WO2014101580A1 - 一种太阳能连续供热的海水淡化装置及方法 - Google Patents

一种太阳能连续供热的海水淡化装置及方法 Download PDF

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Publication number
WO2014101580A1
WO2014101580A1 PCT/CN2013/087184 CN2013087184W WO2014101580A1 WO 2014101580 A1 WO2014101580 A1 WO 2014101580A1 CN 2013087184 W CN2013087184 W CN 2013087184W WO 2014101580 A1 WO2014101580 A1 WO 2014101580A1
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Prior art keywords
seawater
heat
flasher
fresh water
outlet
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PCT/CN2013/087184
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English (en)
French (fr)
Inventor
陈义龙
杨清萍
张岩丰
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中盈长江国际新能源投资有限公司
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Priority to DK13867204.3T priority Critical patent/DK2939981T3/en
Application filed by 中盈长江国际新能源投资有限公司 filed Critical 中盈长江国际新能源投资有限公司
Priority to SG11201504977YA priority patent/SG11201504977YA/en
Priority to CA2896316A priority patent/CA2896316A1/en
Priority to EP13867204.3A priority patent/EP2939981B1/en
Priority to JP2015548164A priority patent/JP6154023B2/ja
Priority to SI201331013T priority patent/SI2939981T1/en
Priority to RU2015130676/05A priority patent/RU2603799C1/ru
Priority to AU2013370015A priority patent/AU2013370015B2/en
Priority to KR1020157019810A priority patent/KR20150099590A/ko
Priority to LTEP13867204.3T priority patent/LT2939981T/lt
Publication of WO2014101580A1 publication Critical patent/WO2014101580A1/zh
Priority to US14/749,672 priority patent/US20150291463A1/en
Priority to HRP20180683TT priority patent/HRP20180683T1/hr

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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
    • C02F1/14—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
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B01D1/0029—Use of radiation
    • B01D1/0035—Solar energy
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/26—Multiple-effect evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B01D3/065—Multiple-effect flash distillation (more than two traps)
    • 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
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • 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
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • 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
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • 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
    • C02F1/50—Treatment of water, waste water, or sewage by addition or application of a germicide or by oligodynamic treatment
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/02—Temperature
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/04—Disinfection
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2307/00—Location of water treatment or water treatment device
    • 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
    • Y02A20/131—Reverse-osmosis
    • 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
    • Y02A20/211—Solar-powered water purification
    • 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
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the invention relates to a seawater desalination device and a method for continuously heating solar energy, belonging to the technical field of seawater desalination (including inland brackish water desalination).
  • the invention can also be used in the field of sewage treatment.
  • the remote water diversion project In addition to the huge investment, the remote water diversion project also requires a large amount of cultivated land, and there are also environmental hazards in the water diversion area.
  • the Yellow River Jiqing (Island) project covers an area of 62,000 mu, which will cause ecological and environmental problems such as the Yellow River's cutoff and vegetation destruction, and the destruction of the ecological environment is economically difficult to estimate.
  • the technical problem to be solved by the present invention is:
  • the invention provides a seawater desalination device and method for continuously heating solar energy, which can produce fresh water continuously and environmentally in the coastal areas and inland brackish water areas, and solve the problem of shortage of fresh water in the area.
  • the technical solution adopted by the present invention is:
  • a seawater desalination device for continuously heating solar energy comprising a seawater purification system and a seawater desalination system; characterized in that: the seawater desalination system mainly comprises a solar concentrating heat collecting device, a solar thermal storage tank, a net seawater heater and at least The first-stage seawater flasher and the seawater flasher are mainly composed of a flasher body and a seawater cooler; wherein the heat-conducting medium cavity of the solar concentrating heat collecting device and the solar heat storage tank, and the heat-conducting medium heat exchanger in the net seawater heater The closed closed communication constitutes a heat transfer medium circulation path; the total net seawater outlet of the seawater purification system is connected with the net seawater heater and the seawater cooler respectively; the seawater outlet of the net seawater heater is connected with the flasher body; the flasher body is provided with a brine outlet Fresh water outlet and steam outlet.
  • the steam outlet is collected in the fresh water main pipe together with the fresh water outlet through the steam heat exchanger in the sea water cooler.
  • the closed fresh water storage tank at the end of the fresh water main pipe is connected with the vacuum pump.
  • the concentrated brine outlet and the salt production plant pipeline Connected; the seawater outlet of the seawater cooler passes through the body condenser in the body of the flasher.
  • the seawater heater is connected; when there is at least two-stage seawater flasher, the concentrated brine outlet of the front-stage flasher body is connected with the lower-stage flasher body, and the concentrated brine outlet of the last-stage flasher body is connected with the salt-making plant pipeline;
  • the pressure in the body of the steamer is gradually reduced to form a negative pressure.
