CN210317415U - Absorption type seawater desalination and closed cycle power generation system - Google Patents
Absorption type seawater desalination and closed cycle power generation system Download PDFInfo
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- CN210317415U CN210317415U CN201921277292.8U CN201921277292U CN210317415U CN 210317415 U CN210317415 U CN 210317415U CN 201921277292 U CN201921277292 U CN 201921277292U CN 210317415 U CN210317415 U CN 210317415U
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Abstract
The utility model provides an absorption-type sea water desalination and closed circulation power generation system, include: heat source, absorption formula sea water desalination return circuit and supercritical carbon dioxide circulation return circuit, the utility model provides an absorption formula sea water desalination and closed circulation power generation system pass through absorption formula sea water desalination return circuit and are used for sea water desalination with the used heat of supercritical carbon dioxide circulation release, can realize the use of low-grade used heat, and sea water desalination energy consumption is low, adopts the supercritical carbon dioxide circulation of simple backheat mode, and system structure is simple compact, and the operating temperature of generator is lower, can absorb the low temperature section heat of heat source, improves heat source efficiency.
Description
Technical Field
The utility model relates to the technical field of power generation, especially relate to an absorption-type sea water desalination and closed circulation power generation system.
Background
Water is a fundamental natural resource and a strategic economic resource. With the rapid increase of the total population of the world, the rapid development of economic society and the influence of climate change, the world faces an increasingly serious water shortage crisis. The seawater desalination is used as an open source increment technology for realizing sustainable utilization of water resources, can increase the total amount of fresh water, is little influenced by climate, has stable water supply, good water quality of products and strong reliability, can provide high-quality municipal water supply and industrial high-quality water for coastal areas, and has become an important means for solving the global crisis of shortage of fresh water resources in the coastal areas. Currently, global desalination yields exceed 1 billion cubic meters per day and increase at a rate of over 10% per year.
In order to obtain better economy, a power generation system and a desalination system are integrated by adopting a power and water cogeneration mode. At present, electricity and water cogeneration combines a turbo generator unit and a seawater desalination device, and is divided into three main categories: power plant + distillation desalination, power plant + reverse osmosis desalination, power plant + distillation desalination + reverse osmosis desalination. For other types of generator sets, a better combination mode needs to be explored.
In recent years, the supercritical carbon dioxide cycle has become a hot spot and is believed to have a number of potential advantages. The critical point of carbon dioxide is 31 ℃/7.4MPa, and the state when the temperature and pressure exceed the critical point is a supercritical state. The carbon dioxide has stable chemical property, high density, no toxicity, low cost, simple circulating system, compact structure, high efficiency and air cooling, and the supercritical carbon dioxide can be combined with various heat sources to form a power generation system, so the carbon dioxide has good application prospect in the fields of thermal power generation, nuclear power generation, solar thermal power generation, waste heat power generation, geothermal power generation, biomass power generation and the like. However, the supercritical carbon dioxide cycle main heater has a narrow endothermic temperature range, which may cause heat source loss, especially, is more disadvantageous for sensible heat source.
SUMMERY OF THE UTILITY MODEL
In view of the above shortcomings in the prior art, the technical problem to be solved by the present invention is to solve the problem that when supercritical carbon dioxide is cyclically applied to a power generation system, the interval of the heat absorption temperature of the main heater is relatively narrow, which causes heat source loss, especially to the disadvantage of sensible heat source.
