CN219824379U - Continuous green hydrogen coupling coal chemical preparation synthetic ammonia system - Google Patents
Continuous green hydrogen coupling coal chemical preparation synthetic ammonia system Download PDFInfo
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- CN219824379U CN219824379U CN202321127026.3U CN202321127026U CN219824379U CN 219824379 U CN219824379 U CN 219824379U CN 202321127026 U CN202321127026 U CN 202321127026U CN 219824379 U CN219824379 U CN 219824379U
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- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 137
- 239000001257 hydrogen Substances 0.000 title claims abstract description 136
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 135
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 103
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 51
- 239000003245 coal Substances 0.000 title claims abstract description 37
- 238000002360 preparation method Methods 0.000 title claims abstract description 15
- 239000000126 substance Substances 0.000 title claims abstract description 11
- 230000008878 coupling Effects 0.000 title claims abstract description 7
- 238000010168 coupling process Methods 0.000 title claims abstract description 7
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 162
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 81
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 52
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 52
- 239000001301 oxygen Substances 0.000 claims abstract description 52
- 238000003860 storage Methods 0.000 claims abstract description 47
- 238000005406 washing Methods 0.000 claims abstract description 41
- 239000007788 liquid Substances 0.000 claims abstract description 39
- 230000005611 electricity Effects 0.000 claims abstract description 34
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000002309 gasification Methods 0.000 claims abstract description 24
- 239000002994 raw material Substances 0.000 claims abstract description 24
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 22
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 22
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 238000009826 distribution Methods 0.000 claims abstract description 8
- 238000010248 power generation Methods 0.000 claims description 20
- 238000000926 separation method Methods 0.000 claims description 17
- 238000012824 chemical production Methods 0.000 claims 5
- 238000004519 manufacturing process Methods 0.000 abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 24
- 238000005868 electrolysis reaction Methods 0.000 abstract description 17
- 238000000034 method Methods 0.000 description 22
- 239000007789 gas Substances 0.000 description 20
- 230000008569 process Effects 0.000 description 15
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000001569 carbon dioxide Substances 0.000 description 6
- 230000007547 defect Effects 0.000 description 6
- 239000003034 coal gas Substances 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 230000002194 synthesizing effect Effects 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000004480 active ingredient Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The utility model relates to a continuous green hydrogen coupling coal chemical preparation synthetic ammonia system; the device comprises a raw material coal bin, a green electricity unit, an electrolytic cell device, an oxygen outlet channel of the electrolytic cell device, a hydrogen buffer tank and a hydrogen storage unit, wherein the raw material coal bin is connected with an ammonia synthesis device through a gasification furnace, a conversion device, a low-temperature methanol washing device and a liquid nitrogen washing and nitrogen distribution device; the green electricity unit is matched with the water electrolysis hydrogen production process to achieve the purpose of saving electricity charge, meanwhile, one part of hydrogen raw materials are used for production, and the other part of raw materials are subjected to hydrogen storage operation, so that when the water electrolysis hydrogen production process stops running due to the fact that the green electricity unit does not generate electricity, the hydrogen in the hydrogen storage operation is used for producing synthetic ammonia, and the advantage of continuous operation of the synthetic ammonia production system is achieved.
Description
Technical Field
The utility model relates to the technical field of synthetic ammonia preparation, in particular to a continuous green hydrogen coupling coal chemical preparation synthetic ammonia system.
Background
In the prior art, hydrogen is one of important raw materials in the preparation of synthetic ammonia; the method for preparing hydrogen in the field of coal chemical industry is a mode of preparing hydrogen by coal, namely the mode of preparing hydrogen by coal gasification is composed of four parts of preparing coal gas by converting coal steam, purifying the coal gas, converting the coal gas and purifying the hydrogen by pressure swing adsorption, coal or coke reacts with the water steam at high temperature to generate the coal gas mainly containing hydrogen, carbon monoxide and carbon dioxide, the coal gas is mixed with the water steam for conversion reaction after cooling, dedusting and desulfurizing, most of the carbon monoxide is converted into hydrogen and carbon dioxide to become converted gas, and then the converted gas is subjected to pressure swing adsorption (process to obtain high-purity hydrogen.
