CN110344898B - Absorption type sea water desalination and closed cycle power generation system - Google Patents
Absorption type sea water desalination and closed cycle power generation system Download PDFInfo
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- CN110344898B CN110344898B CN201910718666.3A CN201910718666A CN110344898B CN 110344898 B CN110344898 B CN 110344898B CN 201910718666 A CN201910718666 A CN 201910718666A CN 110344898 B CN110344898 B CN 110344898B
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- 239000013535 sea water Substances 0.000 title claims abstract description 100
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 64
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 57
- 238000010248 power generation Methods 0.000 title claims abstract description 31
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 90
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 45
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 45
- 239000000243 solution Substances 0.000 claims description 48
- 239000006096 absorbing agent Substances 0.000 claims description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 28
- 239000013505 freshwater Substances 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 14
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 12
- 239000003507 refrigerant Substances 0.000 claims description 12
- 239000012267 brine Substances 0.000 claims description 10
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 10
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 239000002028 Biomass Substances 0.000 claims description 4
- 230000002745 absorbent Effects 0.000 claims description 3
- 239000002250 absorbent Substances 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 abstract description 20
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000001172 regenerating effect Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 5
- 238000004821 distillation Methods 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
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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
- F01K13/00—General layout or general methods of operation of complete plants
-
- 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
- F01K25/103—Carbon dioxide
-
- 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
- F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
- F01K7/32—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines using steam of critical or overcritical pressure
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention provides an absorption type sea water desalination and closed circulation power generation system, which comprises: the absorption type seawater desalination and closed cycle power generation system provided by the invention uses the waste heat released by the supercritical carbon dioxide circulation to desalinate the seawater through the absorption type seawater desalination loop, can realize the use of low-grade waste heat, has low seawater desalination energy consumption, adopts the supercritical carbon dioxide circulation of a simple regenerative mode, has a simple and compact system structure, has lower working temperature of a generator, can absorb the low temperature Duan Reliang of the heat source, and improves the heat source efficiency.
Description
Technical Field
The invention relates to the technical field of power generation, in particular 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 growth of the population of the world, the rapid development of the economic society and the influence of climate change, the world faces an increasingly serious water deficiency crisis. As an open source increment technology for realizing sustainable utilization of water resources, the seawater desalination can increase the total amount of fresh water, is less affected by climate, has stable water supply, good water quality of product water and strong reliability, can provide high-quality municipal water supply and industrial high-quality water for coastal areas, and becomes an important means for solving the crisis of fresh water resource shortage in coastal areas globally. Currently, global desalination yields exceed 1 hundred million cubic meters per day and increase at rates of more than 10% per year.
In order to obtain better economy, a power generation system and a desalination system are often integrated by adopting a mode of cogeneration. At present, the cogeneration is to combine a steam turbine generator unit with a sea water desalting device, and the three main types are divided: power plant + distillation desalination, power plant + reverse osmosis desalination, power plant + distillation desalination + reverse osmosis desalination. For other forms of generator sets, there is also a need to explore better combinations.
In recent years, supercritical carbon dioxide recycling has become a hotspot and is considered to have a number of potential advantages. The critical point of carbon dioxide is 31 ℃/7.4MPa, and the state when the temperature and the pressure exceed the critical point is the supercritical state. The supercritical carbon dioxide circulation can be combined with various heat sources to form a power generation system, and has good application prospects 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 circulation main heater has a relatively narrow heat absorption temperature range, which may cause heat source loss, in particular, is more unfavorable to sensible heat sources.
Disclosure of Invention
In view of the above-mentioned drawbacks of the prior art, the present invention is to solve the technical problem that when the supercritical carbon dioxide cycle is applied to a power generation system, heat source loss is caused due to a relatively narrow heat absorption temperature interval of the main heater, and in particular, the problem of disadvantage to sensible heat source is solved.
