CN115928105B - Regenerative green hydrogen ammonia energy storage system - Google Patents
Regenerative green hydrogen ammonia energy storage system Download PDFInfo
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- CN115928105B CN115928105B CN202310059585.3A CN202310059585A CN115928105B CN 115928105 B CN115928105 B CN 115928105B CN 202310059585 A CN202310059585 A CN 202310059585A CN 115928105 B CN115928105 B CN 115928105B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 209
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 110
- 239000001257 hydrogen Substances 0.000 title claims abstract description 47
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 47
- 230000001172 regenerating effect Effects 0.000 title claims abstract description 11
- 238000004146 energy storage Methods 0.000 title claims abstract description 8
- 125000004435 hydrogen atom Chemical class [H]* 0.000 title 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 84
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 82
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 80
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 41
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000011084 recovery Methods 0.000 claims abstract description 23
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims description 13
- 230000006835 compression Effects 0.000 claims description 10
- 238000007906 compression Methods 0.000 claims description 10
- 238000004821 distillation Methods 0.000 claims description 10
- 150000002431 hydrogen Chemical class 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 5
- 238000005265 energy consumption Methods 0.000 abstract description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 abstract description 3
- 229910001882 dioxygen Inorganic materials 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 9
- 239000000203 mixture Substances 0.000 description 8
- 238000000034 method Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000005266 casting Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention relates to a regenerative green hydrogen-ammonia energy storage system, which comprises an electrolytic water hydrogen production subsystem, a cryogenic air molecular system, a synthetic ammonia subsystem and a heat recovery subsystem, wherein the hydrogen output end of the electrolytic water hydrogen production subsystem is connected with the input end of the synthetic ammonia subsystem; the nitrogen output end of the cryogenic air molecular system is connected with the input end of the synthesis ammonia subsystem, unreacted hydrogen and nitrogen which are separated out by the synthesis ammonia subsystem are conveyed to the heat recovery subsystem, the hydrogen end of the heat recovery subsystem is connected with the input end of the synthesis ammonia subsystem, and the public engineering water output end of the heat recovery subsystem is connected with the heat input ends of the electrolytic water hydrogen production subsystem and the synthesis ammonia subsystem. The cold and heat energy between different subsystems are utilized, the cold and heat energy between different components can be recovered and transported to the components requiring corresponding energy for energy cascade utilization, and the energy cascade utilization device is used for outputting ammonia gas and oxygen gas with high efficiency and storing energy, so that the problems of high energy consumption, heat pollution and low cold and heat energy utilization efficiency of the green hydrogen-ammonia system are solved.
Description
Technical Field
The invention relates to a regenerative green hydrogen ammonia energy storage system.
Background
Clean energy sources such as solar energy and wind energy have intermittence and volatility, so that the generated power of the new energy source is predicted, and the problems of unstable voltage, out-of-limit frequency and the like often occur. Ammonia is widely used in agriculture and industry fields, and has the advantages of large volume energy density, mature production technology, low toxicity and the like when being used as an energy carrier. In addition, the ammonia storage and transportation infrastructure is perfect, and the compression cost is low, so that the ammonia storage and transportation infrastructure has feasibility in both technical and economic aspects as an energy carrier.
The reaction of nitrogen and hydrogen to synthesize ammonia usually needs to be carried out under the action of a catalyst and the action of high temperature and high pressure, and a great amount of heat energy is often generated in the process. Meanwhile, the water needs to be heated before electrolysis, and the process of separating nitrogen from air is accompanied by a large amount of cold energy to be released. Therefore, if cold energy and heat energy flow between different components and are utilized, the whole energy consumption of the system can be reduced, and the heat pollution to the environment can be reduced.
Disclosure of Invention
The invention aims at improving the problems existing in the prior art, namely the technical problem to be solved by the invention is to provide a regenerative green hydrogen ammonia energy storage system.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows: the regenerative green hydrogen-ammonia energy storage system comprises an electrolytic water hydrogen production subsystem, a cryogenic air molecular system, a synthetic ammonia subsystem and a heat recovery subsystem, wherein the hydrogen output end of the electrolytic water hydrogen production subsystem is connected with the input end of the synthetic ammonia subsystem; the nitrogen output end of the cryogenic air molecular system is connected with the input end of the synthesis ammonia subsystem, unreacted hydrogen and nitrogen are separated by the synthesis ammonia subsystem and are conveyed to the heat recovery subsystem, the hydrogen end of the heat recovery subsystem is connected with the input end of the synthesis ammonia subsystem, and the public engineering water output end of the heat recovery subsystem is respectively connected with the heat input ends of the electrolytic water hydrogen production subsystem and the synthesis ammonia subsystem.
