CN110697821B - Seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system - Google Patents
Seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system Download PDFInfo
- Publication number
- CN110697821B CN110697821B CN201910921503.5A CN201910921503A CN110697821B CN 110697821 B CN110697821 B CN 110697821B CN 201910921503 A CN201910921503 A CN 201910921503A CN 110697821 B CN110697821 B CN 110697821B
- Authority
- CN
- China
- Prior art keywords
- seawater
- heat
- carbon dioxide
- distiller
- effect
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
- C02F1/14—Treatment of water, waste water, or sewage by heating by distillation or evaporation using solar energy
-
- 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
- C02F1/06—Flash evaporation
-
- 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
-
- 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
- Y02A20/138—Water desalination using renewable energy
- Y02A20/142—Solar thermal; Photovoltaics
-
- 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
- Y02A20/20—Controlling water pollution; Waste water treatment
- Y02A20/208—Off-grid powered water treatment
- Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
Abstract
The invention discloses a seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system, and the whole system is applied to the field of seawater desalination. The main equipment comprises a solar heat collector, a multi-effect seawater distiller, an expansion tank, a heat conduction oil-seawater heat exchanger, a fused salt-heat conduction oil heat exchanger, a high-temperature fused salt storage tank, a low-temperature fused salt storage tank, a carbon dioxide evaporator, a carbon dioxide compressor unit, a carbon dioxide expansion unit, a condenser and the like. By arranging the molten salt heat storage module, the day and night intermittence of solar energy is overcome, so that the system can continuously work; by arranging the carbon dioxide heat pump unit, the carbon dioxide is compressed to the supercritical carbon dioxide with high density by using the compressor, and the volume of equipment for circulating the heat pump is small; the seawater source trans-critical carbon dioxide heat pump system is used for absorbing seawater heat, and then the seawater is desalted in a multi-effect mode through the seawater distiller, so that efficient seawater desalination is achieved.
Description
Technical Field
The invention belongs to the field of solar energy utilization and seawater desalination, relates to a heat pump seawater desalination technology, and particularly relates to a solar-assisted seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system technology.
Background
Fresh water is one of the substances that humans have come to live and develop. The shortage of fresh water resources is becoming serious and serious, and becomes a global environmental problem. And nearly 97.5 percent of the total water resource in the world is the saline water resource such as seawater and the like. The research on the efficient and environment-friendly seawater desalination technology is significant for solving the problem of water resource shortage. The existing technology for desalinating seawater by utilizing solar energy is mature, compared with the traditional power source and heat source, the solar energy has the advantages of safety, environmental protection, no consumption of conventional energy, no pollution, high purity of obtained fresh water and the like, the combination of two systems of solar energy collection and desalination process is a sustainable development seawater desalination technology, and the technology has great application potential in regions with shortage of fresh water resources and high environmental protection requirements. In the existing seawater desalination technology, on the basis of solar energy, the modes of coupling and utilizing wind energy, terrestrial heat, industrial waste heat or other energy sources are common.
However, in terms of the current solar seawater desalination technology, the pure solar seawater desalination efficiency is low, the pure heat pump seawater desalination cost is high, and the organic working medium adopted by the traditional heat pump can cause greenhouse effect and ozone layer holes. The conventional solar seawater desalination equipment is generally large in size, high in desalination energy consumption, easy to corrode and high in overall cost. In addition, the solar energy has instability and day and night intermittence, which causes the discontinuous work of the solar seawater desalination system, influences the energy efficiency and the water generation ratio of the solar seawater desalination system to a certain extent, and increases the cost of seawater desalination.
Disclosure of Invention
Aiming at the defects and shortcomings of the existing solar seawater desalination technology, the invention aims to provide a solar-assisted seawater source trans-critical carbon dioxide heat pump comprehensive energy system for realizing efficient seawater desalination.
In order to achieve the purpose, the invention adopts the following technical scheme to realize the purpose:
a seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system comprises a solar heat collection and storage unit, a trans-critical carbon dioxide heat pump unit and a seawater desalination unit, and is characterized in that,
-the solar heat collection and storage unit comprises at least a solar heat collector, a high temperature side of a heat transfer oil-seawater heat exchanger, and a heat transfer oil heat exchange side of a molten salt-heat transfer oil heat exchanger, wherein,
the solar heat collector, the high-temperature side of the heat conducting oil-seawater heat exchanger and the heat conducting oil heat exchanging side of the molten salt-heat conducting oil heat exchanger are sequentially communicated through pipelines to form a closed heat conducting oil circulation loop;
a bypass pipeline is arranged between an inlet and an outlet of the solar heat collector, a bypass valve is arranged on the bypass pipeline, and a main path valve is arranged at the inlet of the solar heat collector;
one end opening of a fused salt heat exchange side of the fused salt-heat conducting oil heat exchanger is communicated with a low-temperature fused salt storage tank through a pipeline, and the other end opening of the fused salt-heat conducting oil heat exchanger is communicated with a high-temperature fused salt storage tank through a pipeline;
the transcritical carbon dioxide heat pump unit at least comprises a cold side of a carbon dioxide evaporator, a carbon dioxide compressor unit, a carbon dioxide expansion unit and a heating pipeline in the first-effect seawater distiller, wherein the cold side of the carbon dioxide evaporator, the carbon dioxide compressor unit, the heating pipeline in the first-effect seawater distiller and the carbon dioxide expansion unit are sequentially communicated through pipelines to form a closed carbon dioxide circulation loop;
the seawater desalination unit at least comprises a first effect seawater distiller, a second effect seawater distiller, a condenser, a low-temperature side of a heat transfer oil-seawater heat exchanger, a seawater shunt three-way regulating valve and a seawater and brine three-way mixing valve, wherein,
the inlet of the seawater shunt three-way regulating valve is formed into a fresh seawater inlet which is not desalted, the first outlet of the seawater shunt three-way regulating valve sequentially passes through the low-temperature side of the condenser and the low-temperature side of the heat conduction oil-seawater heat exchanger through pipelines and then is respectively communicated with the fresh seawater inlets at the tops of the first effect seawater distiller and the second effect seawater distiller, and pressure regulating valves are respectively arranged on the fresh seawater inlet pipelines at the tops of the first effect seawater distiller and the second effect seawater distiller;
the top or the position close to the top of the first-effect seawater distiller and the second-effect seawater distiller is provided with a fresh water steam outlet, the bottom of the first-effect seawater distiller is provided with a strong brine outlet, the fresh water steam outlet of the first-effect seawater distiller is communicated with the inlet of a heating pipeline arranged in the second-effect seawater distiller through a pipeline, the outlet of the heating pipeline in the second-effect seawater distiller and the fresh water steam outlet of the second-effect seawater distiller are respectively communicated with the high-temperature side inlet of the condenser through pipelines, and the high-temperature side outlet of the condenser is formed as a desalted water outlet; the strong brine outlet of the first effect seawater distiller is led in through a pipeline in the second effect seawater distiller, the strong brine outlet of the second effect seawater distiller is divided into two branches, wherein the strong brine is directly discharged through the first branch, a regulating valve is arranged on the first branch, the second branch is communicated with the first inlet of the seawater brine tee-joint mixing valve, the second inlet of the seawater brine tee-joint mixing valve is communicated with the second outlet of the seawater shunting tee-joint regulating valve through a pipeline, the outlet of the seawater brine tee-joint mixing valve is communicated with the hot side inlet of the carbon dioxide evaporator through a pipeline, and the hot side outlet of the carbon dioxide evaporator is formed into a seawater outlet.