In order to solve the technical problems, the invention provides an absorption type sea water desalination and closed cycle power generation system, which comprises: a heat source, an absorption type sea water 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 outlet of the evaporator is connected with the inlet of the absorber, the outlet of the solution pump is connected with the low-temperature side inlet of the solution heat exchanger, the outlet of the low-temperature side outlet of the solution heat exchanger is connected with the inlet of the generator, the outlet of the solution hydraulic turbine is also connected with the inlet of the solution hydraulic turbine, the outlet of the seawater heat exchanger is connected with the inlet of the seawater heat exchanger, the outlet of the evaporator is connected with the inlet of the seawater heat exchanger, and the outlet of the concentrated brine pump is connected with the inlet of the evaporator;
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 an 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 is converged with a high-pressure side outlet of the low-temperature heat regenerator and is divided into two paths, one path of the low-pressure side outlet of the absorber is connected with a low-temperature side inlet of the condenser, the other path of the low-temperature side outlet of the condenser is connected with a high-pressure side outlet of the medium-temperature heat regenerator and is 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 heater, an outlet of the working medium heater is connected with an inlet of the high-temperature heat regenerator, a low-pressure side outlet of the high-temperature heat regenerator is connected with a low-pressure side inlet of the high-temperature heat regenerator, and a low-pressure side of the high-temperature heat regenerator is connected with a high-temperature side evaporator, and a high-temperature side evaporator is connected with a high-temperature side inlet of the high-temperature heat regenerator, and a high-pressure side evaporator is connected with a high-temperature side inlet of the high-temperature heat regenerator.
The heat source provides heat for the generator of the absorption type sea water desalination loop and the working medium heater of the supercritical carbon dioxide circulation loop.
Alternatively, 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 for the working medium heater, and heat exhausted from the coal-fired boiler is provided for the generator.
Optionally, the working medium pair of the absorption type sea water desalination loop is aqueous solution of lithium bromide. Wherein, water is used as refrigerant and lithium bromide is used as 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 coaxially arranged.
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 more than or equal to 15MPa, the inlet temperature of the turbine is more than or equal to 500 ℃, and the outlet pressure of the turbine is 5MPa to 8MPa.
Optionally, in the absorption type sea water desalination loop, the pressure of the evaporator is 2-8 kPa, and the pressure of the condenser is 0.1-1 MPa.
Optionally, the heat source of the seawater preheater in the absorption type seawater desalination loop is from a precooler in the supercritical carbon dioxide circulation loop.
Compared with the prior art, the absorption type sea water desalination and closed circulation power generation system has the following beneficial effects:
The 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 sea water desalination energy consumption is low.
In the absorption type sea water desalination loop, a generator can be driven by a medium-high temperature heat source, an evaporator absorbs low-temperature heat for evaporating sea water, and the absorber and a condenser can release medium-low grade heat.
In the supercritical carbon dioxide circulation loop, part of waste heat is recovered by the working medium discharged by the turbine through the high-temperature heat regenerator, the medium-temperature heat regenerator and the low-temperature heat regenerator in sequence, then low-grade waste heat is recovered by the evaporator of the absorption type sea water desalination loop, and the low-grade waste heat is cooled by the precooler and finally returned to the inlet of the compressor, so that the use of the low-grade waste heat is realized, and the energy consumption of sea water desalination is greatly reduced.
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 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 provided for a working medium heater, and medium-temperature heat of boiler smoke exhaust is provided for a generator, so that combustion heat is fully utilized.
Drawings
FIG. 1 is a schematic diagram of an absorption type sea water desalination and closed cycle power generation system according to an embodiment of the present invention;
Wherein: 1-compressor, 2-low temperature regenerator, 3-medium temperature regenerator, 4-high temperature regenerator, 5-working medium heater, 6-turbine, 7-generator, 8-precooler, 9-evaporator, 10-absorber, 11-solution pump, 12-solution heat exchanger, 13-gas-liquid separator, 14-solution hydraulic turbine, 15-condenser, 16-water heat exchanger, 17-sea water hydraulic turbine, 18-fresh water hydraulic turbine, 19-concentrated brine pump, 20-generator, 21-sea water preheater, 100-absorption sea water desalination loop, 200-boiler, 300-supercritical carbon dioxide circulation loop.