Further, the electrolytic water hydrogen production subsystem comprises a mixer A, an electrolytic tank, a flash tank A and a flash tank B, wherein a heat exchanger A is connected between the output end of the mixer A and the input end of the electrolytic tank, a heat exchanger B is connected between the cathode product output end of the electrolytic tank and the flash tank A, and a heat exchanger C is connected between the anode product output end of the electrolytic tank and the flash tank B; the synthesis ammonia subsystem comprises a mixer B, an air compression assembly, an ammonia synthesis reactor and a flash tank C which are sequentially connected, wherein the input end of the mixer B is connected with the exhaust end of the flash tank A; a heat exchanger D is arranged between the air compression assembly and the ammonia synthesis reactor, and a condenser A is arranged between the ammonia synthesis reactor and the flash tank C; the cryogenic air molecular system comprises an air compressor A, a heat exchanger E, a distillation tower and a heat exchanger F which are connected in sequence, wherein liquid nitrogen separated in the distillation tower is heated and gasified in the heat exchanger F and is sent into a mixer B; the heat recovery subsystem comprises a heat exchanger G, a condenser B and a flash tank D which are sequentially connected, unreacted hydrogen and nitrogen separated by the flash tank C sequentially pass through the heat exchanger G and the condenser B and then enter the flash tank D, and the hydrogen separated by the flash tank D is sent into the mixer B.
Further, the liquid water separated from the flash tank A and the flash tank B flows back to the mixer A.
Further, the air compression assembly comprises an air compressor B and an air compressor C which are sequentially arranged; the ammonia synthesis reactor comprises an ammonia synthesis reactor A, an ammonia synthesis reactor B and an ammonia synthesis reactor C which are sequentially arranged, the heat exchanger D is arranged between the air compressor C and the ammonia synthesis reactor A, a heat exchanger H is arranged between the ammonia synthesis reactor A and the ammonia synthesis reactor B, a heat exchanger I is arranged between the ammonia synthesis reactor B and the ammonia synthesis reactor C, and the condenser A is connected between the ammonia synthesis reactor C and the flash tank C; the heat exchanger F is also connected between the ammonia synthesis reactor C and the condenser A.
Further, a heat exchanger J is arranged between the hydrogen output end of the flash tank D and the input end of the mixer B.
Further, the heat recovery subsystem further comprises a mixer C and a public engineering water input system, the public engineering water input system is provided with a water outlet end A, a water outlet end B and a water outlet end C, the water outlet end A of the public engineering water input system is connected with the input end of the mixer C through a heat exchanger D, the water outlet end B of the public engineering water input system is connected with the input end of the mixer C through a heat exchanger B and a heat exchanger H in sequence, the water outlet end C of the public engineering water input system is connected with the input end of the mixer C through the heat exchanger C and a heat exchanger I in sequence, and the output water of the mixer C flows through the heat exchanger A and the heat exchanger J in sequence.
Further, the nitrogen separated from the flash tank D is sent to the heat exchanger E.
Further, a water pump is connected between the heat exchanger A and the mixer A.
Compared with the prior art, the invention has the following effects: the invention has reasonable design, utilizes cold and heat energy among different subsystems, can recycle the cold and heat energy among different components and convey the cold and heat energy to the components needing corresponding energy for energy cascade utilization, is used for outputting ammonia gas and oxygen gas with high efficiency and storing energy, and solves the problems of high energy consumption, heat pollution, low cold and heat energy utilization efficiency of the green hydrogen-ammonia system.
Drawings
Fig. 1 is a schematic configuration of an embodiment of the present invention.