Preferably, in the transcritical carbon dioxide heat pump unit, the carbon dioxide expansion unit expands the introduced carbon dioxide to a subcritical state, the subcritical carbon dioxide is introduced to a cold side of the carbon dioxide evaporator to absorb heat, and the subcritical carbon dioxide is compressed by the compressor unit to reach a supercritical state.
Preferably, the solar heat collection and storage unit further comprises a heat conduction oil pump, and the heat conduction oil pump is arranged on the heat conduction oil circulation loop and used for driving the heat conduction oil in the circulation loop to circularly flow among all the components.
Further, the heat-conducting oil pump is arranged on an inlet pipeline and/or an outlet pipeline of the solar heat collector.
Preferably, an expansion tank is further arranged in the heat conduction oil circulation loop, and the expansion tank is used for adapting to the increase of the volume of the heated heat conduction oil and supplementing the heated heat conduction oil when the heat conduction oil is insufficient.
Further, the expansion tank is arranged on a communication pipeline between the solar heat collector and the high-temperature side of the heat conduction oil-seawater heat exchanger.
Furthermore, a heat conduction oil supply pipeline with a valve and a heat conduction oil discharge pipeline with a valve are also arranged on the expansion tank, and when the heat conduction oil needs to be replaced, the valve on the heat conduction oil discharge pipeline is opened to discharge the old heat conduction oil; and opening a valve on the heat-conducting oil supply pipeline when heat-conducting oil needs to be added.
Preferably, the temperature of the fresh seawater sequentially flows through the condenser and the heat transfer oil-seawater heat exchanger is increased, and then the fresh seawater enters the first-effect seawater distiller and the second-effect seawater distiller for fractional desalination, wherein the working pressure in the first-effect seawater distiller is higher than that in the second-effect seawater distiller.
Preferably, the concentrated brine discharged by the second-effect seawater distiller and the fresh seawater shunted by the seawater shunt three-way regulating valve are mixed in a certain proportion in the seawater and brine three-way mixing valve to be used as a heat source of the carbon dioxide evaporator, so that the average heat absorption temperature of the carbon dioxide heat pump unit is increased.
Preferably, the seawater desalination unit further comprises a seawater drainage pump, a concentrated brine pump and a desalination water pump, wherein the seawater drainage pump is arranged on the seawater discharge pipeline of the carbon dioxide evaporator, the concentrated brine pump is arranged on a concentrated brine outlet pipeline of the second-effect seawater distiller, and the desalination water pump is arranged on a high-temperature side outlet pipeline of the condenser.
Preferably, the system comprises at least a heat storage and pump desalination mode, a heat release and pump desalination mode, a heat storage and flash desalination mode, and a heat release and flash desalination mode.
Further, when the solar energy is sufficient, a heat storage and heat pump desalination mode is started, at the moment, a bypass valve in the solar heat collection and storage unit is closed, a main valve is opened, heat conduction oil in the heat conduction oil circulation loop is conveyed into the solar heat collector, heated high-temperature heat conduction oil is introduced into a heat conduction oil heat exchange side of the molten salt-heat conduction oil heat exchanger, low-temperature molten salt in the low-temperature molten salt storage tank is conveyed to a molten salt heat exchange side of the molten salt-heat conduction oil heat exchanger and is heated to the heat storage temperature by the high-temperature heat conduction oil in the heat conduction oil heat exchange side, and then the low-temperature molten salt is introduced into the high-temperature molten salt storage tank; in a heat storage and heat pump desalination mode, in the carbon dioxide heat pump unit, carbon dioxide introduced into the cold side of the carbon dioxide evaporator absorbs heat and then forms 10-20 ℃ of superheated gas, the superheated carbon dioxide is compressed by the carbon dioxide compressor unit and then reaches a supercritical state, the temperature reaches the high temperature of 100-120 ℃, then the high-temperature supercritical carbon dioxide enters a heating pipeline of the first-effect seawater distiller to heat seawater in the seawater, the carbon dioxide after heat release is expanded by the carbon dioxide expander unit and then converts energy into mechanical energy to form a low-temperature and low-pressure carbon dioxide gas-liquid mixture, and finally the carbon dioxide gas-liquid mixture is introduced into the cold side of the evaporator and then is changed into carbon dioxide superheated gas again to complete carbon dioxide working medium circulation; in the heat storage and heat pump desalination mode, the fresh seawater introduced into the low-temperature side of the heat transfer oil-seawater heat exchanger is heated to about 40 ℃ and then is respectively conveyed into the first-effect seawater distiller and the second-effect seawater distiller, and the fresh seawater and the concentrated brine generated by the second-effect seawater distiller are directly mixed in the seawater brine three-way mixing valve and then are introduced into the hot side of the carbon dioxide evaporator to serve as a heat source of the carbon dioxide evaporator.