Detailed Description
The technical scheme of the invention is described in detail below with reference to examples.
As shown in fig. 1, an absorption type sea water desalination and closed cycle power generation system according to an embodiment of the present invention 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 to the generator 20 of the absorption 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, heat generated by combustion of the coal-fired boiler is supplied to the working medium heater 5, and heat discharged from the coal-fired boiler is supplied to the generator 20.
The absorption type sea water desalination circuit 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 sea water preheater 21, a sea water hydraulic turbine 17 and a concentrated salt water pump 19.
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 inlet of the high-temperature side of the condenser 15, the outlet of the high-temperature side 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 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 inlet of the low-temperature side of the solution heat exchanger 12, the outlet of the low-temperature side of the solution heat exchanger 12 is connected with the inlet of the generator 20, the 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 preheating device 21 and the outlet of the water heat exchanger 16 are connected with the inlet of the seawater hydraulic turbine 17, the outlet of the seawater hydraulic turbine 17 is connected with the inlet of the evaporator 9, and the outlet of the evaporator 9 is connected with the inlet of the concentrated salt pump 19.
The supercritical carbon dioxide circulation loop 300 of the embodiment of the invention comprises a compressor 1, a low-temperature regenerator 2, a condenser 15, a medium-temperature regenerator 3, a high-temperature regenerator 4, a turbine 6, a generator 7, a precooler 8 and a working medium heater 5, wherein an outlet of the compressor 1 is respectively connected with a high-pressure side inlet of the low-temperature regenerator 2 and a low-temperature side inlet of an absorber 10, an outlet of the low-temperature side of the absorber 10 is converged with an outlet of the high-pressure side of the low-temperature regenerator 2 and is divided into two paths, one path is connected with the low-temperature side inlet of the condenser 15, the other path is connected with the high-pressure side inlet of the medium-temperature regenerator 3, the outlet of the low-temperature side of the condenser 15 is converged with the high-pressure side outlet of the medium-temperature regenerator 3 and is connected with the high-pressure side inlet of the high-temperature regenerator 4, the outlet of the high-pressure side of the high-temperature regenerator 4 is connected with the inlet of the working medium heater 5, the outlet of the working medium heater 5 is connected with the inlet of the turbine 6, the outlet of the low-pressure side of the absorber 10 is connected with the low-pressure side inlet of the low-temperature regenerator 3, the low-pressure side outlet of the low-temperature regenerator 4 is connected with the low-pressure side inlet of the low-temperature regenerator 3, the low-pressure side of the high-temperature regenerator 9 is connected with the high-pressure side inlet of the high-temperature regenerator 2, and the high-pressure side of the high-temperature regenerator 2 is connected with the high-pressure side inlet of the high-temperature regenerator 9, and the high-pressure side evaporator is connected with the high-pressure inlet of the high-temperature regenerator 2. The turbine 6 powers the generator 7 and the compressor 1.
The working substance pair of the absorption seawater desalination circuit 100 is an aqueous solution of lithium bromide. Wherein, water is used as refrigerant and lithium bromide is used as 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 illustrates an exemplary three-stage compressor.
The precooler 8 is cooled by seawater, and the heat source of the seawater preheater 21 is from the precooler 8 in the supercritical carbon dioxide circulation loop.
As shown in fig. 1, in the supercritical carbon dioxide circulation circuit 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 more than or equal to 15MPa, the inlet temperature of the turbine 6 is more than or equal to 500 ℃, and the outlet pressure of the turbine 6 is 5MPa to 8MPa. The turbine 6 is single-stage, or two-stage or multi-stage and adopts a reheating mode.
In the absorption type sea water desalination circuit 100, the pressure of the evaporator 9 is 2kPa to 8kPa, and the pressure of the condenser 15 is 0.1MPa to 1MPa.