In the figure:
1-a mixer a; 2-a water pump; 3-heat exchanger a; 4-an electrolytic cell; 5-a heat exchanger C; 6-a heat exchanger B; 7-flash tank a; 8-a flash tank B; 9-a mixer B; 10-an air compressor B; 11-an air compressor C; 12-a heat exchanger D; 13-ammonia synthesis reactor a; 14-a heat exchanger H; 15-an ammonia synthesis reactor B; 16-heat exchanger I; 17-ammonia synthesis reactor C; 18-a heat exchanger F; 19-a condenser a; 20-flash tank C; 21-heat exchanger G; 22-condenser B; 23-flash tank D; 24-air compressor a; 25-heat exchanger E; 26-a distillation column; 27-heat exchanger J; 28-a mixer C; 29-a hydrogen production subsystem by water electrolysis; 30-a cryogenic air molecular system; 31-a synthesis ammonia subsystem; 32-heat recovery subsystem.
Detailed Description
The invention will be described in further detail with reference to the drawings and the detailed description.
In the description of the present invention, it should be understood that the terms "longitudinal," "transverse," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like indicate or are based on the orientation or positional relationship shown in the drawings, merely to facilitate description of the present invention, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus should not be construed as limiting the present invention.
As shown in fig. 1, the regenerative green hydrogen-ammonia energy storage system comprises an electrolytic water hydrogen production subsystem 29, a cryogenic air molecular system 30, a synthetic ammonia subsystem 31 and a heat recovery subsystem 32, wherein the hydrogen output end of the electrolytic water hydrogen production subsystem 29 is connected with the input end of the synthetic ammonia subsystem 31; the nitrogen output end of the cryogenic air molecular system 30 is connected with the input end of the synthetic ammonia subsystem 31, and the hydrogen output by the electrolytic water hydrogen production subsystem and the nitrogen output by the cryogenic air molecular system are prepared into products NH 3 and other unreacted H 2 and N 2 in the synthetic ammonia subsystem; the unreacted hydrogen and nitrogen gas separated from the synthesis ammonia subsystem 31 are conveyed to a heat recovery subsystem 32, the hydrogen end of the heat recovery subsystem 32 is connected with the input end of the synthesis ammonia subsystem 31, and the public engineering water output end of the heat recovery subsystem 32 is respectively connected with the heat input ends of the electrolytic water hydrogen production subsystem 29 and the synthesis ammonia subsystem 31.
In this embodiment, the hydrogen production subsystem 29 by electrolyzing water includes a mixer A1, an electrolyzer 4, a flash tank A7 and a flash tank B8, a heat exchanger A3 is connected between the output end of the mixer A1 and the input end of the electrolyzer 4, and a water pump 2 is connected between the heat exchanger A3 and the mixer A1; a heat exchanger B6 is connected between the cathode product output end of the electrolytic tank 4 and the flash tank A7, and a heat exchanger C5 is connected between the anode product output end of the electrolytic tank 4 and the flash tank B8; the liquid water separated from flash tank A7 and flash tank B8 is returned to mixer A1. When the device works, water enters the electrolytic water hydrogen production subsystem at 25 ℃ and 1bar, is preheated by the heat exchanger A3 and enters the electrolytic tank 4 after being pressurized by the water pump 2, the electrolytic tank electrolyzes the water, H 2 is separated out at the cathode of the electrolytic tank 4, is cooled by the heat exchanger B6 and then enters the flash tank A7 to be separated, and is then sent to the synthesis ammonia subsystem; and the byproduct O 2 is obtained from the anode of the electrolytic tank 4, cooled in the heat exchanger C5 and purified and separated in the flash tank B8. The liquid water separated from flash tank A7 and flash tank B8 is mixed with the feed water in mixer A1 and again flows into the electrolyzer.
In this embodiment, the cryogenic air molecular system 30 includes an air compressor a24, a heat exchanger E25, a distillation column 26 and a heat exchanger F18, which are sequentially connected, wherein air is compressed in the air compressor a24, cooled to a liquid state at a low temperature in the heat exchanger E25, then sent to the distillation column 26 to separate N 2, and liquid nitrogen separated in the distillation column 26 is heated and gasified in the heat exchanger F18 and sent to the ammonia synthesis subsystem 31.
