CN114718679A - Liquefied natural gas cold energy power generation and synthetic ammonia combined system - Google Patents
Liquefied natural gas cold energy power generation and synthetic ammonia combined system Download PDFInfo
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- CN114718679A CN114718679A CN202210348334.2A CN202210348334A CN114718679A CN 114718679 A CN114718679 A CN 114718679A CN 202210348334 A CN202210348334 A CN 202210348334A CN 114718679 A CN114718679 A CN 114718679A
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 247
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 119
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 72
- 238000010248 power generation Methods 0.000 title claims abstract description 26
- 239000007789 gas Substances 0.000 claims abstract description 91
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 81
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 63
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 44
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 25
- 239000003345 natural gas Substances 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 14
- 239000001257 hydrogen Substances 0.000 claims description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 5
- 238000002309 gasification Methods 0.000 claims 1
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 150000002431 hydrogen Chemical class 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 3
- 239000013535 sea water Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
- C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
- C01C1/0488—Processes integrated with preparations of other compounds, e.g. methanol, urea or with processes for power generation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D3/00—Devices using other cold materials; Devices using cold-storage bodies
- F25D3/10—Devices using other cold materials; Devices using cold-storage bodies using liquefied gases, e.g. liquid air
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The invention relates to a liquefied natural gas cold energy power generation and synthetic ammonia combined system, which comprises an LNG cold energy power generation system and a synthetic ammonia system; the ammonia synthesis system and the LNG cold energy power generation system are coupled by three heat exchangers so as to condense the synthesis gas produced by the ammonia synthesis system through the LNG cold energy. The invention realizes the cascade high-efficiency utilization of LNG cold energy while condensing and separating liquid ammonia, thereby achieving the purposes of energy conservation and environmental protection.
Description
Technical Field
The invention belongs to the technical field of energy conservation and environmental protection, and particularly relates to a liquefied natural gas cold energy power generation and ammonia synthesis combined system and method.
Background
Liquefied Natural Gas (LNG) is an energy source which is low in transportation cost, energy-saving, environment-friendly, safe and reliable. Compared with fossil energy sources such as coal, petroleum and the like, the natural gas has low impurity content, generates less harmful gas after being fully combusted, has high combustion heat value and energy density, and is considered as the cleanest fossil energy on the earth. Generally, LNG is transported by sea, and at a receiving end, seawater is generally used as a heat source to directly heat and vaporize the LNG into natural gas, which is then sent to a pipeline network. LNG is usually stored at low temperature and normal pressure, the temperature is about-162 ℃, a large amount of cold energy is contained, and the cold energy is completely wasted by directly exchanging heat with seawater.
Ammonia is one of the most important basic chemical products, and the yield of the ammonia is the first of various chemical products. Because the synthesis rate of ammonia in the ammonia synthesis process is low, and the generated synthesis gas contains a large amount of unreacted gas, the ammonia is separated by adopting a condensation method, and the process consumes a large amount of energy.
Disclosure of Invention
In view of the above, the present invention provides a combined system and method for liquefied natural gas cold energy power generation and ammonia synthesis, which can output electric energy while condensing and separating liquid ammonia, thereby not only realizing the cascade efficient utilization of LNG cold energy, but also reducing the energy consumption of the ammonia synthesis process.
In order to achieve the purpose, the invention adopts the following technical scheme:
a liquefied natural gas cold energy power generation and synthetic ammonia combined system comprises an LNG cold energy power generation system and a synthetic ammonia system; the ammonia synthesis system and the LNG cold energy power generation system are coupled by three heat exchangers so as to condense ammonia gas in the synthesis gas produced by the ammonia synthesis system through LNG cold energy.