It should be noted that, the devices related to the technical scheme of the present invention all belong to the existing devices, and in the embodiment of the present invention, the following devices are specifically adopted: a compressor (axial-flow multi-stage cold carbon dioxide compressor), a low-temperature regenerator (printed circuit board heat exchanger), a medium-temperature regenerator (printed circuit board heat exchanger), a high-temperature regenerator (printed circuit board heat exchanger), a working medium heater (stainless steel tube heater), a turbine (axial-flow carbon dioxide turbine), a generator (three-phase synchronous generator), a precooler (tube cooler), an evaporator (shell-and-tube evaporator), an absorber (spray absorber), a solution pump (centrifugal pump), a solution heat exchanger (shell-and-tube heat exchanger), a gas-liquid separator (spray separator), a solution hydraulic turbine (centripetal turbine), a condenser (tube cooler), a water heat exchanger (shell-and-tube heat exchanger), a seawater hydraulic turbine (centripetal turbine), a freshwater hydraulic turbine (centripetal turbine), a concentrated brine pump (centrifugal pump), a generator (submerged generator), a seawater heater (shell-and-tube heat exchanger), a boiler (n-type furnace).
Besides the above-mentioned necessary structure, valves, fluid machines, meters, auxiliary facilities, electric systems, instrument control systems, etc. may be arranged according to the system control needs.
The absorption type sea water desalination and closed cycle power generation system of the embodiment of the invention is carried out according to the working method:
In the supercritical carbon dioxide circulation loop 300, carbon dioxide working medium enters the compressor 1 to be pressurized and is divided into two paths of working medium at the outlet of the compressor 1, one path of working medium enters the low-temperature heat regenerator 2 to absorb heat of the working medium discharged by the turbine 6, the other path of working medium absorbs heat by the absorber 10 of the absorption type sea water desalination loop 100, the two paths of working medium are converged and then are divided into two paths of working medium again, one path of working medium absorbs heat of the working medium discharged by the turbine 6 by the medium-temperature heat regenerator 3, the other path of working medium absorbs heat by the condenser 15 of the absorption type sea water desalination loop 100, then the two paths of working medium are converged again to enter the high-temperature heat regenerator 4 to absorb heat of the 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 the working medium heater 5 and enters the turbine 6 to expand and do work, the turbine 6 pushes the generator 7 and the compressor 1, part of waste heat of the working medium discharged by the turbine 6 is recovered by the high-temperature heat regenerator 4, the medium is recovered by the evaporator 9 of the absorption type sea water desalination loop 100, the low-grade sea water is cooled by the precooler 8, and finally the waste heat is recovered by the evaporator 8 of the absorption type sea water desalination loop 1, and finally the waste heat is cooled by the compressor 1. The working medium discharged by the turbine 6 is recycled by a high-temperature heat regenerator 4, a medium-temperature heat regenerator 3 and a low-temperature heat regenerator 2 in sequence, then low-grade waste heat is recycled by an evaporator 9 of the absorption type sea water desalination loop 100, and is cooled by a precooler 8, and finally returns to the inlet of the compressor 1.
Meanwhile, in the absorption type sea water desalination loop 100, a heat source 200 heats a working medium pair in a generator 20, a refrigerant evaporates and enters a gas-liquid separator 13 to carry out gas-liquid separation, the refrigerant steam enters a condenser 15, and the rest concentrated solution enters a solution hydraulic turbine 14 to recover work after being cooled by a solution heat exchanger 12 and then enters an absorber 10; the refrigerant vapor enters a condenser 15 to liquefy and release heat to be transferred to a carbon dioxide working medium, the refrigerant is recycled through a water heat exchanger 16 to be used for preheating seawater, then the fresh water hydraulic turbine 18 is used for recycling work, one path of seawater is preheated by the seawater 21, the other path of seawater is converged through the water heat exchanger 16, then the two paths of seawater are combined and recycled to work through the seawater hydraulic turbine 17, the work enters an evaporator 9, the low-grade waste heat of the carbon dioxide working medium is absorbed by the seawater in the evaporator 9 and then evaporated, the concentrated brine is discharged through a concentrated brine pump, the steam enters an absorber 10 to be absorbed by a solution, the heat released in the absorption process is transferred to the carbon dioxide working medium, the solution in the absorber 100 is input into the solution heat exchanger 12 to be preheated by the solution pump 11, and finally the solution returns to the generator 20.