In this embodiment, the ammonia synthesis subsystem 31 includes a mixer B9, an air compression assembly, an ammonia synthesis reactor and a flash tank C20 connected in sequence, wherein an input end of the mixer B9 is connected to the flash tank A7 and an exhaust end of the heat exchanger F18, H 2 separated in the flash tank A7 is input to the mixer B9, and liquid nitrogen separated in the distillation column 26 is heated and gasified in the heat exchanger F18 and is sent to the mixer B9; a heat exchanger D12 is arranged between the air compression assembly and the ammonia synthesis reactor, and a condenser A19 is arranged between the ammonia synthesis reactor and the flash tank C20. Further, the air compression assembly comprises an air compressor B10 and an air compressor C11 which are sequentially arranged; the ammonia synthesis reactor comprises an ammonia synthesis reactor A13, an ammonia synthesis reactor B15 and an ammonia synthesis reactor C17 which are sequentially arranged, the heat exchanger D12 is arranged between the air compressor C11 and the ammonia synthesis reactor A13, a heat exchanger H14 is arranged between the ammonia synthesis reactor A13 and the ammonia synthesis reactor B15, a heat exchanger I16 is arranged between the ammonia synthesis reactor B15 and the ammonia synthesis reactor C17, and the condenser A19 is connected between the ammonia synthesis reactor C17 and the flash tank C20; the heat exchanger F18 is also connected between the ammonia synthesis reactor C17 and the condenser a19. In operation, the separated liquid N 2 is heated to gasify in heat exchanger F18 and fed into mixer B9 to be mixed with H 2 from electrolyzer 4, the mixture of H 2 and N 2 is compressed to operating pressure by air compressor B10 and air compressor C11 and heat exchange takes place in heat exchanger D12 to operating temperature. Subsequently, the mixture undergoes an ammonia synthesis reaction in ammonia synthesis reactor a13, ammonia synthesis reactor B15 and ammonia synthesis reactor C17, and the reaction gas is cooled in heat exchangers H14, I16 provided between the reactors to maintain a desired reaction balance. NH 3 from the outlet of the ammonia synthesis reactor C17 is pre-cooled in heat exchanger F18 while recovering heat energy to gasify the air separated N 2, after which the product NH 3 is condensed in condenser a19 and then separated in flash tank C20 to yield product NH 3 and other unreacted H 2 and N 2.
In this embodiment, the heat recovery subsystem 32 includes a heat exchanger G21, a condenser B22, and a flash tank D23 connected in sequence, where the unreacted hydrogen and nitrogen separated by the flash tank C20 sequentially pass through the heat exchanger G21 and the condenser B22 and then enter the flash tank D23, where H 2 is recovered in the flash tank D23 and sent to the mixer B9 to be mixed with the H 2/N2 mixture, so as to reduce the cost of the system. While the nitrogen separated in flash drum D23 is sent to heat exchanger E25, the separated N 2 is used to cool the feed air in the air separation to recover cold energy, and N 2 is then released to the environment.
In this embodiment, a heat exchanger J27 is disposed between the hydrogen output end of the flash tank D23 and the input end of the mixer B9.
In this embodiment, the heat recovery subsystem 32 further includes a mixer C28 and a utility water input system, where the utility water input system has a water outlet end a, a water outlet end B, and a water outlet end C, the water outlet end a of the utility water input system is connected to the input end of the mixer C28 through a heat exchanger D12, the water outlet end B of the utility water input system is connected to the input end of the mixer C28 through a heat exchanger B6 and a heat exchanger H14 in sequence, the water outlet end C of the utility water input system is connected to the input end of the mixer C28 through a heat exchanger C5 and a heat exchanger I16 in sequence, and the output water of the mixer C flows through the heat exchanger a and the heat exchanger J in sequence. The utility water enters the system and is split into three sections, wherein the two sections cool the water exiting the electrolyzer in heat exchanger C5 and heat exchanger B6, respectively, and then enter the heat exchanger H14 and heat exchanger I16 between the ammonia synthesis reactors to continue to cool the gas at the ammonia synthesis reactor outlet. The other part directly enters the heat exchanger D12 to cool the high-pressure H 2/N2 mixture which is warmed up due to being compressed. The three portions of utility water are then mixed in mixer C28, and passed successively to heat exchanger A3 to heat the feed water to be passed to the electrolyzer and heat exchanger 27J to heat the separated recovered H 2.