Further, the ammonia synthesis system comprises a mixer I, a mixer II, a mixer III, a multi-stage compressor, a heat exchanger I, a heat exchanger II, a heat exchanger III, a heat exchanger IV, a heat exchanger V, a heat exchanger VI, a first-stage ammonia synthesis reaction tower, a second-stage ammonia synthesis reaction tower, a third-stage ammonia synthesis reaction tower, a water cooler I, a water cooler II, a water cooler III, an ammonia separator and an ammonia flash tank; the mixer I, the multistage compressor, the mixer II, the compressor and the heat exchanger I are sequentially connected on the cold side of the synthesis gas; the first section of synthetic ammonia reaction tower, the synthesis gas hot side of the heat exchanger II, the water cooler I, the second section of synthetic ammonia reaction tower, the water cooler II, the third section of synthetic ammonia reaction tower, the water cooler III, the synthesis gas hot side of the heat exchanger I, the synthesis gas side of the heat exchanger III and the synthesis gas hot side of the heat exchanger IV are sequentially connected; the synthesis gas cold side of the heat exchanger I is also connected with the synthesis gas cold side of the heat exchanger II; the cold side of the synthesis gas of the heat exchanger IV is also respectively connected with a mixer III and a mixer II; the mixer III is also respectively connected with an ammonia separator and an ammonia flash tank; the ammonia flash tank is also connected with an ammonia separator.
Further, the LNG cold energy power generation system comprises an LNG storage tank, an LNG pump, an expander, a power generator, an auxiliary heater, a heat exchanger III, a heat exchanger V and a heat exchanger VI; the LNG pump is connected with the LNG storage tank, the heat exchanger III natural gas side, the heat exchanger VI natural gas side, the heat exchanger V natural gas side, the expansion machine and the auxiliary heater in sequence.
The working principle of the liquefied natural gas cold energy power generation and ammonia synthesis combined system comprises the following steps:
the mixer I receives fresh nitrogen and hydrogen, and mixed gas is introduced into a multistage compressor;
the mixer II receives the gas 104 from the compressor multistage compressor and the excessive gas 126 after the synthetic ammonia is separated out, and the excessive gas is mixed to obtain mixed gas 105;
the compressor receives and compresses the mixed gas 105 to obtain compressed gas 106, and then the compressed gas 106 is preheated by the heat exchanger I and the heat exchanger II respectively to form mixed gas 108;
the mixed gas 108 is firstly introduced into a first section of synthetic ammonia reaction tower for ammonia synthesis reaction, is cooled by a heat exchanger II and a water cooler I after reaction, then enters a second section of synthetic ammonia reaction tower for ammonia synthesis reaction, is cooled by the water cooler II, then enters a third section of synthetic ammonia reaction tower for ammonia synthesis reaction, and is cooled by the water cooler III and the heat exchanger I to form the mixed synthetic gas 116;
the mixed synthesis gas 116 is cooled by sequentially passing through a heat exchanger III, a heat exchanger IV, a heat exchanger V and a heat exchanger VI to become a mixed synthesis gas 120;
the ammonia separator separates liquid ammonia 121 at the bottom of the tower, the rest of mixed gas 124 of hydrogen, nitrogen and ammonia is separated from the top of the tower, and the mixed gas 124 is conveyed to the mixer III; the liquid ammonia 121 separated from the bottom of the ammonia separator is conveyed to an ammonia flash tank for further purification;
the ammonia flash tank separates high purity liquid ammonia 122 and excess hydrogen, nitrogen, ammonia mixture 123. The excessive hydrogen, nitrogen and ammonia mixed gas 123 is conveyed to the mixer III to be mixed with the excessive hydrogen, nitrogen and ammonia mixed gas 124, the mixed gas 125 is conveyed to the heat exchanger IV to be preheated, and then is conveyed to the mixer II together with the gas 104 from the multistage compressor to be mixed, and the next synthetic ammonia cycle is started;
the crude synthesis gas which completes the three-stage synthesis ammonia reaction is condensed by LNG. The liquefied natural gas in the LNG storage tank is pressurized by an LNG pump to become supercooled liquefied natural gas, then the crude synthesis gas is condensed by the heat exchangers III, VI and V in sequence, the heat released by the crude synthesis gas is received, and the natural gas is gasified to become natural gas 205; (205 Natural gas obtained by gasifying liquefied natural gas after absorbing Heat from raw Synthesis gas)
Then the natural gas enters an expansion machine to be expanded so as to output mechanical work, and the expansion machine is rigidly connected with a generator to finish the conversion from mechanical energy to electric energy;
the pressure of the expanded natural gas is reduced to the pressure of a pipe network, and the natural gas is heated by seawater through an auxiliary heater and then is conveyed to the pipe network for users to use.
Further, the liquefied natural gas of the LNG storage tank is heated to above zero by the auxiliary heater at the temperature of-162 ℃ and the pressure of 0.1 MPa.
