquid is an organic amine ionic liquid;
the organic amine ionic liquid comprises an organic amine cation solution and an acid anion solution;
the organic amine cation solution is prepared by mixing one or more of diethanolamine, methyldiethanolamine, piperazine or diethylenetriamine with ethanolamine;
the acid anion solution is one of hexafluorophosphoric acid, tetrafluoroboric acid, sulfuric acid or acetic acid.
7. A coal in-situ pyrolysis poly-generation and carbon dioxide sequestration method is characterized by comprising the following steps:
s1, fracturing the coal seam (2) through the first injection well (4) and the second injection well (6), enabling coal seam fractures (9) and a mild oxidation heat supply zone (8) to be generated in the coal seam (2), and injecting propping agents into the coal seam fractures (9) through the first injection well (4) and the second injection well (6);
s2, arranging an inner component vortex heat exchange device (10) towards the interior of a horizontal well (5) and the bottoms of a first injection well (4) and a second injection well (6); the ignition device (14) is used for controlling the mild oxidation heat supply zone to burn, and the temperature of the coal bed to be pyrolyzed is raised;
s3, generating a high-temperature and high-pressure heat carrier through a pressurizing device (12) and a heating device (13), injecting the high-temperature and high-pressure heat carrier into the coal seam (2) through a first injection well (4) and a second injection well (6), and starting in-situ pyrolysis of coal underground under the enhanced heat exchange action of an inner member vortex heat exchange device (10) and a propping agent in a horizontal well (5);
s4, extracting pyrolysis products through the production well (7), sending the pyrolysis products into the product separation processing module (20) through the first heat exchanger (15), and sending heat generated in the pyrolysis process into the heating device (13) through the first heat exchanger (15) to generate high-temperature high-pressure steam to be injected into the coal seam (2) again;
s5, primarily separating the pyrolysis product into a coal tar product and a pyrolysis gas product through a condensation separator (21); the coal tar product is dehydrated by a dehydrating tower (22), then enters a heating furnace (23) for heating, then enters a hydrofining reactor (24) for hydrogenation reaction, the coal tar product leaving the hydrofining reactor (24) firstly enters a hot high-pressure separator (25) for separating hydrogen and then enters the hydrofining reactor (24) for recycling, then enters a hot low-pressure separator (25) for separating residual gas, and finally enters a rectifying tower (27) for separating oil gas products; the pyrolysis gas product is firstly subjected to gas washing absorption treatment through a gas washing tower (28) and an absorption tower (29), then enters an electric tar precipitator (30) to collect residual tar and is sent to a heating furnace (23), then the pyrolysis gas product is sent to a first separator (31) to separate hydrogen and residual heat pyrolysis gas, wherein the hydrogen enters a tar hydrofining reactor (24), and the pyrolysis gas enters a power generation module (50) to be used for power generation;
s6, pumping water into the pyrolyzed coal seam (2) through a third injection well (47) by using a pressure pump (41), heating by using waste heat of the pyrolyzed coal seam, extracting a waste heat product from a produced well (48), and sending the waste heat product into a second heat exchanger (42), evaporating the water into high-temperature steam by the second heat exchanger (42) depending on heat in the waste heat product, and introducing the high-temperature steam into a steam turbine (45) to drive a generator (46) to generate electricity, introducing the waste heat product in the second heat exchanger (42) into a second separator (43), separating the oil gas product carried in the waste heat product by the second separator (43), and introducing the water into a circulating water pump (44) for reuse;
s7, sending carbon dioxide in the power generation module (50) and the product separation module (20) into a carbon dioxide capturing and sealing module, absorbing the carbon dioxide by absorption liquid in the carbon dioxide capturing and sealing module, heating for desorption, collecting carbon dioxide gas, and heating for desorption and recycling the absorption liquid; the collected carbon dioxide gas is processed into a supercritical state by a booster pump (51) and a heater (52), and the supercritical carbon dioxide is injected into the underground coal seam (2) from the first injection well (4), the second injection well (6) or the production well (7) through a pressure pump (53) for geological sequestration.
8. The method for poly-generation and carbon dioxide sequestration by in-situ coal pyrolysis as claimed in claim 7, wherein when injecting the high-temperature high-pressure heat carrier in S2, the temperature is slowly raised, and when the temperature of the whole coal seam (2) reaches a preset temperature, the temperature raising rate is increased.
9. The coal in-situ pyrolysis poly-generation and carbon dioxide sequestration method according to claim 7, wherein when the temperature of the waste heat product is greater than or equal to 100 ℃, the waste heat recovery module normally works, and when the temperature of the waste heat product is lower than 100 ℃, the waste heat recovery module stops working.
10. The system of claim 7, wherein when the absorption liquid absorbs carbon dioxide and then is heated for desorption, the absorption liquid absorbing carbon dioxide is heated to 150 ℃ to complete desorption, so as to obtain pure absorption liquid.
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