Further, when the solar energy is sufficient but the electric energy is insufficient, the heat release and heat pump desalination mode is started, at the moment, a main path valve of the solar heat collector is closed, a bypass valve is opened, high-temperature molten salt in the high-temperature molten salt storage tank flows into a molten salt heat exchange side of the molten salt-heat conduction oil heat exchanger, heat conduction oil in the heat conduction oil circulation loop is heated and the temperature is reduced, and then the heated heat conduction oil is introduced into the low-temperature molten salt storage tank, and at the moment, the working processes of the carbon dioxide heat pump circulation unit and the seawater desalination unit are the same as those in the heat storage and heat pump desalination mode.
Further, when the solar energy is sufficient, the heat storage and flash evaporation desalination mode is started, and the working process of the solar heat collection and storage unit is the same as that in the heat storage and heat pump desalination mode; at the moment, the carbon dioxide heat pump circulation unit stops working, new seawater completely flows into the low-temperature side of the condenser under the action of the seawater shunt three-way regulating valve, and flows into the low-temperature side of the heat conduction oil-seawater heat exchanger after being preheated by condensate gas to be heated to the flash evaporation temperature; the pressure regulating valve at the top of the first-effect seawater distiller is closed, the pressure regulating valve at the top of the second-effect seawater distiller is opened, new seawater in the second-effect seawater distiller is introduced into the second-effect seawater distiller, the pressure is reduced to flash evaporation pressure under the action of the pressure regulating valve, flash evaporation is completed in the second-effect seawater distiller, steam after flash evaporation flows into the condenser and is condensed on the high-temperature side, and strong brine generated in the second-effect seawater distiller is directly discharged.
Further, when the solar energy is insufficient and the electric energy is insufficient, the heat release and flash desalination mode is started, at the moment, a main path valve of the solar heat collector is closed, a bypass valve is opened, high-temperature molten salt in the high-temperature molten salt storage tank flows into a molten salt heat exchange side of the molten salt-heat conduction oil heat exchanger, heat conduction oil in a heat conduction oil circulation loop is heated, the temperature is reduced, and then the heated high-temperature molten salt is introduced into the low-temperature molten salt storage tank, and at the moment, the working process of the seawater desalination unit is the same as that in the heat storage and flash desalination mode.
Preferably, when no electric energy is input to the carbon dioxide compressor unit, the pressure regulating valve at the top of the second-effect seawater distiller is regulated to realize flash evaporation to prepare desalted water.
Furthermore, the system can also drive the carbon dioxide compressor unit by a wind turbine, upgrade the carbon dioxide compressor unit into a wind power desalination water system, and does not need to obtain electric energy from a power grid, thereby being beneficial to the operation of an island.
Compared with the prior art, the solar-assisted seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system has the remarkable technical advantages that: (1) in the seawater desalination system, a fused salt heat storage module is added to a solar heat collection and storage unit, so that the characteristic of solar energy intermittent in day and night is overcome, and the seawater desalination system can continuously work; (2) in the seawater desalination system, a carbon dioxide heat pump unit is arranged, the temperature of a carbon dioxide critical point is close to the ambient temperature, and carbon dioxide is compressed to common supercritical carbon dioxide by a compressor; (3) by adopting a negative-pressure low-temperature multi-effect seawater desalination technology, the corrosion of equipment can be effectively reduced at low temperature, and the negative pressure can reduce the temperature required by seawater distillation and reduce the desalination energy consumption; (4) the system utilizes solar energy to preheat seawater and combines transcritical carbon dioxide heat pump circulation to reduce seawater desalination cost.
Drawings
FIG. 1 is a schematic diagram of a seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings and examples.
As shown in fig. 1, the solar-assisted seawater source transcritical carbon dioxide heat pump circulation multi-effect seawater desalination system comprises a seawater drainage pump 1, a carbon dioxide evaporator 2, a carbon dioxide compressor 3, a carbon dioxide expander 4, a first-effect seawater distiller 5, a second-effect seawater distiller 6, a concentrated brine pump 7, a desalination water pump 8, a condenser 9, a solar heat collector 10, an expansion tank 11, a heat-conducting oil-seawater heat exchanger 12, a molten salt-heat-conducting oil heat exchanger 13, a low-temperature molten salt storage tank 14, a high-temperature molten salt storage tank 15, a heat-conducting oil pump 16, regulating valves V1, V2, V5, V6, V7, V8, V9, a mixing valve V3, a three-way regulating valve V4, necessary pipelines and the like. Specifically, the solar-assisted seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system comprises a solar heat collection and storage unit, a trans-critical carbon dioxide heat pump unit and a seawater desalination unit.
