CN221032782U - Supercritical carbon dioxide power generation coupling ammonia alcohol co-production system - Google Patents
Supercritical carbon dioxide power generation coupling ammonia alcohol co-production system Download PDFInfo
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- CN221032782U CN221032782U CN202323214537.1U CN202323214537U CN221032782U CN 221032782 U CN221032782 U CN 221032782U CN 202323214537 U CN202323214537 U CN 202323214537U CN 221032782 U CN221032782 U CN 221032782U
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- carbon dioxide
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- ammonia
- methanol
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 160
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 146
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 80
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 80
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 75
- 238000010248 power generation Methods 0.000 title claims abstract description 49
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 230000008878 coupling Effects 0.000 title claims abstract description 15
- 238000010168 coupling process Methods 0.000 title claims abstract description 15
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 15
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 200
- 238000000926 separation method Methods 0.000 claims abstract description 67
- 238000002360 preparation method Methods 0.000 claims abstract description 41
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 35
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 35
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 239000001257 hydrogen Substances 0.000 claims abstract description 32
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 32
- 230000001105 regulatory effect Effects 0.000 claims abstract description 16
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 40
- 239000007789 gas Substances 0.000 claims description 34
- 239000003345 natural gas Substances 0.000 claims description 20
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 26
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 13
- 239000000126 substance Substances 0.000 abstract description 8
- 239000002994 raw material Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 230000002194 synthesizing effect Effects 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a supercritical carbon dioxide power generation coupling ammonia alcohol co-production system, and relates to the technical field of energy and chemical treatment. The system comprises an ammonia preparation system and a methanol preparation system which are connected with a supercritical carbon dioxide power generation system, wherein the methanol preparation system comprises a pressure regulating valve, a third three-way valve, a hydrogen compressor, a fourth three-way valve, a methanol synthesis device and a methanol separation device, the pressure regulating valve is sequentially connected with the third three-way valve, the methanol synthesis device and the methanol separation device, the fourth three-way valve is connected with a hydrogen supply device, the methanol separation device is connected with the fourth three-way valve, the fourth three-way valve is connected with the hydrogen compressor, and the hydrogen compressor is connected with the third three-way valve. According to the utility model, the supercritical carbon dioxide power generation system, the ammonia preparation system and the methanol preparation system are coupled, so that the efficiency of the supercritical carbon dioxide power generation system is improved, and the problems of nitrogen sources of the ammonia preparation system and carbon dioxide sources of the methanol preparation system are solved.
Description
Technical Field
The utility model relates to the technical field of energy and chemical treatment, in particular to a supercritical carbon dioxide power generation coupling ammonia alcohol co-production system.
Background
With the increasing prominence of global climate change problems, the green low-carbon transformation and green chemical technology of energy systems have become the main direction of world energy development. The method establishes a sound green low-carbon cyclic development economic system, promotes the comprehensive green transformation of economic and social development, and is beneficial to solving the resource environment ecological problems in China.
The supercritical carbon dioxide power generation technology is a technology for realizing high-efficiency power generation by taking carbon dioxide fluid above a critical point as fluid working medium and utilizing the characteristic of high energy density, has the technical advantages of simplified system, high efficiency, small volume, easy realization of modularized assembly and the like, and has good application prospect and research value.
Ammonia is an important component of all foods and fertilizers on earth, as well as a direct or indirect component in many pharmaceutical and commercial cleaning products. Methanol is a common organic chemical raw material, and is applied to various fields such as chemical industry, pharmacy, light industry, spinning, transportation and the like. At present, the raw material sources for synthesizing ammonia and methanol are mainly petroleum, and petroleum resources have nonrenewability, so that along with the continuous reduction of the resources, other suitable raw materials are actively searched, the problem of energy consumption is very critical, and the ecological environment can be optimized.
Carbon dioxide capture is a core part of carbon capture, utilization and sequestration technologies, and high capture energy consumption is a current technical bottleneck. The method takes the nitrogen obtained by separating the green hydrogen prepared by the renewable energy electrolyzed water from the low-temperature air as the raw material to synthesize ammonia, and takes the split carbon dioxide and the green hydrogen prepared by the renewable energy electrolyzed water as the raw materials to synthesize the methanol, so that the method not only can realize the localized effective absorption of new energy, but also is an important way of chemical green transformation, can obviously reduce the carbon emission in the chemical industry, and has huge scale potential.