In order to solve the technical problem, the utility model provides an absorption-type seawater desalination and closed circulation power generation system, include: a heat source, an absorption seawater desalination loop and a supercritical carbon dioxide circulation loop;
the absorption type seawater desalination loop comprises a generator, a gas-liquid separator, a condenser, a water heat exchanger, a fresh water hydraulic turbine, an evaporator, an absorber, a solution pump, a solution heat exchanger, a solution hydraulic turbine, a seawater preheater, a seawater hydraulic turbine and a concentrated brine pump, wherein the outlet of the generator is connected with the inlet of the gas-liquid separator, the outlet of the gas-liquid separator is connected with the high-temperature side inlet of the condenser, the high-temperature side outlet of the condenser is connected with the inlet of the water heat exchanger, the outlet of the water heat exchanger is connected with the inlet of the fresh water hydraulic turbine, the low-temperature side outlet of the evaporator is connected with the inlet of the absorber, the outlet of the absorber is connected with the inlet of the solution pump, the outlet of the solution pump is connected with the low-temperature side inlet of the solution heat exchanger, and the low-, the high-temperature side outlet of the solution heat exchanger is also connected with the inlet of the solution hydraulic turbine, the outlet of the solution hydraulic turbine is connected with the inlet of the absorber, the outlet of the seawater preheater and the outlet of the water heat exchanger are connected with the inlet of the seawater hydraulic turbine, the outlet of the seawater hydraulic turbine is connected with the inlet of the evaporator, and the outlet of the evaporator is connected with the inlet of the strong brine pump;
the supercritical carbon dioxide circulation loop comprises a compressor, a low-temperature heat regenerator, a condenser, a medium-temperature heat regenerator, a high-temperature heat regenerator, a turbine, a precooler, a generator and a working medium heater, wherein the outlet of the compressor is respectively connected with a high-pressure side inlet of the low-temperature heat regenerator and a low-temperature side inlet of the absorber, a low-temperature side outlet of the absorber and a high-pressure side outlet of the low-temperature heat regenerator are converged and divided into two paths, one path is connected with a low-temperature side inlet of the condenser, the other path is connected with a high-pressure side inlet of the medium-temperature heat regenerator, a low-temperature side outlet of the condenser and a high-pressure side outlet of the medium-temperature heat regenerator are converged and connected with a high-pressure side inlet of the high-temperature heat regenerator, a high-pressure side outlet of the high-temperature heat regenerator is connected with an inlet of the working medium, the low-pressure side outlet of the high-temperature heat regenerator is connected with the low-pressure side inlet of the medium-temperature heat regenerator, the low-pressure side outlet of the medium-temperature heat regenerator is connected with the low-pressure side inlet of the low-temperature heat regenerator, the low-pressure side outlet of the low-temperature heat regenerator is connected with the high-temperature side inlet of the evaporator, the high-temperature side outlet of the evaporator is connected with the high-temperature side inlet of the precooler, the high-temperature side outlet of the precooler is connected with the inlet of the compressor, and the turbine provides power for the generator and the compressor.
The heat source provides heat for the generator of the absorption seawater desalination loop and the working medium heater of the supercritical carbon dioxide circulation loop.
Optionally, the heat source is selected from fossil energy, solar energy, biomass energy or nuclear energy.
Optionally, the heat source is selected from fossil energy and takes the form of a coal-fired boiler, heat generated by combustion of the coal-fired boiler is provided to the working medium heater, and heat of flue gas of the coal-fired boiler is provided to the generator.
Optionally, the working medium pair of the absorption-type seawater desalination circuit is an aqueous solution of lithium bromide. Wherein, water is a refrigerant, and lithium bromide is an absorbent.
Optionally, the compressor is a two-stage or multi-stage compressor with an intercooler.
Optionally, the precooler is cooled by seawater.
Optionally, in the supercritical carbon dioxide circulation loop, the compressor, the turbine and the generator are arranged coaxially.
Optionally, in the supercritical carbon dioxide circulation loop, the outlet temperature of the compressor is not more than 40 ℃, the outlet pressure of the compressor is greater than or equal to 15MPa, the inlet temperature of the turbine is greater than or equal to 500 ℃, and the outlet pressure of the turbine is 5 MPa-8 MPa.
Optionally, in the absorption-type seawater desalination loop, the pressure of the evaporator is 2kPa to 8kPa, and the pressure of the condenser is 0.1MPa to 1 MPa.
Optionally, the heat source of the seawater preheater in the absorption seawater desalination circuit is from a precooler in the supercritical carbon dioxide circulation circuit.
Compared with the prior art, the utility model discloses technical scheme's absorption seawater desalination and closed circulation power generation system have following beneficial effect:
waste heat released by the supercritical carbon dioxide circulation loop is used for sea water desalination through the absorption type sea water desalination loop, so that the use of low-grade waste heat can be realized, and the energy consumption for sea water desalination is low.