The solar heat collection and storage unit at least comprises a solar heat collector 10, a high-temperature side of a heat conduction oil-seawater heat exchanger 12 and a heat conduction oil heat exchange side of a molten salt-heat conduction oil heat exchanger 13, wherein the solar heat collector 10, the high-temperature side of the heat conduction oil-seawater heat exchanger 12 and the heat conduction oil heat exchange side of the molten salt-heat conduction oil heat exchanger 13 are sequentially communicated through a pipeline to form a closed heat conduction oil circulation loop; a bypass pipeline is arranged between an inlet and an outlet of the solar heat collector 10, a bypass valve V8 is arranged on the bypass pipeline, and a main pipeline valve V7 is arranged at the inlet of the solar heat collector 10; one end opening of the fused salt heat exchange side of the fused salt-heat conducting oil heat exchanger 13 is communicated with a low-temperature fused salt storage tank 14 through a pipeline, and the other end opening is communicated with a high-temperature fused salt storage tank 15 through a pipeline. A heat conduction oil pump 16 is further disposed in the heat conduction oil circulation loop, specifically, the heat conduction oil pump 16 may be disposed on an inlet pipeline and/or an outlet pipeline of the solar thermal collector 10, and the heat conduction oil pump 16 is configured to drive the heat conduction oil in the heat conduction oil circulation loop to circulate among the components. An expansion tank 11 is further arranged in the heat conduction oil circulation loop, specifically, the expansion tank 11 can be arranged on a communication pipeline between the solar heat collector 10 and the high-temperature side of the heat conduction oil-seawater heat exchanger 12, and the expansion tank 11 is arranged in the heat conduction oil circulation loop and is used for adapting to the effects that the heat conduction oil is heated to increase the volume and supplement when the heat conduction oil is insufficient. Furthermore, a heat conduction oil supply pipeline with a valve V5 and a heat conduction oil discharge pipeline with a valve V6 are arranged on the expansion tank 11, when heat conduction oil needs to be replaced, the valve V6 is opened, old heat conduction oil is discharged, and new heat conduction oil is added from the valve V5.
The transcritical carbon dioxide heat pump unit at least comprises a cold side of a carbon dioxide evaporator 2, a carbon dioxide compressor unit 3, a carbon dioxide expansion unit 4 and a heating pipeline in a first-effect seawater distiller 5, wherein the cold side of the carbon dioxide evaporator 2, the carbon dioxide compressor unit 3, the heating pipeline in the first-effect seawater distiller 5 and the carbon dioxide expansion unit 4 are sequentially communicated through pipelines to form a closed carbon dioxide circulation loop. The transcritical carbon dioxide heat pump unit uses carbon dioxide as a circulating working medium, the carbon dioxide expansion unit 4 expands the carbon dioxide to a subcritical state, the subcritical carbon dioxide absorbs heat through the carbon dioxide evaporator 2 and is compressed by the carbon dioxide compression unit 3 to reach a supercritical state.
The seawater desalination unit at least comprises a first-effect seawater distiller 5, a second-effect seawater distiller 6, a condenser 9, a low-temperature side of a heat conduction oil-seawater heat exchanger 12, a seawater shunt three-way regulating valve V4 and a seawater and brine three-way mixing valve V3, wherein an inlet of the seawater shunt three-way regulating valve V4 is formed as a fresh seawater inlet which is not desalinated, a first outlet of the seawater shunt three-way regulating valve V4 sequentially passes through the low-temperature side of the condenser 9 and the low-temperature side of the heat conduction oil-seawater heat exchanger 12 through pipelines and then is respectively communicated with fresh seawater inlets at the tops of the first-effect seawater distiller 5 and the second-effect seawater distiller 6, and pressure regulating valves V1 and V2 are respectively arranged on fresh seawater inlet pipelines at the tops of the first-effect seawater distiller 5 and the second-effect seawater distiller 6; the top or the position close to the top of the first-effect seawater distiller 5 and the second-effect seawater distiller 6 are respectively provided with a fresh water steam outlet, the bottom of the first-effect seawater distiller is respectively provided with a strong brine outlet, the fresh water steam outlet of the first-effect seawater distiller 5 is communicated with the inlet of a heating pipeline arranged in the second-effect seawater distiller 6 through a pipeline, the outlet of the heating pipeline in the second-effect seawater distiller 6 and the fresh water steam outlet of the second-effect seawater distiller 6 are respectively communicated with the high-temperature side inlet of the condenser 9 through pipelines, and the high-temperature side outlet of the condenser 9 is formed as a desalted water exhaust outlet; a strong brine outlet of the first-effect seawater distiller 5 is introduced into a second-effect seawater distiller 6 through a pipeline, the strong brine outlet of the second-effect seawater distiller 6 is divided into two branches, the concentrated brine is directly discharged by the first branch, the first branch is provided with a regulating valve V9, the second branch is communicated with a first inlet of a seawater brine three-way mixing valve V3, a second inlet of the seawater brine three-way mixing valve V3 is communicated with a second outlet of a seawater shunt three-way regulating valve V4 through a pipeline, an outlet of the seawater brine three-way mixing valve V3 is communicated with a hot side inlet of the carbon dioxide evaporator 2 through a pipeline, a hot side outlet of the carbon dioxide evaporator 2 is formed as a seawater outlet, the concentrated brine and the fresh seawater are mixed in a certain proportion in the seawater brine three-way mixing valve V3 to be used as a heat source of the carbon dioxide evaporator 2, and the average heat absorption temperature of the carbon dioxide heat pump unit is improved.
In the seawater desalination unit, fresh seawater sequentially flows through a condenser 9 and a heat transfer oil-seawater heat exchanger 12, the temperature is raised, and then the fresh seawater enters a first-effect seawater distiller 5 and a second-effect seawater distiller 6 for fractional desalination. Wherein the pressure in the first effect seawater distiller 5 is higher than that in the second effect seawater distiller 6. Preferably, the brine outlet of the first effect seawater distiller 5 is led to the bottom of the second effect seawater distiller 6 through a pipeline. Further, the seawater desalination unit further comprises a seawater draining pump 1, a concentrated brine pump 7 and a desalination water pump 8, wherein the seawater draining pump 1 is arranged on a seawater discharging pipeline of the carbon dioxide evaporator 2, the concentrated brine pump 7 is arranged on a concentrated brine outlet pipeline of the second-effect seawater distiller 6, and the desalination water pump 8 is arranged on a high-temperature side outlet pipeline of the condenser 9.
The solar-assisted seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system at least comprises four seawater desalination modes, namely a heat storage and heat pump desalination mode, a heat release and heat pump desalination mode, a heat storage and flash evaporation desalination mode, a heat release and flash evaporation desalination mode and the like.