Compared with the prior art, the invention has the following beneficial effects:
the invention realizes the condensation separation of ammonia gas in the ammonia synthesis process by using LNG cold energy instead of the traditional refrigeration mode, and can greatly reduce the energy consumption of the ammonia synthesis process. Meanwhile, LNG absorbs heat generated in the ammonia synthesis process, and the gasified LNG enters an expansion machine to directly expand to do work to drive a generator to rotate so as to convert mechanical energy into electric energy to be output. Through the organic combination of the LNG direct expansion power generation and the ammonia synthesis process and the efficient matching of the heat exchange process, the LNG cold energy can be recycled in a gradient manner to output electric energy externally, and the energy consumption of the ammonia synthesis process can be reduced.
Drawings
FIG. 1 is a schematic diagram of the system architecture of the present invention;
in the figure: 1-mixer I, 2-multistage compressor, 3-mixer II, 4-compressor, 5-heat exchanger I, 6-heat exchanger II, 7-first section synthetic ammonia reaction tower, 8-water cooler I, 9-second section synthetic ammonia reaction tower, 10-water cooler II, 11-third section synthetic ammonia reaction tower, 12-water cooler III, 13-heat exchanger III, 14-heat exchanger IV, 15-heat exchanger V, 16-heat exchanger VI, 17-ammonia separator, 18-ammonia flash tank, 19-mixer III, 20-LNG storage tank, 21-LNG pump, 22-expander, 23-generator and 24-auxiliary heater.
Detailed Description
The invention is further explained below with reference to the drawings and the embodiments.
Referring to fig. 1, the invention provides a liquefied natural gas cold energy power generation and ammonia synthesis combined system, which comprises an LNG cold energy power generation system and an ammonia synthesis system; the synthetic ammonia system comprises three mixers 1, 3 and 19, two compressors 2 and 4, three heat exchangers 5, 6 and 14, three synthetic ammonia reaction towers 7, 9 and 11, three water coolers 8, 10 and 12, an ammonia separator and an ammonia flash tank; the LNG cold energy power generation system comprises an LNG storage tank, an LNG pump, an expander, a power generator and an auxiliary heater. The ammonia synthesis system is coupled to the LNG cold energy power generation system by heat exchangers 13, 15, 16 to condense the synthesis gas produced by the ammonia synthesis system from the LNG cold energy.
The mixer 1 receives fresh nitrogen 101 and hydrogen 102, and the mixed gas is introduced into the multistage compressor 2 for pressurization;
the mixer 3 receives the gas 104 from the compressor 2 and the excessive gas 126 separated from the synthetic ammonia to mix, and the mixed gas is 105;
the compressor 4 receives and compresses the gas 105, and then the compressed gas 106 is preheated by the heat exchanger 5 and the heat exchanger 6 respectively to become mixed gas 108;
the mixed gas 108 is introduced into the first-stage ammonia synthesis reaction tower 7 to carry out ammonia synthesis reaction, after the reaction, the mixed gas is cooled by the heat exchanger 6 and the water cooler 8, enters the second-stage ammonia synthesis reaction tower 9 to carry out ammonia synthesis reaction, is cooled by the water cooler 10, enters the third-stage ammonia synthesis reaction tower 11 to carry out ammonia synthesis reaction, and is cooled by the water cooler 12 and the heat exchanger 5 to form the mixed gas 116.
The mixed gas 116 is cooled by the heat exchanger 13, the heat exchanger 14, the heat exchanger 15 and the heat exchanger 16 in sequence to become mixed gas 120.
The ammonia separator 17 separates liquid ammonia 121 from the bottom of the tower and excessive mixed gas 124 of hydrogen, nitrogen and ammonia from the top of the tower, and the mixed gas 124 is sent to the mixer 19; the bottom liquid ammonia 121 is sent to the ammonia flash tank 18 for further purification.
The ammonia flash tank separates high-purity liquid ammonia 122 and excessive mixed gas 123 of hydrogen, nitrogen and ammonia, the excessive gas 123 is conveyed to the mixer 19 to be mixed with the mixed gas 124, the mixed gas 125 is conveyed to the heat exchanger 14 to be preheated, and then is conveyed to the mixer 3 together with the mixed gas 104 to be mixed, and the next synthetic ammonia cycle is carried out.