In the absorption type seawater desalination loop, a generator can adopt a medium-high temperature heat source as a drive, an evaporator absorbs low-temperature heat for evaporating seawater, and an absorber and a condenser can release medium-low grade heat.
In the supercritical carbon dioxide circulation loop, the working medium discharged by the turbine sequentially passes through the high-temperature heat regenerator, the medium-temperature heat regenerator and the low-temperature heat regenerator to recover partial waste heat, then passes through the evaporator of the absorption type seawater desalination loop to recover low-grade waste heat, is cooled by the precooler and finally returns to the inlet of the compressor, so that the use of the low-grade waste heat is realized, the energy consumption of seawater desalination is greatly reduced, and the system has a simple and compact structure by adopting a heat regeneration mode.
The waste heat discharged by the supercritical carbon dioxide circulation loop is used as the heat of the evaporator, and the heat of the absorber and the condenser is transferred to the outlet working medium of the compressor, so that the efficiency of the supercritical carbon dioxide circulation is further improved.
The coal-fired boiler is used as a heat source, heat of a high-temperature section generated by combustion is supplied to the working medium heater, and medium-temperature heat of boiler exhaust smoke is supplied to the generator, so that the combustion heat is fully utilized.
Drawings
Fig. 1 is a schematic structural diagram of an absorption-type seawater desalination and closed-cycle power generation system according to an embodiment of the present invention;
wherein: the system comprises a compressor, a low-temperature heat regenerator, a 3-medium-temperature heat regenerator, a 4-high-temperature heat regenerator, a 5-working medium heater, a 6-turbine, a 7-generator, an 8-precooler, a 9-evaporator, a 10-absorber, an 11-solution pump, a 12-solution heat exchanger, a 13-gas-liquid separator, a 14-solution hydraulic turbine, a 15-condenser, a 16-water heat exchanger, a 17-seawater hydraulic turbine, an 18-fresh water hydraulic turbine, a 19-concentrated brine pump, a 20-generator, a 21-seawater preheater, a 100-absorption seawater desalination loop, a 200-boiler and a 300-supercritical carbon dioxide circulation loop.
Detailed Description
The technical solution of the present invention will be described in detail with reference to the following examples.
As shown in fig. 1, the utility model discloses absorption seawater desalination and closed cycle power generation system of embodiment includes: a heat source 200, an absorption seawater desalination circuit 100 and a supercritical carbon dioxide circulation circuit 300.
The heat source 200 provides heat for the generator 20 of the absorption-type seawater desalination circuit 100 and the working medium heater 5 of the supercritical carbon dioxide circulation circuit 300.
The heat source 200 may be selected from fossil energy, solar energy, biomass energy, nuclear energy, or the like. In the embodiment of the present invention, the heat source 200 is selected from fossil energy and takes the form of a coal-fired boiler, the heat generated by the combustion of the coal-fired boiler is provided to the working medium heater 5, and the heat of the exhaust gas of the coal-fired boiler is provided to the generator 20.
The absorption-type seawater desalination loop 100 comprises a generator 20, a gas-liquid separator 13, a condenser 15, a water heat exchanger 16, a fresh water hydraulic turbine 18, an evaporator 9, an absorber 10, a solution pump 11, a solution heat exchanger 12, a solution hydraulic turbine 14, a seawater preheater 21, a seawater hydraulic turbine 17 and a concentrated brine pump 19.
Wherein, the outlet of the generator 20 is connected with the inlet of the gas-liquid separator 13, the outlet of the gas-liquid separator 13 is connected with the high-temperature side inlet of the condenser 15, the high-temperature side outlet of the condenser 15 is connected with the inlet of the water heat exchanger 16, the outlet of the water heat exchanger 16 is connected with the inlet of the fresh water hydraulic turbine 18, the low-temperature side outlet of the evaporator 9 is connected with the inlet of the absorber 10, the outlet of the absorber 10 is connected with the inlet of the solution pump 11, the outlet of the solution pump 11 is connected with the low-temperature side inlet of the solution heat exchanger 12, the low-temperature side outlet of the solution heat exchanger 12 is connected with the inlet of the generator 20, the high-temperature side outlet of the solution heat exchanger 12 is also connected with the inlet of the solution hydraulic turbine 14, the outlet of the solution hydraulic turbine 14 is connected with the inlet of the absorber 10, the outlet of the seawater, the outlet of the evaporator 9 is connected to the inlet of a concentrated brine pump 19.
The utility model discloses a supercritical carbon dioxide circulation loop 300 includes compressor 1, low temperature regenerator 2, condenser 15, medium temperature regenerator 3, high temperature regenerator 4, turbine 6, generator 7, precooler 8 and working medium heater 5, the export of compressor 1 is connected the high pressure side import of low temperature regenerator 2 and the low temperature side import of absorber 10 respectively, the low temperature side export of absorber 10 joins and divide into two the tunnel with the high pressure side export of low temperature regenerator 2, the low temperature side import of condenser 15 is connected all the way, the high pressure side import of medium temperature regenerator 3 is connected to another way, the low temperature side export of condenser 15 joins and is connected the high pressure side import of high temperature regenerator 4 with the high pressure side export of medium temperature regenerator 3, the import of working medium heater 5 is connected to the high pressure side export of high temperature regenerator 4, the import of turbine 6 is connected to the export of working medium heater 5, the outlet of the turbine 6 is connected with the low-pressure side inlet of the high-temperature heat regenerator 4, the low-pressure side outlet of the high-temperature heat regenerator 4 is connected with the low-pressure side inlet of the medium-temperature heat regenerator 3, the low-pressure side outlet of the medium-temperature heat regenerator 3 is connected with the low-pressure side inlet of the low-temperature heat regenerator 2, the low-pressure side outlet of the low-temperature heat regenerator 2 is connected with the high-temperature measuring inlet of the evaporator 9, the high-temperature measuring port of the evaporator 9 is connected with the high-temperature side inlet of the precooler 8, and the high-temperature side. Turbine 6 powers generator 7 and compressor 1.
The working medium pair of the absorption-type seawater desalination circuit 100 is an aqueous solution of lithium bromide. Wherein, water is a refrigerant, and lithium bromide is an absorbent.
The compressor 1 is a two-stage or multi-stage compressor with an intercooler, and both the compressor 1 and the turbine 6 are arranged coaxially with the generator 7. Fig. 1 schematically illustrates a three-stage compressor.
Precooler 8 is cooled by seawater, and the heat source of seawater preheater 21 is from precooler 8 in the supercritical carbon dioxide circulation loop.
As shown in fig. 1, in the supercritical carbon dioxide cycle 300, the compressor 1, the turbine 6, and the generator 7 are coaxially arranged.
In the supercritical carbon dioxide circulation loop 300, the outlet temperature of the compressor 1 is not more than 40 ℃, the outlet pressure of the compressor 1 is greater than or equal to 15MPa, the inlet temperature of the turbine 6 is greater than or equal to 500 ℃, and the outlet pressure of the turbine 6 is 5MPa to 8 MPa. The turbine 6 is single-stage or two-stage or multi-stage and adopts a reheating mode.
In the absorption-type seawater desalination circuit 100, the pressure of the evaporator 9 is 2kPa to 8kPa, and the pressure of the condenser 15 is 0.1MPa to 1 MPa.
It should be noted that, the utility model discloses the equipment that technical scheme related to all belongs to existing equipment the embodiment of the utility model provides an in, specifically adopted following equipment: compressor (axial flow multi-stage cold carbon dioxide compressor), low temperature heat regenerator (printed circuit board heat exchanger), medium temperature heat regenerator (printed circuit board heat exchanger), high temperature heat regenerator (printed circuit board heat exchanger), working medium heater (stainless steel tube heater), turbine (axial flow carbon dioxide turbine), generator (three-phase AC synchronous generator), precooler (tube cooler), evaporator (shell-and-tube evaporator), absorber (spray absorber), solution pump (centrifugal pump), solution heat exchanger (shell-and-tube heat exchanger), gas-liquid separator (spray separator), solution hydraulic turbine (centripetal turbine), condenser (tube cooler), water heat exchanger (shell-and-tube heat exchanger), seawater hydraulic turbine (centripetal turbine), fresh water hydraulic turbine (centripetal turbine), concentrated brine pump (centrifugal pump), a generator (immersion generator), a seawater preheater (shell-and-tube heat exchanger), and a boiler (pi-shaped furnace).