When the solar energy is sufficient, the heat storage and heat pump desalination mode is started, at the moment, the bypass valve V8 in the solar heat collection and storage unit is closed, the main valve V7 is opened, the heat conduction oil in the heat conduction oil circulation loop enters the solar heat collector 10 under the driving of the heat conduction oil pump 16, the heated high-temperature heat conduction oil flows into the high-temperature side of the molten salt-heat conduction oil heat exchanger 13, the low-temperature molten salt in the low-temperature molten salt storage tank 14 is conveyed to the molten salt heat exchange side of the molten salt-heat conduction oil heat exchanger 13 and is heated to the heat storage temperature by the high-temperature heat conduction oil, and then the heated high-temperature molten salt is introduced into the high-temperature molten salt storage tank 15.
With continued reference to fig. 1, in the heat storage and heat pump desalination mode, the temperature of the superheated carbon dioxide gas in the carbon dioxide heat pump unit after absorbing heat through the cold side of the carbon dioxide evaporator 2 is 10-20 ℃. The superheated carbon dioxide gas is compressed by the carbon dioxide compressor unit 3 and then reaches a supercritical state, and the temperature can reach 100-120 ℃. The high-temperature supercritical carbon dioxide enters a heating pipeline of the first-effect seawater distiller 5 to heat the seawater in the first-effect seawater distiller. The carbon dioxide after heat release is converted into mechanical energy by recovering energy in the carbon dioxide through the carbon dioxide expansion unit 4, and then the carbon dioxide is changed into a low-temperature and low-pressure carbon dioxide gas-liquid mixture. Finally, the carbon dioxide gas-liquid mixture passes through the cold side of the evaporator 2 and then is changed into carbon dioxide superheated gas again, and the circulation of the carbon dioxide working medium is completed.
With continued reference to fig. 1, in the heat storage and heat pump desalination mode, the fresh seawater in the seawater desalination loop is divided into two branches, wherein the first fresh seawater branch sequentially flows through the low-temperature side of the condenser 9 and the low-temperature side of the heat transfer oil-seawater heat exchanger 12 to absorb heat and then enters the first effect seawater distiller 5, so as to reduce the irreversible heat transfer loss in the first effect seawater distiller 5. The second new seawater branch and the concentrated brine generated by the second effect seawater distiller 6 are directly mixed at a mixing valve V3 and then are introduced into the hot side of the carbon dioxide evaporator 2 to be used as a heat source of the carbon dioxide evaporator 2. And the fresh water steam and the strong brine automatically flow into the second-effect seawater distiller 6 step by step to heat the seawater with lower pressure, finally the fresh water steam of the first-effect seawater distiller 5 and the second-effect seawater distiller 6 is liquefied in a condenser 9, and the strong brine is discharged from the bottom of the second-effect seawater distiller 6 and then is mixed with the fresh seawater of the second branch at a mixing valve V3.
Referring to fig. 1, when solar energy is sufficient but the power is insufficient, the heat release and heat pump desalination mode is initiated, wherein the main valve V7 of the solar collector 10 is closed and the bypass valve V8 thereof is opened. The high-temperature molten salt in the high-temperature molten salt storage tank 15 flows into the molten salt heat exchange side of the molten salt-heat conducting oil heat exchanger 13, heats the heat conducting oil in the heat conducting oil circulation loop to reduce the temperature, and then flows into the low-temperature molten salt storage tank 14. At the moment, the working processes of the carbon dioxide heat pump circulating unit and the seawater desalination unit are the same as those in the heat storage and heat pump desalination modes.
Referring to fig. 1, when the solar energy is sufficient, the heat storage and flash desalination mode is started, and at this time, the working process of the solar heat collection and storage unit is the same as that in the heat storage and heat pump desalination mode. At this time, the carbon dioxide heat pump circulation unit stops working, and the fresh seawater completely flows into the low-temperature side of the condenser 9 under the action of the seawater shunt three-way regulating valve V4, and flows into the low-temperature side of the heat transfer oil-seawater heat exchanger 12 after being preheated by the condensed gas, and is heated to the flash evaporation temperature. Throttle V1 is closed and the pressure of the seawater is reduced to the flash pressure by throttle V2 and the flash is completed in the second effect seawater distiller 6. The steam after flash evaporation flows into the high-temperature side of the condenser 9 to be condensed, the concentrated brine generated in the second-effect seawater distiller 6 is directly discharged through a valve V9, and a mixing valve V3 is closed.
Referring to fig. 1, when solar energy is insufficient and electric energy is also insufficient, the heat release and flash desalination mode is started, wherein the main valve V7 of the solar collector 10 is closed and the bypass valve V8 thereof is opened. The high-temperature molten salt in the high-temperature molten salt storage tank 15 flows into the molten salt heat exchange side of the molten salt-heat conducting oil heat exchanger 13, heats the heat conducting oil in the heat conducting oil circulation loop to reduce the temperature, and then flows into the low-temperature molten salt storage tank 14. At the moment, the working process of the seawater desalination unit is the same as that in the heat storage and flash evaporation desalination modes.