The raw synthesis gas 116, which completes the three-stage synthesis ammonia reaction, is condensed by LNG. The liquefied natural gas 201 in the LNG storage tank 20 has a temperature of-162 ℃ and a pressure of 0.1MPa, is pressurized to 10MPa by the LNG pump 21 to become subcooled liquefied natural gas 202, and then passes through the heat exchangers 13, 16, and 15 to condense the raw synthesis gas, receive the heat released by the raw synthesis gas, and is gasified to become natural gas 205. The natural gas then enters the expander 22 to expand to output mechanical work, which is rigidly connected to the generator 23, completing the conversion of mechanical energy into electrical energy. The pressure of the expanded natural gas is reduced to 5MPa of the pressure of the pipe network, and the natural gas is heated to above zero degree by the auxiliary heater 24 and then enters the pipe network for users to use.
The above description is only a preferred embodiment of the present invention, and all the equivalent changes and modifications made according to the claims of the present invention should be covered by the present invention.
Claims (5)
1. A liquefied natural gas cold energy power generation and synthetic ammonia combined system is characterized by comprising an LNG cold energy power generation system and a synthetic ammonia system; the synthetic ammonia system and the LNG cold energy power generation system are coupled through three heat exchangers so as to condense the synthetic gas produced by the synthetic ammonia system through the LNG cold energy.
2. The integrated liquefied natural gas cold energy power generation and ammonia synthesis system of claim 1, wherein the integrated liquefied natural gas cold energy power generation and ammonia synthesis system comprises a mixer I, a mixer II, a mixer III, a multistage compressor, a heat exchanger I, a heat exchanger II, a heat exchanger III, a heat exchanger IV, a heat exchanger V, a heat exchanger VI, a first-stage ammonia synthesis reaction tower, a second-stage ammonia synthesis reaction tower, a third-stage ammonia synthesis reaction tower, a water cooler I, a water cooler II, a water cooler III, an ammonia separator and an ammonia flash tank; the mixer I, the multistage compressor, the mixer II, the compressor and the heat exchanger I are sequentially connected on the cold side of the synthesis gas; the first section of synthetic ammonia reaction tower, the synthesis gas hot side of the heat exchanger II, the water cooler I, the second section of synthetic ammonia reaction tower, the water cooler II, the third section of synthetic ammonia reaction tower, the water cooler III, the synthesis gas hot side of the heat exchanger I, the synthesis gas side of the heat exchanger III and the synthesis gas hot side of the heat exchanger IV are sequentially connected; the synthesis gas cold side of the heat exchanger I is also connected with the synthesis gas cold side of the heat exchanger II; the cold side of the synthesis gas in the heat exchanger IV is also respectively connected with a mixer III and a mixer II; the mixer III is also respectively connected with an ammonia separator and an ammonia flash tank; the ammonia flash tank is also connected with an ammonia separator.
3. The LNG cold energy power generation and ammonia synthesis combined system of claim 2, wherein the LNG cold energy power generation system comprises an LNG storage tank, an LNG pump, an expander, a generator, an auxiliary heater, a heat exchanger III, a heat exchanger V and a heat exchanger VI; the LNG pump is sequentially connected with the LNG storage tank, the heat exchanger III natural gas side, the heat exchanger VI natural gas side, the heat exchanger V natural gas side, the expansion machine and the auxiliary heater.