The specific implementation process comprises the following steps:
In the start-up phase, water enters the system at 25 ℃ and 1bar, is pressurized by the water pump 2, preheated by the heat exchanger A3 and fed into the electrolytic tank 4.H 2 is separated out at the cathode of the electrolytic tank 4, cooled by the heat exchanger B6, separated in the flash tank A7 and sent to the next unit, and the byproduct O 2 is obtained at the anode of the electrolytic tank 4, cooled by the heat exchanger C5 and purified and separated in the flash tank B8. The liquid water separated from flash tank A7 and flash tank B8 is mixed with the feed water in mixer A1 and again flows into the electrolytic tank 4.
Meanwhile, after being compressed in the air compressor a24, the air is cryogenically cooled to a liquid state in the heat exchanger E25, and then sent to the distillation column 26 to separate N 2. The separated liquid N 2 is gasified by heating in the heat exchanger F18 and fed into the mixer B9 to be mixed with H 2 from the electrolytic tank 4. The mixture of H 2 and N 2 is compressed to operating pressure by air compressor a24 and air compressor B10 and heat exchange takes place in heat exchanger D12 to operating temperature. Subsequently, the mixture undergoes an ammonia synthesis reaction in ammonia synthesis reactor a13, ammonia synthesis reactor B15, ammonia synthesis reactor C17, and the reaction gas is cooled in heat exchanger H14, heat exchanger I16 between the ammonia synthesis reactors to maintain a desired reaction balance. NH 3 from the outlet of the ammonia synthesis reactor C17 is pre-cooled in heat exchanger F18 while recovering thermal energy to gasify the air separated N 2. Product NH 3 is then condensed in condenser a19 and then separated in flash tank C20 to yield product NH 3 and other unreacted H 2 and N 2, which are cooled in heat exchanger G21 and condensed in condenser B22, recovered in flash tank D23, H 2 and sent to mixer B9 to mix with the H 2/N2 mixture to reduce the cost of the system. While the separated N 2 is used to cool the feed air in the air separation to recover cold energy, N 2 is then released into the environment.
In addition, the system adds utility water to improve the fluidity of the energy. After entering the system, the utility water at 25 ℃ and 1bar is split into three parts, wherein the two parts cool the water coming out of the electrolytic cell 4 in heat exchangers C5 and B6, respectively, and then enter the heat exchanger H14 and the heat exchanger I16 between the ammonia synthesis reactors for further cooling the gas at the outlet of the ammonia synthesis reactor. The other part directly enters the heat exchanger D12 to cool the high-pressure H 2/N2 mixture which is warmed up due to being compressed. The three parts of utility water are then mixed in mixer C28, successively entering heat exchanger A3 to heat the feed water to be fed to the electrolyzer 4 and heat exchanger J27 to heat the separated recovered H 2.
The invention has the advantages that: the system efficiently utilizes cold energy and heat energy among different subsystems in the green hydrogen ammonia synthesis system, can recover the cold energy and the heat energy among different components and convey the cold energy and the heat energy to the components needing corresponding energy for energy cascade utilization, is used for efficiently outputting ammonia gas and oxygen gas and storing energy, and solves the problems of high energy consumption, heat pollution, low cold energy utilization efficiency and low heat energy utilization efficiency of the green hydrogen ammonia system.
If the invention discloses or relates to components or structures fixedly connected with each other, then unless otherwise stated, the fixed connection is understood as: detachably fixed connection (e.g. using bolts or screws) can also be understood as: the non-detachable fixed connection (e.g. riveting, welding), of course, the mutual fixed connection may also be replaced by an integral structure (e.g. integrally formed using a casting process) (except for obviously being unable to use an integral forming process).
In addition, terms used in any of the above-described aspects of the present disclosure to express positional relationship or shape have meanings including a state or shape similar to, similar to or approaching thereto unless otherwise stated.
Any part provided by the invention can be assembled by a plurality of independent components, or can be manufactured by an integral forming process.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention and not for limiting the same; while the invention has been described in detail with reference to the preferred embodiments, those skilled in the art will appreciate that: modifications may be made to the specific embodiments of the present invention or equivalents may be substituted for part of the technical features thereof; without departing from the spirit of the invention, it is intended to cover the scope of the invention as claimed.