In addition to the above-described necessary structures, valves, fluid machines, meters, auxiliary facilities, electrical systems, meter control systems, and the like may be arranged according to system control requirements.
The utility model discloses absorption seawater desalination goes on with working method that closed circulation power generation system pressed:
in the supercritical carbon dioxide circulation loop 300, a carbon dioxide working medium enters a compressor 1 for pressurization and is divided into two paths of working media at the outlet of the compressor 1, one path of working media enters a low-temperature heat regenerator 2 and absorbs heat of a working medium discharged by a turbine 6, the other path of working media absorbs heat through an absorber 10 of an absorption type seawater desalination loop 100, after the two paths of working media are converged, the two paths of working media are divided into two paths of working media again, one path of working media absorbs heat of the working medium discharged by the turbine 6 through a medium-temperature heat regenerator 3, the other path of working media absorbs heat through a condenser 15 of the absorption type seawater desalination loop 100, then the two paths of working media are converged again and enter a high-temperature heat regenerator 4 to absorb heat of a high-temperature section of the working medium discharged by the turbine 6, the working medium discharged by the high-temperature heat regenerator 4 is heated by a working medium heater 5 and then enters, The intermediate-temperature heat regenerator 3 and the low-temperature heat regenerator 2 recover partial waste heat, then the low-grade waste heat is recovered by an evaporator 9 of the absorption seawater desalination loop 100, and then the low-grade waste heat is cooled by a precooler 8 and finally returns to an inlet of the compressor 1. The working medium discharged by the turbine 6 is sequentially recycled part of waste heat through the high-temperature heat regenerator 4, the medium-temperature heat regenerator 3 and the low-temperature heat regenerator 2, then recycled low-grade waste heat through the evaporator 9 of the absorption type seawater desalination loop 100, cooled through the precooler 8 and finally returned to the inlet of the compressor 1.
Meanwhile, in the absorption-type seawater desalination loop 100, the heat source 200 heats the working medium pair in the generator 20, the refrigerant is evaporated and enters the gas-liquid separator 13 for gas-liquid separation, the refrigerant steam enters the condenser 15, the remaining concentrated solution is cooled by the solution heat exchanger 12, enters the solution hydraulic turbine 14 for recovering work, and then enters the absorber 10; refrigerant steam enters a condenser 15 to be liquefied and release heat to be transmitted to a carbon dioxide working medium, the refrigerant recovers waste heat through a water heat exchanger 16 to be used for preheating seawater, work is recovered through a fresh water hydraulic turbine 18, one path of seawater passes through a seawater preheating 21 device, the other path of seawater passes through a water heat exchanger 16, two paths of seawater are converged and then work is recovered through a seawater hydraulic turbine 17, the seawater enters an evaporator 9, the seawater absorbs low-grade waste heat of the carbon dioxide working medium in the evaporator 9 and then is evaporated, strong brine is discharged through a strong brine pump, the steam enters an absorber 10 to be absorbed by the solution, the heat released in the absorption process is transmitted to the carbon dioxide working medium, the solution in the absorber 100 is input into a solution heat exchanger 12 through a solution pump 11 to be preheated, and.
The embodiment of the utility model provides an absorption-type sea water desalination and closed circulation power generation system's a concrete working example as follows:
in the supercritical carbon dioxide cycle 300, a carbon dioxide working medium firstly enters the compressor 1 to be pressurized to 30MPa, the compressor 1 is in three-stage intercooling, and the carbon dioxide working medium at the outlet of the compressor 1 is divided into two paths: one path absorbs heat of working medium discharged by a turbine 6 through a low-temperature heat regenerator 2, the other path absorbs heat through an absorber 10 of an absorption type seawater desalination loop 100, the two paths of working medium are merged and then divided into two paths, one path absorbs heat of the working medium discharged by the turbine 6 through a medium-temperature heat regenerator 3, the other path absorbs heat through a condenser 15 of the absorption type seawater desalination loop 100, then the two paths of working medium are merged and enter a high-temperature heat regenerator 4 to absorb heat of a high-temperature section of the working medium discharged by the turbine 6, the working medium discharged by the high-temperature heat regenerator 4 is heated to 620 ℃ through a working medium heater 5, then enters the turbine 6 to expand and do work, the turbine 6 pushes a generator 7 and a compressor 1, the pressure of the working medium discharged by the turbine 6 is reduced to 7MPa, partial waste heat is recovered through the high-temperature heat regenerator 4, the medium-temperature heat regenerator 3 and the low-temperature heat regenerator 2 in sequence, and finally back to the compressor 1 inlet.