4. A control method of a liquefied natural gas cold energy power generation and ammonia synthesis combined system is characterized by comprising the following steps:
the mixer I receives fresh nitrogen and hydrogen, and mixed gas is introduced into a multistage compressor;
the mixer II receives the gas 104 from the multistage compressor and the gas 126 after the synthesis ammonia is separated, and the gas is mixed to obtain mixed gas 105;
the compressor receives and compresses the mixed gas 105 to obtain compressed gas 106, and then the compressed gas 106 is preheated by the heat exchanger I and the heat exchanger II respectively to form mixed gas 108;
the mixed gas 108 is firstly introduced into a first section of synthetic ammonia reaction tower for ammonia synthesis reaction, cooled by a heat exchanger II and a water cooler I after the reaction, enters a second section of synthetic ammonia reaction tower for ammonia synthesis reaction, cooled by the water cooler II, enters a third section of synthetic ammonia reaction tower for ammonia synthesis reaction, and cooled by a water cooler III and the heat exchanger I to form the synthetic gas 116;
the synthesis gas 116 is cooled by passing through a heat exchanger III, a heat exchanger IV, a heat exchanger V and a heat exchanger VI in sequence to become synthesis gas 120;
the ammonia separator separates liquid ammonia 121 at the bottom of the tower, the rest of mixed gas 124 of hydrogen, nitrogen and ammonia is separated from the top of the tower, and the mixed gas 124 is conveyed to the mixer III; the liquid ammonia 121 separated from the bottom of the ammonia separator is conveyed to an ammonia flash tank for further purification;
the ammonia flash tank separates high-purity liquid ammonia 122 and a mixed gas 123 of hydrogen, nitrogen and ammonia; the mixed gas 123 of hydrogen, nitrogen and ammonia is delivered to the mixer III to be mixed with the mixed gas 124 of hydrogen, nitrogen and ammonia, the mixed gas 125 is delivered to the heat exchanger IV to be preheated, and then is mixed with the gas 104 from the multistage compressor in the mixer II to enter the next synthetic ammonia cycle;
the crude synthesis gas which completes the three-stage synthesis ammonia reaction is condensed by LNG. The liquefied natural gas in the LNG storage tank is pressurized by an LNG pump to become supercooled liquefied natural gas, then the crude synthesis gas is condensed by the heat exchangers III, VI and V in sequence, the heat released by the crude synthesis gas is received, and the natural gas is obtained after gasification;
then the natural gas enters an expansion machine to expand so as to output mechanical work, and the expansion machine is rigidly connected with a generator to finish the conversion from mechanical energy to electric energy;
and the pressure of the expanded natural gas is reduced to the pressure of a pipe network, and the natural gas is heated by an auxiliary heater and then is conveyed to the pipe network for users to use.
5. The method for controlling the LNG cold energy power generation and ammonia synthesis combined system according to claim 4, wherein the LNG storage tank is heated to a temperature of-162 ℃ and a pressure of 0.1MPa by the auxiliary heater.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210348334.2A CN114718679A (en) | 2022-04-01 | 2022-04-01 | Liquefied natural gas cold energy power generation and synthetic ammonia combined system |
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| CN202210348334.2A CN114718679A (en) | 2022-04-01 | 2022-04-01 | Liquefied natural gas cold energy power generation and synthetic ammonia combined system |
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| CN114718679A true CN114718679A (en) | 2022-07-08 |
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| CN202210348334.2A Pending CN114718679A (en) | 2022-04-01 | 2022-04-01 | Liquefied natural gas cold energy power generation and synthetic ammonia combined system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115991493A (en) * | 2023-02-17 | 2023-04-21 | 福州大学 | Open heat pump air separation and high-efficient synthetic ammonia system based on LNG cold energy |
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| CN203463934U (en) * | 2013-07-30 | 2014-03-05 | 江苏中核华纬工程设计研究有限公司 | Synthetic ammonia purge gas treatment device utilizing liquefied natural gas cold energy |
| EP3623343A1 (en) * | 2018-09-11 | 2020-03-18 | Casale Sa | Process for the synthesis of ammonia |
| CN111547740A (en) * | 2020-03-24 | 2020-08-18 | 福州大学化肥催化剂国家工程研究中心 | Synthetic ammonia separation process |
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2022
- 2022-04-01 CN CN202210348334.2A patent/CN114718679A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US20120067059A1 (en) * | 2009-05-26 | 2012-03-22 | Jgc Corporation | Process for recovery of carbon dioxide from a fluid stream, in particular from syngas |
| CN102229434A (en) * | 2011-04-05 | 2011-11-02 | 宁波金远东工业科技有限公司 | Apparatus for joint production of methanol and synthetic ammonia by using exhaust gas from methanol synthesis |
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| EP3623343A1 (en) * | 2018-09-11 | 2020-03-18 | Casale Sa | Process for the synthesis of ammonia |
| CN111547740A (en) * | 2020-03-24 | 2020-08-18 | 福州大学化肥催化剂国家工程研究中心 | Synthetic ammonia separation process |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115991493A (en) * | 2023-02-17 | 2023-04-21 | 福州大学 | Open heat pump air separation and high-efficient synthetic ammonia system based on LNG cold energy |
| CN115991493B (en) * | 2023-02-17 | 2024-06-07 | 福州大学 | Open heat pump air separation and high-efficient synthetic ammonia system based on LNG cold energy |
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Application publication date: 20220708 |