At present, related equipment for coupling a carbon dioxide power generation system, an ammonia preparation system and a methanol preparation system is lacking in the market, so that a supercritical carbon dioxide power generation coupling ammonia alcohol co-production system is necessary to be provided.
Disclosure of utility model
In order to solve the technical problems, the utility model adopts the following technical scheme:
a supercritical carbon dioxide power generation coupled ammonia alcohol co-production system comprising:
a supercritical carbon dioxide power generation system;
the ammonia preparation system is connected with the supercritical carbon dioxide power generation system;
The system comprises a methanol preparation system, wherein the methanol preparation system is connected with a supercritical carbon dioxide power generation system and comprises a pressure regulating valve, a third three-way valve, a hydrogen compressor, a fourth three-way valve, a methanol synthesis device and a methanol separation device, wherein the pressure regulating valve is connected with the supercritical carbon dioxide power generation system, the pressure regulating valve is sequentially connected with the third three-way valve, the methanol synthesis device and the methanol separation device, the fourth three-way valve is connected with a hydrogen supply device, the methanol separation device is connected with one port of the fourth three-way valve, the other port of the fourth three-way valve is connected with an inlet of the hydrogen compressor, and an outlet of the hydrogen compressor is connected with one port of the third three-way valve.
Further, a third heat regenerator is connected between the third three-way valve and the methanol synthesis device, and the methanol synthesis device is sequentially connected with the third heat regenerator and the methanol separation device.
Further, the supercritical carbon dioxide power generation system comprises an air separation device, a combustor, a turbine expander, a generator, a second heat regenerator, a precooler, a water separation device and a carbon dioxide compressor, wherein an oxygen outlet of the air separation device is connected with the combustor, the combustor is provided with a natural gas inlet, the combustor is sequentially connected with the turbine expander, the second heat regenerator, the precooler, the water separation device and the carbon dioxide compressor, the carbon dioxide compressor is sequentially connected with the second heat regenerator and the combustor, and the turbine expander is connected with the generator.
Further, the natural gas inlet is connected with a natural gas compressor, and the natural gas compressor is externally connected with a natural gas supply device.
Further, an oxygen compressor is arranged between the oxygen outlet of the air separation device and the burner.
Further, the water separation device is connected with the carbon dioxide compressor and the methanol preparation system through a fifth three-way valve, and the precooler is connected with the methanol preparation system.
Further, the ammonia preparation system comprises a first three-way valve, a second three-way valve, a mixed gas compressor, an ammonia synthesis device and an ammonia separation device, one port of the first three-way valve is connected with the supercritical carbon dioxide power generation system, the other port is externally connected with a hydrogen supply device, one end of the first three-way valve, which is not filled with gas, is connected with one port of the second three-way valve, which is not connected with the first three-way valve, is sequentially connected with the mixed gas compressor, the ammonia synthesis device and the ammonia separation device, and the ammonia separation device is connected with one port of the second three-way valve.
Further, a first heat regenerator is connected between the mixed gas compressor and the ammonia synthesis device, and the ammonia synthesis device is sequentially connected with the first heat regenerator and the ammonia separation device.
The utility model has the beneficial effects that:
according to the supercritical carbon dioxide power generation coupling ammonia alcohol co-production system provided by the utility model, natural gas is used as fuel, carbon dioxide is fully trapped in an oxygen-enriched combustion mode, high-energy-density carbon dioxide is used as working medium to do work in a turbine expander for power generation, so that the heat-power conversion efficiency is improved, and when the working medium is in a supercritical state, the change of the phase state of the working medium is avoided, so that the consumption of compression work is reduced.
The nitrogen separated by the air separation device required by oxygen-enriched combustion is used as a nitrogen source of the ammonia preparation system, so that the local effective absorption of the separable nitrogen is realized, and the green production of ammonia synthesis chemical industry can be realized.
By diverting the carbon dioxide collected by the supercritical carbon dioxide power generation system to the methanol preparation system, the difficult problem of high energy consumption of carbon dioxide capture is solved, and meanwhile, the localized effective utilization of the carbon dioxide and the chemical green production of methanol synthesis are realized.
Through reasonable operation regulation and control, the single modules and the coupling operation among the modules for generating power, synthesizing ammonia and synthesizing methanol and the simultaneous operation of the whole co-production system can be realized, and the net zero emission and high economical operation of the whole co-production system are realized.