In order to overcome the defects and the irreplaceable background of the hydrogen demand, partial enterprises try to adopt the form of hydrogen production by water electrolysis, and the unit consumption of the current water electrolysis hydrogen production process is 5kwh/Nm 3 The theoretical power consumption for generating 1 cubic meter of hydrogen is 2.94kwh according to Faraday law, and the cost of electricity for preparing hydrogen in the method is too high, so that the price for preparing synthetic ammonia in the process is high, and the enterprise competitiveness is reduced.
In summary, how to prepare hydrogen to meet the requirements of the synthesis ammonia on the premise of reducing carbon dioxide emission and production and operation costs is a problem to be solved in the industry.
Disclosure of Invention
The utility model aims to provide a continuous green hydrogen coupled coal chemical preparation synthetic ammonia system, which aims to solve the problems in the background technology.
In order to achieve the above purpose, the present utility model provides the following technical solutions:
the utility model provides a continuous green hydrogen coupling coal chemical industry preparation synthetic ammonia system, including raw materials coal bunker, raw materials coal bunker links to each other with ammonia synthesizer through gasifier, conversion equipment, low temperature methanol washing device and liquid nitrogen washing nitrogen fitting, still includes green electricity unit, and green electricity unit is connected with the electrolysis trough device electricity, and the oxygen outlet channel of electrolysis trough device links to each other with the gasifier, and the hydrogen outlet channel of electrolysis trough device links to each other with the import of hydrogen buffer tank, and the export of hydrogen buffer tank links to each other with liquid nitrogen washing nitrogen fitting and hydrogen storage unit respectively.
The beneficial effects of the utility model are as follows: the green electricity unit is matched with the water electrolysis hydrogen production process to achieve the purpose of saving electricity charge, and can be a solar power generation device, a water energy power generation device and a wind power generation device, but the green electricity unit is severely restricted by natural environment, and the solar power generation device is taken as an example, so that the power resources are abundant in daytime, and the power cannot be generated at night or in overcast and rainy days; the water energy power generation is limited by the environment and the withering factor of water, and the wind energy power generation is also influenced by weather factors; in order to overcome the defect that a system for preparing the synthetic ammonia cannot stably operate for a long time due to lack of raw materials, the utility model uses one part of hydrogen raw materials for production, and the other part of raw materials are subjected to hydrogen storage operation, when the green electricity unit does not generate electricity to cause the operation stop of the water electrolysis hydrogen production process, the hydrogen in the hydrogen storage operation is used for supplying the production of the synthetic ammonia; meanwhile, in order to improve the hydrogen storage capacity in the hydrogen storage operation, the utility model couples the process of the hydrogen storage operation with the liquid nitrogen washing and nitrogen distributing device, so that the hydrogen is changed into liquid hydrogen to achieve the characteristic of improving the hydrogen storage capacity in a limited storage space.
In the above technical solution, preferably, the green electricity unit is a solar power generation device or a wind power generation device.
In the above technical solution, preferably, a nitrogen inlet of the liquid nitrogen washing nitrogen distribution device is connected with a nitrogen outlet channel of the air separation device.
In the above technical solution, preferably, the oxygen outlet channel of the air separation device is connected with an oxygen storage tank, a first valve and a tee joint are arranged between the oxygen storage tank and the gasifier, and a second valve is arranged between the oxygen outlet channel of the electrolyzer device and the tee joint;
an oxygen compressor is arranged between the tee joint and the gasification furnace.
In the above technical scheme, preferably, a third valve is arranged between the outlet of the hydrogen buffer tank and the liquid nitrogen washing and nitrogen distributing device, and a fourth valve is arranged between the outlet of the hydrogen buffer tank and the hydrogen storage unit.
In the above technical scheme, preferably, the hydrogen storage unit comprises a hot side channel of a liquid nitrogen washing and nitrogen distributing device, an outlet of the hot side channel of the liquid nitrogen washing and nitrogen distributing device is connected with the hydrogen storage tank through the hydrogen compressor, and the hydrogen storage tank is connected with the hydrogen buffer tank through the fifth valve.
Compared with the prior art, the utility model provides a continuous green hydrogen coupling coal chemical preparation synthetic ammonia system, which has the following beneficial effects:
1. the green electricity unit is purchased to generate electricity so as to solve the defects of high power consumption and high production cost in the current water electrolysis hydrogen production process, and meanwhile, the green electricity unit has the condition of unstable electricity generation and is easy to cause the problem that the synthetic ammonia production system stops running due to the lack of hydrogen raw materials; the utility model is characterized in that the hydrogen storage unit is arranged and is coupled with the liquid nitrogen washing and distributing device, so that the hydrogen is converted into liquid state from gaseous state by cooling, the hydrogen storage capacity is effectively improved in a limited storage space, and the purpose of long-term stable operation of the synthetic ammonia production system is ensured.