The present invention is not limited to the above preferred embodiments, but rather, any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (14)
1. A seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system comprises a solar heat collection and storage unit, a trans-critical carbon dioxide heat pump unit and a seawater desalination unit, and is characterized in that,
the solar heat collection and storage unit at least comprises a solar heat collector, a high-temperature side of a heat conduction oil-seawater heat exchanger and a heat conduction oil heat exchange side of a molten salt-heat conduction oil heat exchanger, wherein,
the solar heat collector, the high-temperature side of the heat conducting oil-seawater heat exchanger and the heat conducting oil heat exchanging side of the molten salt-heat conducting oil heat exchanger are sequentially communicated through pipelines to form a closed heat conducting oil circulation loop;
a bypass pipeline is arranged between an inlet and an outlet of the solar heat collector, a bypass valve is arranged on the bypass pipeline, and a main path valve is arranged at the inlet of the solar heat collector;
one end opening of a fused salt heat exchange side of the fused salt-heat conducting oil heat exchanger is communicated with a low-temperature fused salt storage tank through a pipeline, and the other end opening of the fused salt-heat conducting oil heat exchanger is communicated with a high-temperature fused salt storage tank through a pipeline;
the transcritical carbon dioxide heat pump unit at least comprises a cold side of a carbon dioxide evaporator, a carbon dioxide compressor unit, a carbon dioxide expansion unit and a heating pipeline in the first-effect seawater distiller, wherein the cold side of the carbon dioxide evaporator, the carbon dioxide compressor unit, the heating pipeline in the first-effect seawater distiller and the carbon dioxide expansion unit are sequentially communicated through pipelines to form a closed carbon dioxide circulation loop;
the seawater desalination unit at least comprises a first-effect seawater distiller, a second-effect seawater distiller, a condenser, the low-temperature side of a heat conduction oil-seawater heat exchanger, a seawater shunt three-way regulating valve and a seawater and brine three-way mixing valve, wherein,
the inlet of the seawater shunt three-way regulating valve is formed into a fresh seawater inlet which is not desalted, the first outlet of the seawater shunt three-way regulating valve sequentially passes through the low-temperature side of the condenser and the low-temperature side of the heat conduction oil-seawater heat exchanger through pipelines and then is respectively communicated with the fresh seawater inlets at the tops of the first effect seawater distiller and the second effect seawater distiller, and pressure regulating valves are respectively arranged on the fresh seawater inlet pipelines at the tops of the first effect seawater distiller and the second effect seawater distiller;
the top or the position close to the top of the first-effect seawater distiller and the second-effect seawater distiller is provided with a fresh water steam outlet, the bottom of the first-effect seawater distiller is provided with a strong brine outlet, the fresh water steam outlet of the first-effect seawater distiller is communicated with the inlet of a heating pipeline arranged in the second-effect seawater distiller through a pipeline, the outlet of the heating pipeline in the second-effect seawater distiller and the fresh water steam outlet of the second-effect seawater distiller are respectively communicated with the high-temperature side inlet of the condenser through pipelines, and the high-temperature side outlet of the condenser is formed as a desalted water outlet; a strong brine outlet of the first-effect seawater distiller is introduced into the second-effect seawater distiller through a pipeline, the strong brine outlet of the second-effect seawater distiller is divided into two branches, wherein the first branch directly discharges strong brine, a regulating valve is arranged on the first branch, the second branch is communicated with a first inlet of a seawater brine three-way mixing valve, a second inlet of the seawater brine three-way mixing valve is communicated with a second outlet of the seawater diversion three-way regulating valve through a pipeline, an outlet of the seawater brine three-way mixing valve is communicated with a hot side inlet of the carbon dioxide evaporator through a pipeline, and a hot side outlet of the carbon dioxide evaporator is formed as a seawater outlet;
the system at least comprises a heat storage and heat pump desalination mode, a heat release and heat pump desalination mode, a heat storage and flash evaporation desalination mode and a heat release and flash evaporation desalination mode.
2. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein in the trans-critical carbon dioxide heat pump unit, the carbon dioxide expansion unit expands the introduced carbon dioxide to a subcritical state, the subcritical carbon dioxide is introduced to a cold side of the carbon dioxide evaporator to absorb heat, and the subcritical carbon dioxide is compressed by the compressor unit to reach a supercritical state.
3. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein the solar heat collection and storage unit further comprises a heat conduction oil pump, and the heat conduction oil pump is arranged on the heat conduction oil circulation loop and used for driving heat conduction oil in the circulation loop to circularly flow among all components.
4. The seawater source transcritical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 3, wherein the heat transfer oil pump is arranged on the inlet pipeline and/or the outlet pipeline of the solar heat collector.
5. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein an expansion tank is further arranged in the heat transfer oil circulation loop, and the expansion tank is used for adapting to volume increase caused by heating of heat transfer oil and supplementing when the heat transfer oil is insufficient.
6. The seawater source transcritical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 5, wherein the expansion tank is arranged on a communicating pipe between the solar heat collector and the high temperature side of the heat transfer oil-seawater heat exchanger.
7. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 6, wherein the expansion tank is further provided with a heat conduction oil supply pipeline with a valve and a heat conduction oil discharge pipeline with a valve, and when heat conduction oil needs to be replaced, the valve on the heat conduction oil discharge pipeline is opened to discharge old heat conduction oil; and opening a valve on the heat-conducting oil supply pipeline when heat-conducting oil needs to be added.
8. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein the temperature of fresh seawater sequentially passes through the condenser and the heat transfer oil-seawater heat exchanger, and then the fresh seawater is subjected to fractional desalination in a first-effect seawater distiller and a second-effect seawater distiller, wherein the working pressure in the first-effect seawater distiller is higher than that in the second-effect seawater distiller.
9. The seawater source transcritical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein the concentrated brine discharged from the second effect seawater distiller and the fresh seawater branched by the seawater branched three-way regulating valve are mixed in a certain proportion in the seawater branched three-way mixing valve to be used as a heat source of the carbon dioxide evaporator, so that the average heat absorption temperature of the carbon dioxide heat pump unit is increased.
10. The seawater source transcritical carbon dioxide heat pump cycle multiple-effect seawater desalination system of claim 1, wherein the seawater desalination unit further comprises a seawater drain pump, a concentrated brine pump and a desalination water pump, wherein the seawater drain pump is arranged on the seawater discharge pipeline of the carbon dioxide evaporator, the concentrated brine pump is arranged on the concentrated brine outlet pipeline of the second-effect seawater distiller, and the desalination water pump is arranged on the high-temperature side outlet pipeline of the condenser.
11. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein when solar energy is sufficient, a heat storage and heat pump desalination mode is started, at this time, a bypass valve in the solar heat collection and storage unit is closed, a main valve is opened, heat transfer oil in the heat transfer oil circulation loop is conveyed to the solar heat collector, heated high-temperature heat transfer oil is introduced into a heat transfer oil heat exchange side of the molten salt-heat transfer oil heat exchanger, and low-temperature molten salt in the low-temperature molten salt storage tank is conveyed to a molten salt heat exchange side of the molten salt-heat transfer oil heat exchanger and heated to a heat storage temperature by high-temperature heat transfer oil in the heat transfer oil heat exchange side, and then introduced into the high-temperature molten salt storage tank; in a heat storage and heat pump desalination mode, in the carbon dioxide heat pump unit, carbon dioxide introduced into the cold side of the carbon dioxide evaporator absorbs heat and then forms 10-20 ℃ of superheated gas, the superheated carbon dioxide is compressed by the carbon dioxide compressor unit and then reaches a supercritical state, the temperature reaches the high temperature of 100-120 ℃, then the high-temperature supercritical carbon dioxide enters a heating pipeline of the first-effect seawater distiller to heat seawater in the seawater, the carbon dioxide after heat release is expanded by the carbon dioxide expander unit and then converts energy into mechanical energy to form a low-temperature and low-pressure carbon dioxide gas-liquid mixture, and finally the carbon dioxide gas-liquid mixture is introduced into the cold side of the evaporator and then is changed into carbon dioxide superheated gas again to complete carbon dioxide working medium circulation; in the heat storage and heat pump desalination mode, the fresh seawater introduced into the low-temperature side of the heat transfer oil-seawater heat exchanger is heated to 40 ℃ and then is respectively conveyed into the first-effect seawater distiller and the second-effect seawater distiller, and the fresh seawater and the concentrated brine generated by the second-effect seawater distiller are directly mixed in the seawater brine three-way mixing valve and then are introduced into the hot side of the carbon dioxide evaporator to serve as a heat source of the carbon dioxide evaporator.
12. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein when solar energy is sufficient but electric energy is insufficient, the heat release and heat pump desalination mode is started, at this time, a main path valve of the solar collector is closed, a bypass valve is opened, high-temperature molten salt in the high-temperature molten salt storage tank flows into a molten salt heat exchange side of the molten salt-heat conduction oil heat exchanger, heat conduction oil in the heat conduction oil circulation loop is heated, the temperature is reduced, and then the high-temperature molten salt flows into the low-temperature molten salt storage tank, and at this time, the working processes of the trans-critical carbon dioxide heat pump unit and the seawater desalination unit are the same as those in the heat storage and heat pump desalination mode.
13. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein when solar energy is sufficient, the heat storage and flash evaporation desalination mode is started, and at the moment, the working process of the solar heat collection and storage unit is the same as that in the heat storage and heat pump desalination mode; at the moment, the transcritical carbon dioxide heat pump unit stops working, new seawater completely flows into the low-temperature side of the condenser under the action of the seawater shunt three-way regulating valve, and flows into the low-temperature side of the heat conduction oil-seawater heat exchanger after being preheated by condensate gas to be heated to the flash evaporation temperature; the pressure regulating valve at the top of the first-effect seawater distiller is closed, the pressure regulating valve at the top of the second-effect seawater distiller is opened, new seawater in the second-effect seawater distiller is introduced into the second-effect seawater distiller, the pressure is reduced to flash evaporation pressure under the action of the pressure regulating valve, flash evaporation is completed in the second-effect seawater distiller, steam after flash evaporation flows into the condenser and is condensed on the high-temperature side, and strong brine generated in the second-effect seawater distiller is directly discharged.
14. The seawater source trans-critical carbon dioxide heat pump cycle multi-effect seawater desalination system of claim 1, wherein when solar energy is insufficient and electric energy is insufficient, the heat release and flash desalination mode is started, at the same time, a main path valve of the solar collector is closed, a bypass valve is opened, high-temperature molten salt in the high-temperature molten salt storage tank flows into a molten salt heat exchange side of the molten salt-heat conduction oil heat exchanger, heat conduction oil in a heat conduction oil circulation loop is heated, the temperature is reduced, and then the high-temperature molten salt flows into a low-temperature molten salt storage tank, and at the same time, the working process of the seawater desalination unit is the same as that in the heat storage and flash desalination mode.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910921503.5A CN110697821B (en) | 2019-09-27 | 2019-09-27 | Seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910921503.5A CN110697821B (en) | 2019-09-27 | 2019-09-27 | Seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110697821A CN110697821A (en) | 2020-01-17 |
| CN110697821B true CN110697821B (en) | 2021-10-26 |
Family
ID=69198162
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910921503.5A Active CN110697821B (en) | 2019-09-27 | 2019-09-27 | Seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110697821B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115010200B (en) * | 2022-08-10 | 2022-10-21 | 山东天瑞重工有限公司 | System for utilize sea water source heat pump to carry out sea water desalination |
| CN116565962B (en) * | 2023-07-11 | 2023-10-31 | 国网天津市电力公司电力科学研究院 | Wind-solar heat storage integrated system and wide-load peak shaving operation method |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1724395A (en) * | 2005-04-11 | 2006-01-25 | 国家海洋局天津海水淡化与综合利用研究所 | Apparatus of combined solar energy heat pump for desaltination of sea water |