  • a hot sea water pump with adjustable rotational speed is arranged between the seawater outlet of the net seawater heater and the body of the flasher, and the seawater outlet of the clean seawater heater is connected to the throttling device on the body of the flasher through the hot sea water pump.
  • the flow device is located above the liquid surface; inside the flasher body, a defoamer is arranged above the throttling device, a fresh water storage tray is arranged above the defoamer, a bulk condenser is arranged on the fresh water storage tray; the steam outlet is located at the top of the flasher body, and the fresh water outlet Located above the freshwater storage tray, the brine outlet is located below the throttling device.
  • a seawater temperature sensor and a backup heat exchanger are further disposed in the clean seawater heater, and the heat source of the standby heat exchanger is a hot oil furnace, an electric heating furnace, a boiler flue gas waste heat, or a steam engine residual steam heat.
  • a hydrothermal pump is disposed between the solar heat storage tank and the heat exchanger in the clean sea water heater.
  • the solar concentrating heat collecting device is a tower type solar collector, or a parabolic trough type vacuum tube collector, or an all glass vacuum tube collector, or a heat pipe type vacuum tube collector.
  • the seawater purification system is a multi-stage purification system, which sequentially includes a crude seawater extraction well, a seawater sterilization clarifier, a multi-stage ultrafiltration tank equipped with an activated carbon filter layer and a multi-fiber filter layer.
  • a seawater deoxygenation decarbonization tower for deoxygenation and decarbonization; a clean sea pool between the multistage ultrafiltration tank and the seawater oxygen removal and decarbonization tower;
  • the seawater deoxygenation decarbonization tower is connected with the total clean seawater outlet;
  • the extracted seawater well is connected to the seawater sterilization clarifier through the seawater lift pump, and the seawater sterilization clarifier is connected to the multistage ultrafiltration tank through a seawater transfer pump, multi-stage super
  • the filter tank is connected to the clean sea pool through another seawater transfer pump.
  • the clean sea water tank is connected to the seawater oxygen removal and decarbonization tower through the third sea water pump, and the seawater oxygen removal and decarbonization tower is connected to the total clean sea water outlet through the clean sea water pump;
  • a sterilizing agent and a flocculating agent are added to the sterilization clarifier.
  • the extraction seawater well is built on the beach, the wellhead is located above the highest tide line of the seawater, and the bottom of the well is located several meters below the sea level at low tide; the well wall adopts a porous concrete structure, and the outside of the well wall is gravel and gravel Filled with sand from the beach.
  • the seawater desalination method adopting the above seawater desalination device is characterized in that seawater is purified into a clean seawater through multi-stage purification; the solar concentrating heat collecting device collects sunlight to heat the heat conductive medium, converts the solar energy into heat energy of the heat conduction medium, and heat energy through the heat conduction medium Continuously heating the purified clean seawater to a set temperature, and then heating the heated clean seawater to at least one flash evaporator for flashing.
  • the pressure in the flasher body is gradually decreased step by step. Forming a negative pressure; the steam after flashing separates fresh water by condensation, and some of the steam that has not once condensed becomes fresh water after being exchanged by the seawater cooler;
  • the concentrated brine at the bottom of the flasher flows into the subsequent secondary flashers in sequence, and then condenses and separates the fresh water during the flashing process.
  • the concentrated brine without gasification is finally sent to the salt production plant; the solar concentrating collector collects the solar thermal energy and uses the heat transfer medium to heat the clean sea water while storing the heat transfer medium heat energy in the solar heat storage tank at night or overcast.
  • the seawater is continuously heated by the stored heat transfer medium.
  • the heat transfer medium sets the set temperature of the clean sea water to 55 ° C to 70 ° C or 70 ° C to 120 ° C, and the solar heat collector heats the heat transfer medium to 178 ° C to 600 ° C.
  • the heat transfer medium sets the set temperature of the clean sea water to ⁇ 70 ° C, and the solar heat collector heats the heat transfer medium to 275 ° C to 395 ° C.
  • the invention adopts a high-efficiency solar heat collector to heat a heat-conducting medium (such as heat-conducting oil, silicone oil, paraffin, molten salt), and then uses a heat-conducting medium to heat the clean seawater to a set temperature, thereby avoiding the device for directly heating the seawater by the solar heat collector.
  • a heat-conducting medium such as heat-conducting oil, silicone oil, paraffin, molten salt
  • fresh water plants need 24 hours of uninterrupted supply of fresh water.
  • solar thermal energy By storing solar thermal energy through a heat-conducting medium, it is possible to heat sea water at night and continuously produce fresh water.
  • the role of solar thermal storage tanks is set; one is to maintain the stability of solar heat output for cloudy weather at night, and the second is to provide 24-hour uninterrupted water supply for fresh water supply centers, both for civilian and industrial use.