2. The utility model uses byproduct oxygen as combustion improver to be transported into gasification furnace for use, so as to replace traditional oxygen, thereby achieving the purpose of utilizing the byproduct of the electrolytic water hydrogen production process and reducing production cost.
3. When the byproduct oxygen in the water electrolysis hydrogen production process is used as the gasifier, the utility model can store the oxygen in the air separation device for standby in order to ensure the stable operation of the gasifier when the water electrolysis hydrogen production process stops operating, thereby ensuring the long-time stable operation of the gasifier.
Drawings
For a clearer description of the technical solutions of the embodiments of the present utility model, the drawings that are needed in the description of the embodiments will be briefly described below, it will be apparent that the drawings in the description below are only some embodiments of the present utility model, and that other drawings can be obtained according to these drawings without inventive effort for a person skilled in the art:
FIG. 1 is a schematic view of the whole structure of the present utility model.
In the figure: 1. a raw material coal bunker; 2. a gasification furnace; 3. a conversion device; 4. a low temperature methanol washing device; 5. a nitrogen preparing device for liquid nitrogen washing; 6. an ammonia synthesis device; 7. a green electricity unit; 8. an electrolyzer device; 9. a hydrogen buffer tank; 10. an air separation device; 11. a nitrogen outlet channel; 12. an oxygen outlet channel; 13. an oxygen storage tank; 14. a first valve; 15. a tee joint; 16. a second valve; 17. an oxygen compressor; 18. a third valve; 19. a fourth valve; 20. a hydrogen compressor; 21. a hydrogen storage tank; 22. and a fifth valve.
Detailed Description
The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model.
Referring to fig. 1, a continuous green hydrogen coupled coal chemical preparation synthetic ammonia system comprises a raw material coal bunker 1, wherein the raw material coal bunker 1 is connected with an ammonia synthesis device 6 through a gasification furnace 2, a conversion device 3, a low-temperature methanol washing device 4 and a liquid nitrogen washing and nitrogen distribution device 5, and further comprises a green electricity unit 7, wherein the green electricity unit 7 is electrically connected with an electrolytic tank device 8, an oxygen outlet channel of the electrolytic tank device 8 is connected with the gasification furnace 2, a hydrogen outlet channel of the electrolytic tank device 8 is connected with an inlet of a hydrogen buffer tank 9, and an outlet of the hydrogen buffer tank 9 is respectively connected with the liquid nitrogen washing and nitrogen distribution device 5 and a hydrogen storage unit. The low-temperature methanol washing apparatus 4 of the present utility model mainly includes, but is not limited to, the following devices: a methanol washing tower, a CO2 resolving tower, an H2S concentration tower, a heat regeneration tower, a nitrogen stripping tower, an unconverted gas washing tower and a medium-pressure flash tower; liquid nitrogen wash nitrogen dosing device 5 includes, but is not limited to, the following: a nitrogen scrubber, a high-pressure nitrogen cooler, a raw material gas cooler, a gas-liquid separator and a hydrogen separator; ammonia synthesis unit 6 includes, but is not limited to, the following: an ammonia synthesis tower, a start-up heating furnace, a steam superheater, a steam generator, an ammonia cooler, a high-pressure ammonia separator and a medium-pressure ammonia separator; the electrolyzer unit 8 includes, but is not limited to, the following: a power supply transformer, an electrolysis water tank, a gas-liquid separation tank, a circulating liquid cooler and a gas purifier; the transformation means 3 include, but are not limited to, the following: a shift converter, a heat exchanger, etc. As described above, the raw material hydrogen is needed for the production of the synthetic ammonia, and the conventional method is a coal hydrogen production process, so that the method has the characteristics of low investment, low operation cost and sufficient hydrogen yield, and accords with the synthetic ammonia preparation process, but has the defect of discharging a large amount of carbon dioxide; in order to overcome the defects, the hydrogen production process by water electrolysis is adopted, and has the characteristics of environmental protection, but the operation cost is too high due to high power consumption; the defect of high operation cost can be overcome by purchasing the green electricity unit 7, and the development requirement of green clean energy is met; based on the above, the technical scheme of the utility model is that the green electricity unit 7 is used for generating electricity, so that the green electricity and the water electrolysis hydrogen production process are combined to solve the problem of low operation cost, and meanwhile, the byproduct oxygen of the water electrolysis hydrogen production process is used as a combustion improver to be conveyed to the gasification furnace 2, so that the aim of reducing the operation cost again is fulfilled.