| CA2688610A1 (en) * | 2009-04-22 | 2010-10-22 | Hte Water Corporation | System and process for converting non-fresh water to fresh water or steam |
| CN101955238A (en) * | 2010-10-08 | 2011-01-26 | 河北工业大学 | Seawater desalting method and device |
| CN103670522A (en) * | 2012-09-18 | 2014-03-26 | 株式会社神户制钢所 | System combining power generation apparatus and desalination apparatus |
| WO2015004300A1 (en) * | 2013-07-09 | 2015-01-15 | Green Sea Bio System, S.L. | Installation for obtaining biomass by means of the culture of algae and obtaining a biorefined product for the production of bio-oil and bioproducts and a method for obtaining same |
| CN105923674A (en) * | 2016-06-07 | 2016-09-07 | 重庆大学 | Dual-heat-source seawater desalination system driven by supercritical CO2 heat pump |
| CN106673097A (en) * | 2017-02-15 | 2017-05-17 | 上海交通大学 | Seawater desalting plant for solar coupled heat pump |
| CN108128831A (en) * | 2018-01-16 | 2018-06-08 | 大连海洋大学 | Solar heat pump desalination plant |
| CN108425709A (en) * | 2018-02-05 | 2018-08-21 | 西安交通大学 | A kind of carbon dioxide low temperature Rankine cycle electricity generation system |
| CN109340066A (en) * | 2018-10-16 | 2019-02-15 | 中国科学院工程热物理研究所 | A kind of supercritical carbon dioxide solar power generation energy storage integrated system |
| CN110230523A (en) * | 2019-07-01 | 2019-09-13 | 西安热工研究院有限公司 | A kind of supercritical CO 2 electricity generation system and method coupling sea water desalination |
-
2019
- 2019-09-27 CN CN201910921503.5A patent/CN110697821B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1724395A (en) * | 2005-04-11 | 2006-01-25 | 国家海洋局天津海水淡化与综合利用研究所 | Apparatus of combined solar energy heat pump for desaltination of sea water |
| CA2688610A1 (en) * | 2009-04-22 | 2010-10-22 | Hte Water Corporation | System and process for converting non-fresh water to fresh water or steam |
| CN101955238A (en) * | 2010-10-08 | 2011-01-26 | 河北工业大学 | Seawater desalting method and device |
| CN103670522A (en) * | 2012-09-18 | 2014-03-26 | 株式会社神户制钢所 | System combining power generation apparatus and desalination apparatus |
| WO2015004300A1 (en) * | 2013-07-09 | 2015-01-15 | Green Sea Bio System, S.L. | Installation for obtaining biomass by means of the culture of algae and obtaining a biorefined product for the production of bio-oil and bioproducts and a method for obtaining same |
| CN105923674A (en) * | 2016-06-07 | 2016-09-07 | 重庆大学 | Dual-heat-source seawater desalination system driven by supercritical CO2 heat pump |
| CN106673097A (en) * | 2017-02-15 | 2017-05-17 | 上海交通大学 | Seawater desalting plant for solar coupled heat pump |
| CN108128831A (en) * | 2018-01-16 | 2018-06-08 | 大连海洋大学 | Solar heat pump desalination plant |
| CN108425709A (en) * | 2018-02-05 | 2018-08-21 | 西安交通大学 | A kind of carbon dioxide low temperature Rankine cycle electricity generation system |
| CN109340066A (en) * | 2018-10-16 | 2019-02-15 | 中国科学院工程热物理研究所 | A kind of supercritical carbon dioxide solar power generation energy storage integrated system |
| CN110230523A (en) * | 2019-07-01 | 2019-09-13 | 西安热工研究院有限公司 | A kind of supercritical CO 2 electricity generation system and method coupling sea water desalination |
Non-Patent Citations (2)
| Title |
|---|
| 热力压缩低温多效海水淡化特点及控制技术;孙小军等;《电站辅机》;20090930;第30卷(第03期);12-15 * |
| 热法海水淡化前沿技术及其应用进展;齐春华等;《中国给水排水》;20151217;第31卷(第24期);34-38 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110697821A (en) | 2020-01-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105923676B (en) | High-efficiency solar sea water desalination and air conditioner refrigerating cooperation method and system | |
| WO2022037711A1 (en) | Flexible power station employing supercritical carbon dioxide power cycle in combination with seawater desalination and an adjustment method thereof | |
| CN103411347A (en) | Coupling type heat pump waste heat recovery system | |
| CN102320674A (en) | Marine cold and heat cogeneration seawater desalting method and equipment | |
| CN110697821B (en) | Seawater source trans-critical carbon dioxide heat pump circulation multi-effect seawater desalination system | |
| KR20090105608A (en) | The way recovery and use heat of waste water of sludge in fire-extinguishing tank of the sewage disposal plant and heat of squeezed water in sludge | |
| CN105649901B (en) | A kind of solar energy light gathering and heat collecting power generator based on absorption heat pump | |
| CN208312760U (en) | Three combined production device of solar refrigeration supplying hot water and fresh water | |
| CN203730205U (en) | Two-stage permeation concentration difference working device driven by low-grade heat source | |
| CN103090582B (en) | The absorption energy storage equipment of a kind of boosting type three-phase | |
| CN210505692U (en) | Distributed tower type solar-driven supercritical carbon dioxide seawater desalination system | |
| CN110526318B (en) | Comprehensive utilization method and system for energy of smoke whitening coupling sea water desalination | |
| CN110529212B (en) | Cold electric fresh water co-production system based on LNG cold energy utilization | |
| CN116294425A (en) | Blast furnace slag flushing water and exhaust steam waste heat recovery cold and hot combined supply system | |
| CN110542241A (en) | Single-double effect composite evaporation-absorption two-section steam type first-class lithium bromide absorption heat pump unit | |
| CN108002623B (en) | Marine energy supply system of hot film coupling | |
| CN215809427U (en) | Ocean temperature difference energy cold, heat and electricity and fresh water poly-generation system based on solar energy assistance | |
| CN203190713U (en) | Pressurization type three-phase absorption energy storage device | |
| CN205316748U (en) | Compound heat pump hydrothermal coproduction device | |
| CN103726975A (en) | Low-grade heat source driven and two-stage infiltration adopted concentration difference working device and method | |
| CN103807947A (en) | Forward osmosis regeneration device of heat source tower antifreeze solution | |
| CN211204490U (en) | Single-double effect composite evaporation-absorption two-section steam type first-class lithium bromide absorption heat pump unit | |
| CN212425487U (en) | MED seawater desalination system using absorption heat pump coupled evaporator | |
| CN211233441U (en) | Single-effect and double-effect composite steam type first-type lithium bromide absorption heat pump unit | |
| CN103542592A (en) | Direct combustion type lithium bromide absorption cold and hot water unit with heat recycling function |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |