CN115109618A - Low-rank coal and photovoltaic energy cooperative conversion method - Google Patents
Low-rank coal and photovoltaic energy cooperative conversion method Download PDFInfo
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- 239000003245 coal Substances 0.000 title claims abstract description 80
- 238000000034 method Methods 0.000 title claims abstract description 31
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 30
- 239000001257 hydrogen Substances 0.000 claims abstract description 105
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 105
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 85
- 239000007789 gas Substances 0.000 claims abstract description 62
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000000197 pyrolysis Methods 0.000 claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 35
- 238000000605 extraction Methods 0.000 claims abstract description 28
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000000746 purification Methods 0.000 claims abstract description 22
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 21
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 19
- 238000010248 power generation Methods 0.000 claims abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000001301 oxygen Substances 0.000 claims abstract description 13
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 13
- 238000003860 storage Methods 0.000 claims abstract description 13
- 239000002351 wastewater Substances 0.000 claims abstract description 13
- 239000000295 fuel oil Substances 0.000 claims abstract description 11
- 239000003921 oil Substances 0.000 claims abstract description 11
- 230000007062 hydrolysis Effects 0.000 claims abstract description 8
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 8
- 238000002309 gasification Methods 0.000 claims abstract description 3
- 239000011269 tar Substances 0.000 claims description 41
- 150000002431 hydrogen Chemical class 0.000 claims description 30
- 239000000571 coke Substances 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 11
- 230000008569 process Effects 0.000 claims description 10
- 239000003034 coal gas Substances 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000012545 processing Methods 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 7
- 239000011280 coal tar Substances 0.000 claims description 6
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 230000003301 hydrolyzing effect Effects 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 5
- 239000007787 solid Substances 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000008213 purified water Substances 0.000 claims description 4
- 238000007605 air drying Methods 0.000 claims description 3
- 238000004458 analytical method Methods 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 238000011033 desalting Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 238000010791 quenching Methods 0.000 claims description 3
- 230000000171 quenching effect Effects 0.000 claims description 3
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 12
- 230000005611 electricity Effects 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000004484 Briquette Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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Classifications
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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
-
- 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
- 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
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
-
- 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
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- 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
-
- 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
- C10K1/02—Dust removal
- C10K1/028—Dust removal by electrostatic precipitation
-
- 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
- C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
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- H—ELECTRICITY
- H02—GENERATION; CONVERSION OR DISTRIBUTION OF ELECTRIC POWER
- H02J—CIRCUIT ARRANGEMENTS OR SYSTEMS FOR SUPPLYING OR DISTRIBUTING ELECTRIC POWER; SYSTEMS FOR STORING ELECTRIC ENERGY
- H02J7/00—Circuit arrangements for charging or depolarising batteries or for supplying loads from batteries
- H02J7/34—Parallel operation in networks using both storage and other dc sources, e.g. providing buffering
- H02J7/35—Parallel operation in networks using both storage and other dc sources, e.g. providing buffering with light sensitive cells
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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
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
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- Chemical & Material Sciences (AREA)
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- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
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- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention discloses a low-rank coal and photovoltaic energy cooperative conversion method.A photovoltaic power is supplied to a water electrolysis unit and generates oxygen and hydrogen which are respectively used as raw material gases of a low-rank coal pyrolysis unit and a tar hydrogenation and separation unit; the semicoke produced by the lump coal pyrolysis unit is a product, the produced raw gas is treated by a gas purification and hydrogen extraction unit to obtain coal-based hydrogen and purified gas, and the produced crude tar and the foreign raw oil are treated by a purification and phenol extraction unit together to obtain phenol-containing wastewater, low-phenol tar and industrial crude phenol products; the hydrolysis hydrogen and the coal-based hydrogen are mixed and then communicated with a hydrogen storage unit, and the mixed hydrogen and the low-phenol tar are converted in a tar hydrogenation and separation unit to obtain a fuel oil product and non-condensable gas; the non-condensable gas and the purified gas are converted by the tail gas power generation unit to obtain external power and internal power which is transmitted to the power supply regulation and control unit, and the phenolic wastewater is used as a gasification agent and is transmitted to the lump coal pyrolysis unit; the method realizes the high-efficiency co-conversion of the low-rank coal and the photovoltaic energy, and has remarkable economic and environmental benefits.
Description
Technical Field
The invention relates to a low-rank coal utilization technology, in particular to a low-rank coal and photovoltaic energy cooperative conversion method.
Background
The reserves of the low-rank coal in China are rich, and lump coal pyrolysis is an important means for quality-based conversion of the low-rank coal and is an important method for high-efficiency clean utilization of the coal. The main product of the low-rank coal briquette pyrolysis technology is semicoke (semi coke), and the byproducts are tar and raw coke gas. Wherein, the semi-coke is widely used as a raw material in industries such as clean fuel or metallurgy, and the tar and the raw coke gas also have higher added values after being upgraded.
The main flow reactor adopted in the conventional low-rank lump coal pyrolysis process is an internal heating type reaction furnace, namely, air is blown into the bottom of the pyrolysis furnace to perform combustion reaction with a small part of incandescent semi-coke and the like, high-temperature flue gas flows upwards through a coal bed and performs physical and chemical reactions such as partial reduction reaction of the flue gas and pyrolysis reaction of lump coal, the generated gaseous tar and pyrolysis gas are used as raw coke to enter a downstream purification process along with the flue gas, and the bottom semi-coke is transported as a main product after being quenched.
However, the technology has many disadvantages, mainly including: firstly, can produce partial phenol-containing waste water among the lump coal pyrolysis product purification process, the processing degree of difficulty is great, treatment cost is high. Secondly, the yield of the lump coal pyrolysis tar is low, generally in the range of 6-10%, and according to an industrial structure adjustment instruction catalog (2019) published by the national development and improvement commission, from 1 month and 1 day in 2020, a single set of coal tar processing device of 5 ten thousand tons/year or less belongs to the rejected capacity, and the construction of the tar deep processing by using the self-produced tar of the pyrolysis device as a raw material is generally restricted by scale benefits. Thirdly, the hydrogen concentration in the raw gas is low, and the extraction cost of hydrogen in unit volume in the raw gas is increased along with the increase of the hydrogen yield, but the hydrogen extraction process with low yield is difficult to meet the requirement of a matched coal tar hydrogenation device on the hydrogen consumption. Fourthly, the byproduct crude gas is usually used for power generation, however, with the advance of power reformation, the difference between the peak electricity price in the daytime and the low-valley electricity price at night is continuously enlarged, the generated power plant is difficult to be absorbed at night, and the online delivery is almost cost-reduced.
With the continuous progress of the technology and the large-scale operation of suppliers, the photovoltaic power generation industry becomes mature day by day, the investment of power generation and the operation and maintenance cost are continuously reduced, and the photovoltaic power serving as a green energy conversion carrier gradually comes up to the explosive development period. However, the main disadvantages of photovoltaic power generation are periodicity and instability, so that photovoltaic power can encounter a bottleneck in the internet surfing process, and a large amount of photovoltaic power is abandoned.
Therefore, aiming at the defects in the conventional low-rank lump coal pyrolysis conversion process and the difficult problem of photovoltaic energy consumption, a method for realizing the common high-efficiency comprehensive conversion of the low-rank lump coal and the photovoltaic energy, which can realize the consumption and quality improvement of intermediate byproducts in a system, mutual supply and complementation of materials and energy in the system and resource recycling of wastes, needs to be developed urgently.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a low-rank coal and photovoltaic energy cooperative conversion method, so that the high-efficiency co-conversion of the low-rank coal and the photovoltaic energy is realized, and the economic and environmental benefits are improved.
In order to achieve the purpose, the invention adopts the following technical scheme:
a low-rank coal and photovoltaic energy cooperative conversion method comprises the following steps:
1) the low-rank coal, the air, the hydrolyzed oxygen from the water electrolysis unit and the phenol-containing wastewater from the purification and phenol extraction unit are combusted, gasified, pyrolyzed, primarily washed and cooled in the lump coal pyrolysis unit, and then semi-coke, raw coke gas and crude tar are output; wherein, the semicoke after cooling and quenching is taken as a main product to be delivered;
2) the crude tar and the foreign raw oil are subjected to desalting, dephenolizing and dehydrating treatment in a purification and phenol extraction unit to produce industrial crude phenol, phenol-containing wastewater and low-phenol tar; wherein, the industrial crude phenol is delivered as a product;
3) raw gas flows into a downstream gas purification and hydrogen extraction unit, and coal-based hydrogen and purified gas are produced after desulfurization and gas separation;
4) the purified gas and the non-condensable gas produced by the tar hydrogenation and separation unit are combusted in the tail gas power generation unit, and the alternating current generated in the process is divided into an internal power part and an external power part; wherein, the output power is output as a product through a cable;
5) the natural solar energy is absorbed by the photovoltaic power generation unit and then outputs a photovoltaic power supply, and in the power supply regulation and control unit, the internal power is converted into direct current and then is converged with the photovoltaic power supply to form a hydrogen production power supply; the purified water is converted into hydrolysis hydrogen and hydrolysis oxygen by the hydrogen production power supply in the water electrolysis unit;
6) the hydrolytic hydrogen and the coal-based hydrogen are converged and then are introduced into a tar hydrogenation and separation unit together with low-phenol tar for further processing to produce two main material flows of non-condensable gas and fuel oil, wherein the fuel oil is delivered as a product;
7) and two parallel branch pipelines are led out from the main pipeline after the hydrolytic hydrogen and the coal-based hydrogen are converged, the two branch pipelines are communicated with a hydrogen storage unit, and the hydrogen storage unit flexibly absorbs the hydrogen on the main pipeline and releases the hydrogen to the main pipeline through the two branch pipelines respectively.
Further, the content of air drying base volatile components in the industrial analysis data of the low-rank coal is not less than 28%, the content of moisture is not more than 17%, and the mass ratio of materials with the particle size of less than 3cm or more than 8cm in the low-rank coal is not more than 12%.
Further, the lump coal pyrolysis unit comprises, but is not limited to, lump coal feeding equipment, an internal heating type pyrolysis furnace, gas washing equipment and liquid-solid separation equipment, wherein the operating pressure of the pyrolysis furnace is controlled within the range of-0.05-0.5 MPaG.
Furthermore, the extraterrestrial raw oil is medium-low temperature coal tar, the purification and phenol extraction unit comprises but is not limited to water washing equipment and oil-water separation equipment, and the mass ratio of phenolic substances in the low-phenol coal tar is not higher than 2%.
Further, the gas purification and hydrogen extraction unit comprises, but is not limited to, an electric capture deep oil and dust removal device, a desulfurization device, a membrane separation device and a pressure swing adsorption device, and the volume ratio of hydrogen in the coal-based hydrogen is not less than 98%.
Furthermore, the tail gas power generation unit comprises at least 2 sets of gas-fired boilers and matched power generation equipment, and the internal power and the external power are both alternating current.
Further, the photovoltaic power supply is direct current, the power supply regulation and control unit comprises but is not limited to rectifier equipment and transformer equipment, and the water electrolysis unit comprises one or more of alkaline water electrolysis equipment, solid oxide water electrolysis equipment and proton exchange membrane pure water electrolysis equipment.
Furthermore, the volume ratio of oxygen molecules and water molecules in the hydrolyzed hydrogen gas is respectively not more than 60ppm and 800ppm, and the volume ratio of hydrogen molecules in the hydrolyzed hydrogen gas is not less than 99.9%; the mass ratio of non-phenolic substances in the industrial crude phenol is not higher than 5%; the fuel oil includes but is not limited to naphtha, jet fuel, diesel.
Further, the tar hydrogenation and separation unit comprises but is not limited to a tar hydrogenation reactor, a recycle hydrogen compressor, a hot high-pressure separator, a cold high-pressure separator and a fractionating tower, during normal operation, the temperature of the tar hydrogenation reactor is in the range of 320-480 ℃, and the outlet pressure of the reactor is in the range of 4-22 MPaG.
Further, the volume ratio of hydrogen molecules in the non-condensable gas is not higher than 70%, and the dew point of the non-condensable gas is not higher than 40 ℃.
Compared with the prior art, the invention has the following beneficial effects:
firstly, the combination with the low-rank coal quality-based utilization process enables pure green photovoltaic electric energy converted from solar energy to be efficiently consumed, and develops a new direction for electricity abandonment trouble caused by grid access difficulty of photovoltaic electricity to a great extent; the high-efficiency co-conversion of the low-rank coal and the photovoltaic energy is realized, and the economic and environmental benefits are remarkable.
Secondly, two products of hydrogen and oxygen produced in the water electrolysis process are completely consumed and converted as raw materials in the same system for the quality-divided utilization of the low-rank coal, so that the output of intermediate products is greatly reduced, and the overall economy of the whole system is improved;
thirdly, the injection of pure oxygen in the lump coal pyrolysis unit obviously improves the concentration of the synthesis gas in the pyrolysis furnace, and is beneficial to improving the yield and quality of the byproduct tar in the pyrolysis unit;
fourthly, the consumption of air at the bottom of the pyrolysis furnace is greatly reduced by injecting pure oxygen into the lump coal pyrolysis unit, so that the nitrogen content in the system is reduced, the heat value of the coal gas is improved, the reduction of the size of part of equipment is facilitated, and the difficulty of the hydrogen stripping process of the byproduct coal gas is also reduced;
fifthly, the phenol-containing wastewater in the lump coal pyrolysis unit is injected to realize on-site resource utilization of the wastewater, the matched feeding of the wastewater and pure oxygen is beneficial to regulation and control of the reaction temperature of the pyrolysis furnace, and meanwhile, the concentration of the synthesis gas in the pyrolysis furnace is obviously improved;
sixthly, the arrangement of the hydrogen storage unit is convenient for improving the operation elasticity of the system and the flexibility for dealing with emergency situations, so that the safety and the stability of the whole system operation are obviously improved, and the stable consumption of unstable photovoltaic energy is realized through the cache of hydrogen;
and seventhly, the hydrogen production by water electrolysis is complementary with the hydrogen extraction by the pyrolysis coal gas, so that the pain point of high hydrogen extraction cost caused by low hydrogen content in the pyrolysis coal gas is relieved to a great extent. In addition, photovoltaic electric energy is consumed through green hydrogen, and a new idea is provided for carbon dioxide emission reduction in the coal chemical industry.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment of the present invention;
wherein: a. a lump coal pyrolysis unit; b. a purification and phenol extraction unit; c. a gas purification and hydrogen extraction unit; d. a tail gas power generation unit; e. a photovoltaic power generation unit; f. a power supply regulation and control unit; g. a water electrolysis unit; h. a hydrogen storage unit; j. A tar hydrogenation and separation unit;
1. low-rank coal; 2. air; 3. extra raw oil; 4. solar energy; 5. purifying water; 6. a photovoltaic power source; 7. A hydrogen production power supply; 8. hydrolyzing hydrogen; 9. hydrolyzing oxygen; 10. raw gas; 11. coarse tar; 12. phenol-containing wastewater; 13. low phenol tar; 14. coal-based hydrogen; 15. purifying the coal gas; 16. semi-coke; 17. internal power; 18. delivering power; 19. industrial crude phenol; 20. non-condensable gas; 21. fuel oil.
Detailed description of the preferred embodiment
The invention is further illustrated by the following specific examples.
As shown in fig. 1, a method for the cooperative conversion of low-rank coal and photovoltaic energy comprises the following steps:
1) the low-rank coal 1, the air 2, the hydrolyzed oxygen 9 from the water electrolysis unit g and the phenolic wastewater 12 from the purification and phenol extraction unit b are subjected to chemical reactions such as complex combustion, gasification, pyrolysis and the like and preliminary washing and cooling in the lump coal pyrolysis unit a, and three main material flows of semicoke 16, raw coke gas 10 and crude tar 11 are output. Wherein, the semicoke 16 after cooling and quenching is taken as a main product to be delivered;
2) and the crude tar 11 and the foreign raw oil 3 are subjected to desalting, dephenolizing and dehydrating treatment in a purification and phenol extraction unit b to produce three main material flows of industrial crude phenol 19, phenol-containing wastewater 12 and low-phenol tar 13. Wherein the industrial crude phenol 19 is delivered as a product;
3) the raw gas 10 flows into a gas purification and hydrogen extraction unit c at the downstream, and two main material flows of coal-based hydrogen 14 and purified gas 15 are produced after desulfurization and gas separation;
4) the purified gas 15 is combusted in the tail gas power generation unit d together with the noncondensable gas 20 produced by the tar hydrogenation and separation unit j, and the alternating current generated in the process is divided into two parts, namely internal power 17 and external power 18. Wherein the outgoing power 18 is exported as a product via a cable;
5) the natural solar energy 4 is absorbed by the photovoltaic power generation unit e and then outputs the photovoltaic power supply 6, and in the power supply regulation and control unit f, the internal electric power 17 is converted into direct current and then is converged with the photovoltaic power supply 6 to form the hydrogen production power supply 7. The purified water 5 is converted into two main material flows of hydrolyzed hydrogen 8 and hydrolyzed oxygen 9 by a hydrogen production power supply 7 in a water electrolysis unit g;
6) the hydrolysis hydrogen 8 and the coal-based hydrogen 14 are converged and then introduced into a tar hydrogenation and separation unit j together with the low-phenol tar 13 for further processing to produce two main material flows of non-condensable gas 20 and fuel oil 21, wherein the fuel oil 21 is delivered as a product;
7) and two parallel branch pipelines are led out from the main pipeline after the hydrolysis hydrogen 8 and the coal-based hydrogen 14 are converged, and are communicated with a hydrogen storage unit h, and the hydrogen storage unit h flexibly absorbs the hydrogen on the main pipeline and releases the hydrogen to the main pipeline through the two branch pipelines respectively.
The content of air drying base volatile components in the industrial analysis data of the low-rank coal 1 is not less than 28%, the content of water is not more than 17%, and the mass ratio of materials with the particle size of less than 3cm or more than 8cm in the low-rank coal 1 is not more than 12%.
The lump coal pyrolysis unit a comprises, but is not limited to, lump coal feeding equipment, an internal heating type pyrolysis furnace, gas washing equipment and liquid-solid separation equipment, wherein the operating pressure of the pyrolysis furnace is controlled within the range of-0.05-0.5 MPaG.
The out-of-range raw oil 3 is medium-low temperature coal tar, the purification and phenol extraction unit b comprises but is not limited to water washing equipment and oil-water separation equipment, and the mass ratio of phenolic substances in the low-phenol tar 13 is not higher than 2%.
The coal gas purification and hydrogen extraction unit c comprises but is not limited to electric capture deep oil and dust removal equipment, desulfurization equipment, membrane separation equipment and pressure swing adsorption equipment, and the volume ratio of hydrogen in the coal-based hydrogen 14 is not less than 98%.
The tail gas power generation unit d comprises at least 2 sets of gas-fired boilers and matched power generation equipment, and the internal electric power 17 and the external electric power 18 are both alternating current.
The photovoltaic power supply 6 is direct current, the power supply regulation and control unit f includes but is not limited to rectifier equipment and transformer equipment, the purified water 5 needs to meet the requirements of GB/T19774-.
The volume ratio of oxygen molecules and water molecules in the hydrolyzed hydrogen 8 is respectively not more than 60ppm and 800ppm, and the volume ratio of hydrogen molecules in the hydrolyzed hydrogen 8 is not less than 99.9%.
The tar hydrogenation and separation unit j comprises a tar hydrogenation reactor, a recycle hydrogen compressor, a hot high-pressure separator, a cold high-pressure separator and a fractionating tower, wherein during normal operation, the temperature of the tar hydrogenation reactor is within the range of 320-480 ℃, and the outlet pressure of the reactor is within the range of 4-22 MPaG.
The volume ratio of hydrogen molecules in the non-condensable gas 20 is not higher than 70%, and the dew point of the non-condensable gas 20 is not higher than 40 ℃.
The mass ratio of non-phenolic substances in the industrial crude phenol 19 is not higher than 5%.
The fuel oil 21 includes but is not limited to naphtha, jet fuel, diesel.
The working process is as follows:
in the time of sufficient sunshine in the daytime, the water electrolysis unit g can run at full load so as to utilize the photovoltaic power supply 6 to the maximum extent, and the surplus hydrogen can be stored through the hydrogen storage unit h. Meanwhile, the hydrogen extraction load of the gas purification and hydrogen extraction unit c can be properly adjusted to reduce the output of the coal-based hydrogen 14, and the flow of the internal electric power 17 can be properly adjusted to realize the output of more external electric power 18, so as to meet the demand of peak electricity consumption in the daytime.
In the evening, early morning or in the weak sunshine period, the hydrogen stored in the hydrogen storage unit h is preferentially released. Meanwhile, the hydrogen extraction load of the coal gas purification and hydrogen extraction unit c can be moderately adjusted to increase the output of coal-based hydrogen 14, and the processing load of the tar hydrogenation and separation unit can be moderately reduced, so that the demand of the system on hydrogen is reduced, and the output of the outgoing power 18 is ensured, and the demand of the peak power consumption in the daytime is met.
During the low-ebb period of the power utilization in the nighttime social environment, the flow of the internal power 17 is preferentially adjusted and increased for the stable supply of the hydrolysis hydrogen 8 and the hydrolysis oxygen 9, and the storage of the hydrogen in the hydrogen storage unit h is increased. Meanwhile, the hydrogen extraction load of the gas purification and hydrogen extraction unit c can be moderately adjusted to increase the output of coal-based hydrogen 14, and the processing load of the tar hydrogenation and separation unit can be moderately increased, so that the demand of the system on hydrogen is increased, the great reduction and even interruption of the outgoing power 18 are ensured, and the difficulty of internet access outgoing of low-ebb electricity at night is relieved.
The above-described embodiments are provided to better explain the principles of the present invention and not to limit the present invention by any means, such as by making modifications, equivalents, and improvements within the spirit and scope of the present invention as defined by the appended claims.
Claims (10)
1. A low-rank coal and photovoltaic energy cooperative conversion method is characterized by comprising the following steps:
1) the method comprises the following steps of (1) outputting semicoke (16), raw coke gas (10) and crude tar (11) after combustion, gasification, pyrolysis reaction and preliminary washing and cooling in a lump coal pyrolysis unit (a) by using low-rank coal (1), air (2), hydrolyzed oxygen (9) from a water electrolysis unit (g) and phenolic wastewater (12) from a purification and phenol extraction unit (b); wherein, the semicoke (16) after cooling and quenching is taken as a main product to be delivered;
2) the crude tar (11) and the extra-corporeal raw oil (3) are subjected to desalting, dephenolizing and dehydrating treatment in a purifying and phenol extracting unit (b) to produce industrial crude phenol (19), phenol-containing wastewater (12) and low-phenol tar (13); wherein the crude industrial phenol (19) is delivered as product;
3) the raw gas (10) flows into a downstream gas purification and hydrogen extraction unit (c), and coal-based hydrogen (14) and purified gas (15) are produced after desulfurization and gas separation;
4) the purified gas (15) and the non-condensable gas (20) produced by the tar hydrogenation and separation unit (j) are combusted in the tail gas power generation unit (d), and the alternating current generated in the process is divided into internal power (17) and external power (18); wherein the outgoing power (18) is carried out as a product via a cable;