Meanwhile, in the absorption-type seawater desalination loop 100, the working medium pair of the generator 20 is heated by a heat source, the refrigerant is evaporated, the refrigerant enters the gas-liquid separator 13, the refrigerant steam enters the condenser 15, the pressure of the condenser 15 is 0.5MPa, and the remaining concentrated solution is cooled by the solution heat exchanger 12, enters the solution hydraulic turbine 14 to recover work, and then enters the absorber 10; refrigerant steam enters a condenser 15 to be liquefied and releases heat to be transferred to a carbon dioxide working medium, the refrigerant recovers waste heat through a water heat exchanger 16 to be used for preheating seawater, work is recovered through a fresh water hydraulic turbine 18, one path of seawater passes through a seawater preheater 21, the other path of seawater passes through a water heat exchanger 16, two paths of seawater are converged and then work is recovered through a seawater hydraulic turbine 17, the refrigerant enters an evaporator 9, the pressure of the evaporator 9 is 3kPa, the seawater absorbs low-grade waste heat of the carbon dioxide working medium in the evaporator 9 and then evaporates, strong brine is discharged through a strong brine pump 19, the steam enters an absorber 10 to be absorbed by the solution, the heat released in the absorption process is transferred to the carbon dioxide working medium, the solution in the absorber 10 is input into a solution heat exchanger 12 through a solution pump 11 to be preheated.
In the process, the power generation efficiency of the supercritical carbon dioxide cycle 300 can reach more than 45%, and meanwhile, the absorption-type seawater desalination loop 100 can prepare fresh water by utilizing the waste heat of the supercritical carbon dioxide cycle 300, and for a unit with the capacity of 100MW, the by-product fresh water can reach 1200 cubic/day, so that the absorption-type seawater desalination loop has considerable economical efficiency.
While specific embodiments of the present invention have been described in detail, it will be appreciated that modifications and variations can be made by persons skilled in the art in light of the above teachings without inventive faculty. Therefore, the technical solutions that can be obtained by a person skilled in the art through logic analysis, reasoning or limited experiments based on the prior art according to the concepts of the present invention should be within the scope of protection defined by the claims.
Claims (8)
1. An absorption-type seawater desalination and closed cycle power generation system, comprising: a heat source, an absorption seawater desalination loop and a supercritical carbon dioxide circulation loop;
the absorption type seawater desalination loop comprises a generator, a gas-liquid separator, a condenser, a water heat exchanger, a fresh water hydraulic turbine, an evaporator, an absorber, a solution pump, a solution heat exchanger, a solution hydraulic turbine, a seawater preheater, a seawater hydraulic turbine and a concentrated brine pump, wherein the outlet of the generator is connected with the inlet of the gas-liquid separator, the outlet of the gas-liquid separator is connected with the high-temperature side inlet of the condenser, the high-temperature side outlet of the condenser is connected with the inlet of the water heat exchanger, the outlet of the water heat exchanger is connected with the inlet of the fresh water hydraulic turbine, the low-temperature side outlet of the evaporator is connected with the inlet of the absorber, the outlet of the absorber is connected with the inlet of the solution pump, the outlet of the solution pump is connected with the low-temperature side inlet of the solution heat exchanger, and the low-, the high-temperature side outlet of the solution heat exchanger is also connected with the inlet of the solution hydraulic turbine, the outlet of the solution hydraulic turbine is connected with the inlet of the absorber, the outlet of the seawater preheater and the outlet of the water heat exchanger are connected with the inlet of the seawater hydraulic turbine, the outlet of the seawater hydraulic turbine is connected with the inlet of the evaporator, and the outlet of the evaporator is connected with the inlet of the strong brine pump;