A specific working example of the absorption type sea water desalination and closed cycle power generation system of the embodiment of the invention is as follows:
In the supercritical carbon dioxide cycle 300, the carbon dioxide working medium firstly enters a compressor 1 to be pressurized to 30MPa, the compressor 1 is subjected to three-stage intermediate cooling, and the carbon dioxide working medium at the outlet of the compressor 1 is divided into two paths: one path absorbs heat of a working medium through a low-temperature heat regenerator 2 and absorbs heat through an absorber 10 of an absorption type sea water desalination loop 100, the two paths of working medium are converged and then are divided into two paths, one path absorbs heat of the working medium through a medium-temperature heat regenerator 3 and absorbs heat of the working medium through the turbine 6, the other path absorbs heat through a condenser 15 of the absorption type sea water desalination loop 100, then the two paths are converged and enter a high-temperature heat regenerator 4 to absorb heat of a high-temperature section of the working medium, the turbine 6 is discharged, the working medium discharged from the high-temperature heat regenerator 4 is heated to 620 ℃ through a working medium heater 5 and then enters the turbine 6 to perform expansion work, the turbine 6 pushes a generator 7 and a compressor 1, the pressure of the working medium discharged from the turbine 6 is reduced to 7MPa, part of 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, then low-grade waste heat is recovered through an evaporator 9 of the absorption type sea water desalination loop, and finally the low-grade waste heat is cooled through a precooler 8, and finally the working medium is returned to an inlet of the compressor 1.
Meanwhile, in the absorption type sea water desalination loop 100, the working substance 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 rest concentrated solution enters the solution hydraulic turbine 14 to recover work after being cooled by the solution heat exchanger 12 and then enters the absorber 10; the refrigerant vapor enters a condenser 15 to liquefy and release heat to be transferred to a carbon dioxide working medium, the refrigerant is recycled through a water heat exchanger 16 to be used for preheating seawater, then the fresh water hydraulic turbine 18 is used for recycling work, one path of seawater is used for recycling work through a seawater preheater 21, the other path of seawater is used for recycling work through the water heat exchanger 16, the two paths of seawater are combined and then enter an evaporator 9, the pressure of the evaporator 9 is 3kPa, the seawater absorbs the low-grade waste heat of the carbon dioxide working medium in the evaporator 9 and then evaporates, the strong brine is discharged through a strong brine pump 19, the steam enters an absorber 10 to be absorbed by 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 the solution heat exchanger 12 through a solution pump 11 to be preheated, and finally returns to the generator 20.
In the process, the power generation efficiency of the supercritical carbon dioxide cycle 300 can reach more than 45%, meanwhile, the absorption type sea water desalination loop 100 utilizes the waste heat of the supercritical carbon dioxide cycle 300 to prepare fresh water, and for a unit with 100MW capacity, the byproduct fresh water can reach 1200 cubes/day, so that the method has considerable economical efficiency.
While specific embodiments of the invention have been described in detail, it will be appreciated that those skilled in the art, upon attaining an understanding of the principles of the invention, may readily make numerous modifications and variations to the present invention. Therefore, all technical solutions which can be obtained by logic analysis, reasoning or limited experiments based on the prior art by the person skilled in the art according to the inventive concept shall be within the scope of protection defined by the claims.