Drawings
FIG. 1 is a schematic diagram of a coupled ammonia-alcohol cogeneration system for supercritical carbon dioxide power generation according to the utility model.
Wherein, in the figure:
1-an air separation device; a 2-oxygen compressor; 3-a natural gas compressor; a 4-burner; 5-a turbo expander; a 6-generator; 7-a second regenerator; 8-precooler; 9-water separation means; 10-a fifth three-way valve; 11-a carbon dioxide compressor; 12-a first three-way valve; 13-a second three-way valve; 14-a mixed gas compressor; 15-a first regenerator; a 16-ammonia synthesis device; 17-ammonia separation means; 18-a fourth three-way valve; 19-a hydrogen compressor; 20-a third three-way valve; 21-a pressure regulating valve; 22-a third regenerator; a 23-methanol synthesis device; 24-methanol separation device.
Detailed Description
The technical solutions of the embodiments of the present utility model will be clearly and completely described below with reference to fig. 1 of the embodiments of the present utility model, and it is apparent that the described embodiments are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Example 1
The embodiment provides a supercritical carbon dioxide power generation coupling ammonia alcohol co-production system which comprises a supercritical carbon dioxide power generation system, an ammonia preparation system and a methanol preparation system, wherein the supercritical carbon dioxide power generation system comprises an air separation device 1, a combustor 4, a turbine expander 5, a generator 6, a second heat regenerator 7, a precooler 8, a water separation device 9 and a carbon dioxide compressor 11, an oxygen outlet of the air separation device 1 is connected with the combustor 4, the combustor 4 is provided with a natural gas inlet, the combustor 4 is sequentially connected with the turbine expander 5, the second heat regenerator 7, the precooler 8, the water separation device 9 and the carbon dioxide compressor 11, the carbon dioxide compressor 11 is sequentially connected with the second heat regenerator 7 and the combustor 4, and the turbine expander 5 is connected with the generator 6; the ammonia preparation system is connected with a nitrogen outlet of the air separation device 1; the methanol preparation system is connected with the supercritical carbon dioxide power generation system; the supercritical carbon dioxide power generation system and the ammonia preparation system are coupled through the air separation device 1, and nitrogen separated by the air separation device 1 is used as a nitrogen source of the ammonia preparation system.
The burner 4 is provided with a natural gas inlet, an oxygen inlet, a carbon dioxide inlet and a mixed gas outlet after combustion; the hydrogen is green hydrogen prepared by electrolyzing water by renewable energy sources.
The turbine expander 5 can adopt one of a piston type, an axial flow type, a centrifugal type, a screw type or a mixed type, the pressure bearing range is not less than 300bar, and the inlet fluid temperature range is 500-1200 ℃.
Preferably, the second regenerator 7 is a printed circuit board type heat exchanger, and the precooler 8 is one of a shell-and-tube type heat exchanger or a brazed plate type heat exchanger.
The natural gas inlet is connected with a natural gas compressor, and the natural gas compressor is externally connected with a natural gas supply device; an oxygen compressor is arranged between the oxygen outlet of the air separation device and the burner.
The ammonia preparation system comprises a first three-way valve 12, a second three-way valve 13, a mixed gas compressor 14, a first heat regenerator 15, an ammonia synthesis device 16 and an ammonia separation device 17, wherein one port of the first three-way valve 12 is connected with a nitrogen outlet of the air separation device 1, the other port is externally connected with a hydrogen supply device, one end of the first three-way valve 12, which is not filled with gas, is connected with one port of the second three-way valve 13, which is not connected with the first three-way valve 12, is sequentially connected with the mixed gas compressor 14, the first heat regenerator 15 and the ammonia synthesis device 16, the air outlet end of the ammonia synthesis device 16 is sequentially connected with the first heat regenerator 15 and the ammonia separation device 17, and the ammonia separation device 17 is connected with one port of the second three-way valve 13; a first heat regenerator 15 is connected between the mixed gas compressor 14 and the ammonia synthesis device 16, and a discharge end of the ammonia synthesis device 16 is sequentially connected with the first heat regenerator 15 and the ammonia separation device 17.
In this embodiment, the first regenerator 15 is one of a shell-and-tube heat exchanger or a brazed plate heat exchanger.
The water separation device 9 is respectively connected with the carbon dioxide compressor 11 and the methanol preparation system through a fifth three-way valve 10, the fifth three-way valve 10 divides the carbon dioxide generated by the supercritical carbon dioxide power generation system, one of the three-way valves is used as a circulating medium of the supercritical power generation system, the other three-way valve is used as a carbon dioxide raw material of the methanol preparation system, and the precooler 8 is connected with the methanol preparation system.
The methanol preparation system comprises a pressure regulating valve 21, a third three-way valve 20, a hydrogen compressor 19, a fourth three-way valve 18, a methanol synthesis device 23, a methanol separation device 24 and a hydrogen supply device, wherein the water separation device 9 is sequentially connected with the pressure regulating valve 21, the third three-way valve 20, the methanol synthesis device 23 and the methanol separation device 24, the hydrogen supply device is sequentially connected with a precooler 8 and the fourth three-way valve 18, the methanol separation device 24 is connected with one port of the fourth three-way valve 18, the other port of the fourth three-way valve 18 is connected with an inlet of the hydrogen compressor 19, and an outlet of the hydrogen compressor 19 is connected with one port of the third three-way valve 20; a third heat regenerator 22 is connected between the third three-way valve 20 and the methanol synthesis device 23, and the methanol synthesis device 23 is sequentially connected with the third heat regenerator 22 and the methanol separation device 24.
The pressure regulating valve 21 is a self-operated regulating valve, and the pressure regulating range is 50-100bar; the third regenerator 22 is one of a shell and tube heat exchanger or a brazed plate heat exchanger.
In this embodiment, each gas compressor may be one of a piston type, an axial flow type, a centrifugal type, a screw type, or a hybrid type, and the pressure bearing range of each gas compressor is not less than 300bar; and each three-way valve can adopt a mass flow controller flow dividing valve, and the pressure bearing range is not less than 100bar.
Example two
A co-production method of a supercritical carbon dioxide power generation coupling ammonia alcohol co-production system comprises the following steps:
Generating electricity by carbon dioxide: air enters an air separation device 1 to be subjected to gas separation, separated oxygen is compressed to a specified pressure by an oxygen compressor 2 and then enters a combustor 4, the separated oxygen is combusted together with the introduced natural gas in the combustor 4, high-temperature gas generated by combustion is mixed with carbon dioxide introduced into the combustor 4, the formed high-temperature high-pressure mixed gas mainly comprising carbon dioxide enters a turbine expander 5 from an outlet of the combustor 4 to perform work power generation, the exhaust gas of the turbine expander 5 is subjected to heat recovery by a second regenerator 7 and water separation by a precooler 8 cooling and water separation device 9, and then is split by a fifth three-way valve 10, and the split carbon dioxide is compressed to the specified pressure by a carbon dioxide compressor 11 and then flows through the second regenerator 7 to be heated to enter the combustor 4 to be mixed with combustion products of the oxygen and the natural gas and then is continuously circulated;
Ammonia preparation: the air enters the air separation device 1 to be subjected to gas separation, the separated nitrogen is mixed with the hydrogen through a first three-way valve 12, the mixed gas of the nitrogen and the hydrogen is further mixed with the gas separated by an ammonia separation device 17 through a second three-way valve 13, the mixed gas is compressed to a specified pressure through a mixed gas compressor 14, the mixed gas is heated through a first heat regenerator 15 and then enters an ammonia synthesis device 16 to react to generate ammonia, an outlet of the ammonia synthesis device 16 is connected with a high-temperature gas inlet of the first heat regenerator 15, the mixed gas is cooled through the first heat regenerator 15 and then enters the ammonia separation device 17 to separate ammonia, and the mixed gas after ammonia separation flows into the second three-way valve 13 to be mixed with the hydrogen and the nitrogen and then is continuously recycled to prepare ammonia.
Preparation of methanol: the carbon dioxide split by the fifth three-way valve 10 flows into the third three-way valve 20 to be mixed with hydrogen according to a certain proportion after the pressure is regulated by the pressure regulating valve 21; the hydrogen is heated by the precooler 8 and then is further mixed with the gas separated by the methanol separation device 24, then is compressed to the specified pressure by the hydrogen compressor 19, and then enters the third three-way valve 20 to be mixed with the carbon dioxide according to a certain proportion; the mixed gas is heated by the third heat regenerator 22 and then enters the methanol synthesis device 23 to react to generate methanol, the outlet of the methanol synthesis device 23 is connected with the high-temperature gas inlet of the third heat regenerator 22, the mixed gas is cooled by the third heat regenerator 22 and then enters the methanol separation device 24 to separate the methanol, and the mixed gas after the methanol separation flows into the fourth three-way valve 18 to be mixed with hydrogen and then is continuously circulated.
The carbon dioxide source of the methanol preparation system is the carbon dioxide separated by the supercritical carbon dioxide power generation system, and the supercritical carbon dioxide power generation system, the ammonia preparation system and the methanol preparation system are coupled and connected, so that the efficiency of the supercritical carbon dioxide power generation system is improved, the problems of the nitrogen source of the ammonia preparation system and the carbon dioxide source of the methanol preparation system are solved, the raw materials for synthesizing ammonia and synthesizing methanol are provided while the clean zero-emission efficient power generation is realized, the problem of high carbon dioxide capture energy consumption is solved, and the clean zero emission and high economical operation of the whole co-production system are realized through reasonable operation regulation and control.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present utility model. Various modifications to the embodiments described above will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present utility model is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (8)
1. A supercritical carbon dioxide power generation coupled ammonia alcohol co-production system, comprising:
a supercritical carbon dioxide power generation system;
the ammonia preparation system is connected with the supercritical carbon dioxide power generation system;
The system comprises a methanol preparation system, wherein the methanol preparation system is connected with a supercritical carbon dioxide power generation system and comprises a pressure regulating valve, a third three-way valve, a hydrogen compressor, a fourth three-way valve, a methanol synthesis device and a methanol separation device, wherein the pressure regulating valve is connected with the supercritical carbon dioxide power generation system, the pressure regulating valve is sequentially connected with the third three-way valve, the methanol synthesis device and the methanol separation device, the fourth three-way valve is connected with a hydrogen supply device, the methanol separation device is connected with one port of the fourth three-way valve, the other port of the fourth three-way valve is connected with an inlet of the hydrogen compressor, and an outlet of the hydrogen compressor is connected with one port of the third three-way valve.
2. The supercritical carbon dioxide power generation coupling ammonia alcohol co-production system according to claim 1, wherein a third heat regenerator is connected between the third three-way valve and the methanol synthesis device, and the methanol synthesis device is sequentially connected with the third heat regenerator and the methanol separation device.
3. The supercritical carbon dioxide power generation coupling ammonia alcohol co-production system according to claim 1, wherein the supercritical carbon dioxide power generation system comprises an air separation device, a combustor, a turbine expander, a generator, a second regenerator, a precooler, a water separation device and a carbon dioxide compressor, an oxygen outlet of the air separation device is connected with the combustor, the combustor is provided with a natural gas inlet, the combustor is sequentially connected with the turbine expander, the second regenerator, the precooler, the water separation device and the carbon dioxide compressor, the carbon dioxide compressor is sequentially connected with the second regenerator and the combustor, and the turbine expander is connected with the generator.
4. The supercritical carbon dioxide power generation coupling ammonia alcohol co-production system according to claim 3, wherein the natural gas inlet is connected with a natural gas compressor, and the natural gas compressor is externally connected with a natural gas supply device.
5. A supercritical carbon dioxide power generation coupled ammonia alcohol co-production system according to claim 3 wherein an oxygen compressor is disposed between the oxygen outlet of the air separation unit and the burner.
6. A supercritical carbon dioxide power generation coupled ammonia alcohol co-production system according to claim 3, wherein the water separation device is connected to a carbon dioxide compressor and a methanol preparation system through a fifth three-way valve, respectively, and the precooler is connected to the methanol preparation system.
7. The supercritical carbon dioxide power generation coupling ammonia alcohol co-production system according to claim 1, wherein the ammonia preparation system comprises a first three-way valve, a second three-way valve, a mixed gas compressor, an ammonia synthesis device and an ammonia separation device, one port of the first three-way valve is connected with the supercritical carbon dioxide power generation system, the other port is externally connected with a hydrogen supply device, one end of the first three-way valve, which is not filled with gas, is connected with one port of the second three-way valve, and one port of the second three-way valve, which is not connected with the first three-way valve, is sequentially connected with the mixed gas compressor, the ammonia synthesis device and the ammonia separation device, and the ammonia separation device is connected with one port of the second three-way valve.
8. The supercritical carbon dioxide power generation coupling ammonia alcohol co-production system according to claim 7, wherein a first heat regenerator is connected between the mixed gas compressor and the ammonia synthesis device, and the ammonia synthesis device is sequentially connected with the first heat regenerator and the ammonia separation device.
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