the supercritical carbon dioxide circulation loop comprises a compressor, a low-temperature heat regenerator, a condenser, a medium-temperature heat regenerator, a high-temperature heat regenerator, a turbine, a precooler, a generator and a working medium heater, wherein the outlet of the compressor is respectively connected with a high-pressure side inlet of the low-temperature heat regenerator and a low-temperature side inlet of the absorber, a low-temperature side outlet of the absorber and a high-pressure side outlet of the low-temperature heat regenerator are converged and divided into two paths, one path is connected with a low-temperature side inlet of the condenser, the other path is connected with a high-pressure side inlet of the medium-temperature heat regenerator, a low-temperature side outlet of the condenser and a high-pressure side outlet of the medium-temperature heat regenerator are converged and connected with a high-pressure side inlet of the high-temperature heat regenerator, a high-pressure side outlet of the high-temperature heat regenerator is connected with an inlet of the working medium, the low-pressure side outlet of the high-temperature heat regenerator is connected with the low-pressure side inlet of the medium-temperature heat regenerator, the low-pressure side outlet of the medium-temperature heat regenerator is connected with the low-pressure side inlet of the low-temperature heat regenerator, the low-pressure side outlet of the low-temperature heat regenerator is connected with the high-temperature side inlet of the evaporator, the high-temperature side outlet of the evaporator is connected with the high-temperature side inlet of the precooler, the high-temperature side outlet of the precooler is connected with the inlet of the compressor, and the turbine provides power for the generator and the compressor;
the heat source provides heat for the generator of the absorption seawater desalination loop and the working medium heater of the supercritical carbon dioxide circulation loop.
2. The absorption-type desalination and closed-cycle power generation system of claim 1, wherein the heat source is selected from fossil energy, solar energy, biomass energy, or nuclear energy.
3. The absorption-type seawater desalination and closed-cycle power generation system of claim 1, wherein the heat source is selected from fossil energy sources and takes the form of a coal-fired boiler, the heat generated by combustion of the coal-fired boiler is provided to the working fluid heater, and the heat of the flue gas of the coal-fired boiler is provided to the generator.
4. The absorption-type seawater desalination and closed cycle power generation system of claim 1, wherein the working substance pair of the absorption-type seawater desalination circuit is an aqueous solution of lithium bromide, wherein water is a refrigerant and lithium bromide is an absorbent.
5. The absorption-type seawater desalination and closed-cycle power generation system of claim 1, wherein the compressor is a two-stage or multi-stage compressor with an intercooler.
6. The absorption-type seawater desalination and closed-cycle power generation system of claim 1, wherein the precooler employs seawater cooling.
7. The absorption-type seawater desalination and closed-cycle power generation system of claim 1, wherein the compressor, the pervaporation and the generator are coaxially arranged in the supercritical carbon dioxide recycle loop.
8. The absorption-type seawater desalination and closed-cycle power generation system of claim 1, wherein the heat source of the seawater preheater in the absorption-type seawater desalination circuit is from a precooler in the supercritical carbon dioxide circulation circuit.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110344898A (en) * | 2019-08-05 | 2019-10-18 | 上海发电设备成套设计研究院有限责任公司 | Absorption type desalination and closed cycle electricity generation system |
| WO2022037711A1 (en) * | 2020-12-28 | 2022-02-24 | 中国长江三峡集团有限公司 | Flexible power station employing supercritical carbon dioxide power cycle in combination with seawater desalination and an adjustment method thereof |
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2019
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110344898A (en) * | 2019-08-05 | 2019-10-18 | 上海发电设备成套设计研究院有限责任公司 | Absorption type desalination and closed cycle electricity generation system |
| CN110344898B (en) * | 2019-08-05 | 2024-04-23 | 上海发电设备成套设计研究院有限责任公司 | Absorption type sea water desalination and closed cycle power generation system |
| WO2022037711A1 (en) * | 2020-12-28 | 2022-02-24 | 中国长江三峡集团有限公司 | Flexible power station employing supercritical carbon dioxide power cycle in combination with seawater desalination and an adjustment method thereof |
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