Claims (9)
1. An absorption sea water desalination and closed cycle power generation system, comprising: a heat source, an absorption type sea water 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 outlet of the evaporator is connected with the inlet of the absorber, the outlet of the solution pump is connected with the low-temperature side inlet of the solution heat exchanger, the outlet of the low-temperature side outlet of the solution heat exchanger is connected with the inlet of the generator, the outlet of the solution hydraulic turbine is also connected with the inlet of the solution hydraulic turbine, the outlet of the seawater heat exchanger is connected with the inlet of the seawater heat exchanger, the outlet of the evaporator is connected with the inlet of the seawater heat exchanger, and the outlet of the concentrated brine pump is connected with the inlet of the evaporator;
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 the high-pressure side inlet of the low-temperature heat regenerator and the low-temperature side inlet of the absorber, the low-temperature side outlet of the absorber is converged with the high-pressure side outlet of the low-temperature heat regenerator and is divided into two paths, one path is connected with the low-temperature side inlet of the condenser, the other path is connected with the high-pressure side inlet of the medium-temperature heat regenerator, the low-temperature side outlet of the condenser is converged with the high-pressure side outlet of the medium-temperature heat regenerator and is connected with the high-pressure side inlet of the high-temperature heat regenerator, the high-pressure side outlet of the high-temperature heat regenerator is connected with the inlet of the working medium heater, the outlet of the working medium heater is connected with the inlet of the turbine, the outlet of the turbine is connected with the low-pressure side inlet of the high-temperature heat regenerator, 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 measuring 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 type sea water desalination loop and the working medium heater of the supercritical carbon dioxide circulation loop;
In the absorption type sea water desalination loop, the pressure of the evaporator is 2-8 kPa, and the pressure of the condenser is 0.1-1 MPa.
2. The absorption seawater 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 seawater desalination and closed cycle power generation system of claim 1, wherein the heat source is selected from fossil energy and takes the form of a coal-fired boiler, heat generated by combustion in the coal-fired boiler is provided to the working medium heater, and heat exhausted from the coal-fired boiler is provided to the generator.
4. The absorption seawater desalination and closed cycle power generation system of claim 1, wherein the pair of working media of the absorption seawater desalination loop is an aqueous solution of lithium bromide, wherein water is a refrigerant and lithium bromide is an absorbent.
5. The absorption sea water desalination and closed cycle power generation system as defined in claim 1 wherein the compressor is a two-stage or multi-stage compressor with an intercooler.
6. The absorption seawater desalination and closed cycle power generation system of claim 1, wherein the precooler is cooled with seawater.
7. An absorption seawater desalination and closed cycle power generation system as claimed in claim 1, wherein the compressor, the permeance average and the generator are arranged coaxially in the supercritical carbon dioxide circulation loop.
8. The absorption sea water desalination and closed cycle power generation system of claim 1 wherein in the supercritical carbon dioxide circulation loop, the outlet temperature of the compressor is no 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 5MPa to 8MPa.
9. The absorption seawater desalination and closed cycle power generation system of claim 1, wherein the heat source of the seawater preheater in the absorption seawater desalination loop is from a precooler in the supercritical carbon dioxide circulation loop.
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| CN112249293A (en) * | 2020-10-09 | 2021-01-22 | 东南大学 | Ship nuclear power system with supercritical carbon dioxide circulation and seawater desalination coupling |
| CN112483207A (en) * | 2020-12-10 | 2021-03-12 | 湖南大学 | Supercritical carbon dioxide circulation and double-effect absorption type power circulation combined 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 |
| CN112627925B (en) * | 2020-12-28 | 2023-03-10 | 中国长江三峡集团有限公司 | Flexible power station based on combination of supercritical carbon dioxide power cycle and seawater desalination and adjusting method thereof |
| CN113339696A (en) * | 2021-05-18 | 2021-09-03 | 西安交通大学 | Carbon dioxide pressurizing storage device and method |
| CN215444173U (en) * | 2021-08-26 | 2022-01-07 | 比亚迪股份有限公司 | Supercritical carbon dioxide cycle power generation-brine lithium extraction coupling system |
| US11311818B1 (en) * | 2021-09-28 | 2022-04-26 | King Abdulaziz University | Brayton cycle adsorption desalination system |
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