Further, the green electricity unit 7 is a solar power generation device or a wind power generation device. The green power unit 7 in the utility model can use a solar power generation device or a wind power generation device to generate power, and can be specifically selected according to actual conditions.
Further, the nitrogen inlet of the liquid nitrogen washing nitrogen distributing device 5 is connected with the nitrogen outlet channel 11 of the air separating device 10. The air separation plant 10 of the present utility model includes, but is not limited to, an air compressor, an air cooling tower, a turbo expander, a fractionation tower, etc., and the air separation plant 10 is used in the present utility model to separate nitrogen for use in the liquid nitrogen scrubbing nitrogen unit 5.
Further, an oxygen outlet channel 12 of the air separation device 10 is connected with an oxygen storage tank 13, a first valve 14 and a tee joint 15 are arranged between the oxygen storage tank 13 and the gasification furnace 2, and a second valve 16 is arranged between the oxygen outlet channel of the electrolytic tank device 8 and the tee joint 14; an oxygen compressor 17 is arranged between the tee 15 and the gasification furnace 2. In order to ensure stable operation of the gasification furnace 2, the present utility model preferably uses the electrolyzer unit 8 to supply oxygen to the gasification furnace 2, and when the electrolyzer unit 8 stops operating, the air separation unit 10 is selected to supply oxygen to the gasification furnace 2; namely: during operation of the electrolyzer unit 8, oxygen separated by the air separation unit 10 may be temporarily stored for use by the oxygen storage tank 13.
Further, a third valve 18 is arranged between the outlet of the hydrogen buffer tank 9 and the liquid nitrogen washing and nitrogen distributing device 5, and a fourth valve 19 is arranged between the outlet of the hydrogen buffer tank 9 and the hydrogen storage unit. The third valve 18 supplies raw materials to the liquid nitrogen washing and nitrogen distributing device 5, and belongs to a normally open valve; the fourth valve 19 is opened and closed mainly depending on whether the electrolyzer unit 8 is operated or not, when the electrolyzer unit 8 is operated, the fourth valve 19 is in an opened state, and when the electrolyzer unit 8 is stopped, the fourth valve 19 is in a closed state, so as to achieve the purpose of hydrogen storage.
Further, the hydrogen storage unit comprises a hot side channel of the liquid nitrogen washing and nitrogen distributing device 5, an outlet of the hot side channel of the liquid nitrogen washing and nitrogen distributing device 5 is connected with a hydrogen storage tank 21 through a hydrogen compressor 20, and the hydrogen storage tank 21 is connected with a hydrogen buffer tank 9 through a fifth valve 22. The purpose of improving the hydrogen storage capacity can be achieved through the structure, meanwhile, the opening and closing of the fifth valve 22 mainly depends on whether the electrolytic cell device 8 operates, when the electrolytic cell device 8 operates, the fifth valve 22 is in a closed state, and when the electrolytic cell device 8 stops operating, the fourth valve 19 is in an open state, so that the purpose of storing hydrogen is achieved.
The working principle of the utility model is as follows: the green electricity unit 7 generates electric energy, the electric energy is transmitted to the electrolytic tank device 8 for hydrolysis to prepare hydrogen and oxygen, the oxygen is taken as a combustion improver to enter the gasification furnace 2 to replace the traditional oxygen and achieve the purpose of reducing the cost, one part of the hydrogen enters the liquid nitrogen washing nitrogen distribution device 5 to be used as a raw material for preparing synthetic ammonia, and the other part of the hydrogen enters the hydrogen storage unit to be stored for later use; in the process, raw material coal in the raw material coal bunker 1 enters the gasification furnace 2 for combustion to prepare coarse synthesis gas; the crude synthesis gas is converted by a conversion device 3, and the converted conversion gas is removed CO in the conversion gas by a low-temperature methanol washing device 4 2 、H 2 S, COS and other impurities, then enter a liquid nitrogen washing and nitrogen preparing device 5, combine with nitrogen from an air separating device 10 and hydrogen from a hydrogen buffer tank 9, remove CO and enter an ammonia synthesizing device 6 to prepare synthetic ammonia; when the green electricity unit 7 cannot generate electricity due to natural reasons such as weather, the operation of the electrolyzer unit 8 is stopped, and at the moment, the oxygen separated in the air separation unit 10 is used for supplying the gasification furnace 2, so that the hydrogen of the hydrogen storage unit enters the liquid nitrogen washing and nitrogen distributing device through the hydrogen buffer tank 9And 5, ensuring the stable operation of the synthetic ammonia production system for a long time.
Examples
The electrolytic water is used for producing hydrogen and oxygen for synthesizing ammonia, and a set of green ammonia synthesizing device which produces fifty thousand tons each year is constructed; oxygen generated by the electrolytic water hydrogen production process is used for replacing oxygen with purity of 99.6 percent sent by an air separation device by establishing an electrolytic tank device 8; the flow rate of oxygen generated by the electrolytic cell device 8 is 2800Nm 3 And/h, controlling the pressure to 7.8MPa (the temperature is 25 ℃), feeding the oxygen into an outer ring channel of the process burner, controlling the central oxygen flow to be 15-20% of the total oxygen amount through a central oxygen regulating valve, feeding the oxygen into a central channel of the process burner, and carrying out gasification reaction with coal water slurry and oxygen from a raw material coal bunker 1 in a gasification furnace 2 under the conditions of about 6.5MPa and 1350 ℃; gasification reaction to CO and H 2 Raw synthesis gas as active ingredient, the flow rate of the raw synthesis gas is 7052.5Nm 3 And/h, the coal consumption is 5225kg/h; the crude synthesis gas is treated correspondingly so that the dust content in the synthesis gas is less than 1mg/Nm 3 Then the mixture is sent into a conversion device 3; the shift device 3 shifts the raw synthesis gas to reduce the CO content of the shifted shift gas to about 1.45%, and the shifted shift gas enters the low-temperature methanol washing device 4 to remove CO in the shift gas from the upstream shift process 2 、H 2 S, COS and other impurities, simultaneously removing saturated water brought in by the shift gas, and then sending the synthesis gas into a liquid nitrogen washing nitrogen-distributing device 5 for carbon monoxide removal. At the same time, the hydrogen obtained in the electrolyzer unit 8 was fed into the hydrogen buffer tank 9 at a total flow rate of 13440Nm 3 The direct hydrogen production time of the photovoltaic electricity generated by the solar power generation device is about ten hours per day, the hydrogen coming out of the hydrogen buffer tank 9 is divided into two paths, and the hydrogen is regulated by a third valve 18 and a fourth valve 19; when the solar power generation device supplies power, one path of hydrogen is used for adjusting the hydrogen flow to 7840Nm through the fourth valve 19 3 And/h enters a relevant heat exchanger in the liquid nitrogen washing and nitrogen distributing device 5 to exchange heat and cool, and after cooling, the cooled liquid nitrogen is pressurized by a hydrogen compressor 20 and stored in a hydrogen storage tank 21; the other path of hydrogen is regulated to 5600Nm through a third valve 18 3 /h into the liquid nitrogen washing nitrogen distribution device 5 and nitrogen from the air separation device 10The gas is subjected to nitrogen matching, and the reaction gas after the nitrogen matching is completed enters an ammonia synthesis device 6 to synthesize ammonia; when the solar power generation device is not powered, the fourth valve 19 is closed, the fifth valve 22 and the third valve 18 are opened, and the hydrogen gas in the hydrogen gas storage tank 21 is kept at a flow rate of 5600Nm 3 And (h) introducing the reaction gas into the ammonia synthesis device 6 to synthesize ammonia gas after nitrogen preparation by introducing the hydrogen buffer tank 9 and the third valve 18 into the liquid nitrogen washing nitrogen preparation device 5 to prepare nitrogen; in the process, the air separation device 10 continuously works, oxygen generated by separation enters the oxygen storage tank 13 through the oxygen outlet channel 12 for temporary storage, oxygen generated by the electrolytic cell device 8 is preferentially used when the solar power generation device supplies power, and oxygen of the oxygen storage tank 13 is used when the solar power generation device does not supply power, so that long-time stable operation of the gasification furnace 2 is ensured; the process realizes the continuous production of the whole system and the continuous application of solar energy. Ammonia synthesis is carried out in the ammonia synthesis procedure, and the total ammonia yield is 5 ten thousand tons per year;
the utility model realizes the green production of large-scale hydrogen through clean energy power generation and water electrolysis hydrogen production, and simultaneously comprehensively utilizes oxygen generated in the green hydrogen preparation process in the coal gasification working section so as to realize the purpose of reducing the running cost of enterprises, greatly reduce the use amount of raw material coal on the premise of not reducing the synthetic effective air flow, and reduce the emission amount of carbon dioxide in the subsequent working section; in the implementation process, green hydrogen is used for green ammonia synthesis, so that the carbon dioxide emission in the ammonia synthesis process of coal chemical enterprises is reduced, and meanwhile, the production cost of the enterprises is reduced; furthermore, the utility model utilizes the cold energy generated in the nitrogen preparing process of the liquid nitrogen washing and preparing device 5 to reduce the temperature of the hydrogen to liquefy and store the hydrogen, thereby improving the storage efficiency of the hydrogen and realizing the continuous operation of synthesizing the green ammonia from the green hydrogen.