5) the natural solar energy (4) is absorbed by the photovoltaic power generation unit (e) and then outputs a photovoltaic power supply (6), and in the power supply regulation and control unit (f), the internal power (17) is converted into direct current and then is converged with the photovoltaic power supply (6) to form a hydrogen production power supply (7); the purified water (5) is converted into hydrolyzed hydrogen (8) and hydrolyzed oxygen (9) by a hydrogen production power supply (7) in a water electrolysis unit (g);
6) the hydrolysis hydrogen (8) is converged with the coal-based hydrogen (14), and then is introduced into a tar hydrogenation and separation unit (j) together with low-phenol tar (13) for further processing to produce two main material flows of non-condensable gas (20) and fuel oil (21), wherein the fuel oil (21) is delivered as a product;
7) and two parallel branch pipelines are led out from the main pipeline after the hydrolytic hydrogen (8) and the coal-based hydrogen (14) are converged, and are communicated with a hydrogen storage unit (h), and the hydrogen storage unit (h) flexibly absorbs the hydrogen on the main pipeline and releases the hydrogen to the main pipeline through the two branch pipelines respectively.
2. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: in the industrial analysis data of the low-rank coal (1), the content of volatile components of an air drying base is not less than 28%, the content of water is not more than 17%, and the mass ratio of materials with the granularity of less than 3cm or more than 8cm in the low-rank coal (1) is not more than 12%.
3. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the lump coal pyrolysis unit (a) comprises, but is not limited to, lump coal feeding equipment, an internal heating type pyrolysis furnace, gas washing equipment and liquid-solid separation equipment, wherein the operating pressure of the pyrolysis furnace is controlled within the range of-0.05-0.5 MPaG.
4. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the extraterrestrial raw oil (3) is medium-low temperature coal tar, the purification and phenol extraction unit (b) comprises but is not limited to water washing equipment and oil-water separation equipment, and the mass ratio of phenolic substances in the low-phenol tar (13) is not higher than 2%.
5. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the coal gas purification and hydrogen extraction unit (c) comprises, but is not limited to, electric capture deep oil and dust removal equipment, desulfurization equipment, membrane separation equipment and pressure swing adsorption equipment, and the volume ratio of hydrogen in the coal-based hydrogen (14) is not less than 98%.
6. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the tail gas power generation unit (d) comprises at least 2 sets of gas-fired boilers and matched power generation equipment, and the internal power (17) and the external power (18) are both alternating current.
7. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the photovoltaic power supply (6) is direct current, the power supply regulation and control unit (f) comprises but is not limited to rectifier equipment and transformer equipment, and the water electrolysis unit (g) comprises one or more of alkaline water electrolysis equipment, solid oxide water electrolysis equipment and proton exchange membrane pure water electrolysis equipment.
8. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the volume ratio of oxygen molecules and water molecules in the hydrolyzed hydrogen (8) is respectively not more than 60ppm and 800ppm, and the volume ratio of hydrogen molecules in the hydrolyzed hydrogen (8) is not less than 99.9%; the mass proportion of non-phenolic substances in the industrial crude phenol (19) is not higher than 5%; the fuel oil (21) includes but is not limited to naphtha, jet fuel, diesel.
9. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the tar hydrogenation and separation unit (j) comprises a tar hydrogenation reactor, a circulating hydrogen compressor, a hot high-pressure separator, a cold high-pressure separator and a fractionating tower, wherein during normal operation, the temperature of the tar hydrogenation reactor is within the range of 320-480 ℃, and the outlet pressure of the reactor is within the range of 4-22 MPaG.
10. The low-rank coal and photovoltaic energy cooperative conversion method according to claim 1, characterized in that: the volume ratio of hydrogen molecules in the non-condensable gas (20) is not higher than 70%, and the dew point of the non-condensable gas (20) is not higher than 40 ℃.
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