Claims (4)
1. A regenerative green hydrogen ammonia energy storage system is characterized in that: the system comprises an electrolytic water hydrogen production subsystem, a cryogenic air molecular system, a synthetic ammonia subsystem and a heat recovery subsystem, wherein the hydrogen output end of the electrolytic water hydrogen production subsystem is connected with the input end of the synthetic ammonia subsystem; the nitrogen output end of the cryogenic air molecular system is connected with the input end of the synthesis ammonia subsystem, unreacted hydrogen and nitrogen are separated by the synthesis ammonia subsystem and are conveyed to the heat recovery subsystem, the hydrogen end of the heat recovery subsystem is connected with the input end of the synthesis ammonia subsystem, and the public engineering water output end of the heat recovery subsystem is respectively connected with the heat input ends of the electrolytic water hydrogen production subsystem and the synthesis ammonia subsystem;
The hydrogen production subsystem by electrolyzing water comprises a mixer A, an electrolytic tank, a flash tank A and a flash tank B, wherein a heat exchanger A is connected between the output end of the mixer A and the input end of the electrolytic tank, a heat exchanger B is connected between the output end of a cathode product of the electrolytic tank and the flash tank A, and a heat exchanger C is connected between the output end of an anode product of the electrolytic tank and the flash tank B; the synthesis ammonia subsystem comprises a mixer B, an air compression assembly, an ammonia synthesis reactor and a flash tank C which are sequentially connected, wherein the input end of the mixer B is connected with the exhaust end of the flash tank A; a heat exchanger D is arranged between the air compression assembly and the ammonia synthesis reactor, and a condenser A is arranged between the ammonia synthesis reactor and the flash tank C; the cryogenic air molecular system comprises an air compressor A, a heat exchanger E, a distillation tower and a heat exchanger F which are connected in sequence, wherein liquid nitrogen separated in the distillation tower is heated and gasified in the heat exchanger F and is sent into a mixer B; the heat recovery subsystem comprises a heat exchanger G, a condenser B and a flash tank D which are sequentially connected, unreacted hydrogen and nitrogen separated by the flash tank C sequentially pass through the heat exchanger G and the condenser B and then enter the flash tank D, and the hydrogen separated by the flash tank D is sent into the mixer B;
The air compression assembly comprises an air compressor B and an air compressor C which are sequentially arranged; the ammonia synthesis reactor comprises an ammonia synthesis reactor A, an ammonia synthesis reactor B and an ammonia synthesis reactor C which are sequentially arranged, the heat exchanger D is arranged between the air compressor C and the ammonia synthesis reactor A, a heat exchanger H is arranged between the ammonia synthesis reactor A and the ammonia synthesis reactor B, a heat exchanger I is arranged between the ammonia synthesis reactor B and the ammonia synthesis reactor C, and the condenser A is connected between the ammonia synthesis reactor C and the flash tank C; the heat exchanger F is also connected between the ammonia synthesis reactor C and the condenser A;
a heat exchanger J is arranged between the hydrogen output end of the flash tank D and the input end of the mixer B;
the heat recovery subsystem further comprises a mixer C and a public engineering water input system, the public engineering water input system is provided with a water outlet end A, a water outlet end B and a water outlet end C, the water outlet end A of the public engineering water input system is connected with the input end of the mixer C through a heat exchanger D, the water outlet end B of the public engineering water input system is connected with the input end of the mixer C through a heat exchanger B and a heat exchanger H in sequence, the water outlet end C of the public engineering water input system is connected with the input end of the mixer C through the heat exchanger C and the heat exchanger I in sequence, and the output water of the mixer C flows through the heat exchanger A and the heat exchanger J in sequence.
2. The regenerative green ammonia storage system of claim 1, wherein: the liquid water separated from the flash tank A and the flash tank B flows back to the mixer A.
3. The regenerative green ammonia storage system of claim 1, wherein: the nitrogen separated from the flash tank D is sent to a heat exchanger E.
4. The regenerative green ammonia storage system of claim 1, wherein: a water pump is connected between the heat exchanger A and the mixer A.
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| 气头合成氨装置节能优化分析;孟硕;;石油石化绿色低碳;20180420(第02期);全文 * |
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| CN115928105A (en) | 2023-04-07 |
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