It is noted that relational terms such as first and second, and the like are used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Moreover, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising one does not exclude the presence of other like elements in a process, method, article, or apparatus that comprises an element.
Claims (6)
1. The utility model provides a continuous green hydrogen coupling coal chemical industry preparation synthetic ammonia system, includes raw materials coal bunker (1), and raw materials coal bunker (1) link to each other with ammonia synthesizer (6) through gasifier (2), conversion equipment (3), low temperature methanol washing device (4) and liquid nitrogen washing nitrogen device (5), its characterized in that: the device also comprises a green electricity unit (7), wherein the green electricity unit (7) is electrically connected with the electrolytic tank device (8), an oxygen outlet channel of the electrolytic tank device (8) is connected with the gasification furnace (2), a hydrogen outlet channel of the electrolytic tank device (8) is connected with an inlet of a hydrogen buffer tank (9), and an outlet of the hydrogen buffer tank (9) is respectively connected with the liquid nitrogen washing nitrogen distribution device (5) and the hydrogen storage unit.
2. The continuous green hydrogen coupled coal chemical production synthetic ammonia system of claim 1, wherein: the green electricity unit (7) is a solar power generation device or a wind power generation device.
3. The continuous green hydrogen coupled coal chemical production synthetic ammonia system of claim 1, wherein: the nitrogen inlet of the liquid nitrogen washing nitrogen distribution device (5) is connected with the nitrogen outlet channel (11) of the air separation device (10).
4. A continuous green hydrogen-coupled coal chemical production synthesis ammonia system according to claim 3, wherein: an oxygen outlet channel (12) of the air separation device (10) is connected with an oxygen storage tank (13), a first valve (14) and a tee joint (15) are arranged between the oxygen storage tank (13) and the gasification furnace (2), and a second valve (16) is arranged between the oxygen outlet channel of the electrolytic tank device (8) and the tee joint (15);
an oxygen compressor (17) is arranged between the tee joint (15) and the gasification furnace (2).
5. The continuous green hydrogen coupled coal chemical production synthetic ammonia system of claim 1, wherein: a third valve (18) is arranged between the outlet of the hydrogen buffer tank (9) and the liquid nitrogen washing and nitrogen distributing device (5), and a fourth valve (19) is arranged between the outlet of the hydrogen buffer tank (9) and the hydrogen storage unit.
6. A continuous green hydrogen coupled coal chemical production synthesis ammonia system according to claim 1 or 5, wherein: the hydrogen storage unit comprises a hot side channel of the liquid nitrogen washing and nitrogen distributing device (5), an outlet of the hot side channel of the liquid nitrogen washing and nitrogen distributing device (5) is connected with a hydrogen storage tank (21) through a hydrogen compressor (20), and the hydrogen storage tank (21) is connected with a hydrogen buffer tank (9) through a fifth valve (22).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321127026.3U CN219824379U (en) | 2023-05-10 | 2023-05-10 | Continuous green hydrogen coupling coal chemical preparation synthetic ammonia system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321127026.3U CN219824379U (en) | 2023-05-10 | 2023-05-10 | Continuous green hydrogen coupling coal chemical preparation synthetic ammonia system |
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| CN219824379U true CN219824379U (en) | 2023-10-13 |
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| CN202321127026.3U Active CN219824379U (en) | 2023-05-10 | 2023-05-10 | Continuous green hydrogen coupling coal chemical preparation synthetic ammonia system |
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