  • the role of thermal storage tanks is to More storage of solar energy during the day is used for night use.
  • the extracted seawater well is built above the highest tide line of the sea on the beach.
  • the depth of the well is several meters below the sea level at low tide.
  • the diameter of the well should be sufficient to extract the amount of seawater. This allows the seawater in the well to be preliminarily filtered by the sand of the beach, which excludes most of the marine life and impurities.
  • the beach is washed away by the rising tide and the tidal water. The beach can naturally be cleaned every day. Filtering ability.
  • the method of drilling wells on the beach the well wall can be made of porous concrete structure, the outside of the well wall is gravel, and the gravel is filled with sand from the beach.
  • the clean seawater in the deaerator and decarbonization tower driven by the seawater transfer pump needs to further remove oxygen and CO 2 gas. Since the seawater contains about 3.5% of salt, it is highly corrosive. The oxygen and CO 2 gas contained in the sea water will accelerate the corrosion of the equipment and must be removed as much as possible.
  • the net seawater heater is composed of a heater vessel, a heat medium heat exchanger provided in the vessel, and a spare heat medium heat exchanger.
  • the heat medium heat exchanger is arranged to heat the seawater to a certain temperature (for this purpose, a seawater temperature sensor is set in the clean seawater heater for measuring the temperature of the heated seawater), but if there is no sunlight in the rainy day,
  • the 24-hour uninterrupted water supply at the freshwater supply center will be challenged, so that a spare heat exchanger is also installed in the clean seawater heater, and various auxiliary heat sources (such as hot oil furnaces, electric heating furnaces, etc.) can be used in the continuous rainy season.
  • Boiler flue gas waste heat, steam engine exhaust steam, etc. to heat the seawater, so that fresh water can be produced continuously.
  • the flasher consists of a flasher body and a seawater cooler.
  • a throttle device, a defoamer, a fresh water storage tray, and a body condenser are disposed in the body of the flasher from bottom to top.
  • the throttling device provided by the flasher body causes the hot seawater to enter the flasher to have a sudden pressure drop, a large amount of seawater vaporizes, and the steam rises, wherein the entrained larger seawater droplets encounter the defoamer (the desiccator is made of a mesh with a fine mesh) Made of 200 mesh, or 300 mesh, or 400 mesh wire mesh, made of corrosion-resistant materials, such as stainless steel wire, or titanium alloy wire, or carbon fiber wire...) blocked by the steam of the defoamer
  • the bulk condenser a part of which is condensed into fresh water, falls into the fresh water storage tank, and is sent to the fresh water tank. A part of the steam enters the seawater cooler from the top of the flasher,
  • the multi-stage flasher is composed of N identical single-stage flashers, N is a positive integer, and the fresh water output pipe of each single-stage flasher is connected through the fresh water master pipe to the closed fresh water storage tank, and the vacuum pump inlet pipe connection At the top of the water storage tank, when the vacuum pump is running, the pressure in each flash evaporator can be gradually reduced to form a negative pressure, which makes the hot sea water easily vaporize to form steam in each stage of the flasher, and releases latent heat when cold, and condenses into fresh water. .
  • the concentrated seawater at the bottom of the flasher can also be gradually reduced in temperature and flowed into each secondary flasher to be flashed, and then condensed into fresh water, while the concentrated salt water without vaporization is finally sent to the salt production plant.
  • FIG. 1 is a schematic view showing the structure of a seawater desalination apparatus for solar continuous heating according to the present invention.
  • FIG. 2 is a schematic view showing the local structure of a seawater extraction well of the present invention.
  • 1 is a solar heat collecting field
  • 1a is a diversion mother tube of a solar heat collecting field
  • a heat conducting medium is inside the mother tube
  • 2 is a solar heat storage tank
  • 2a is a hydrothermal pump
  • 3 is a sea water heater
  • 3b is Heat transfer medium heat exchanger
  • 3c is a backup heat exchanger
  • 3a is a hot sea water pump with adjustable speed
  • T3e is a temperature sensor set in seawater heater
  • the farthest stage on the far right is a 9-stage flasher
  • 4a is a throttling device, installed at the bottom of the flasher
  • 4b is a defoamer
  • 4c is a fresh water storage tray
  • 4d is a bulk condenser
  • 4e is a seawater cooler.
  • the steam heat exchangers 4f, 5 are arranged in a sealed fresh water storage tank, and the top of the tank is connected with a vacuum pump 5a through a pipeline
  • 5b is a brine pump installed on the brine outlet pipe of the final stage flasher
  • 6 is a seawater sterilization clarifier.
  • 6a is an extraction seawater well built on the highest tidal line on the beach.
  • the depth of the well is several meters below the sea level at low tide.
  • the diameter of the well is moderate (satisfying the amount of seawater pumped)
  • 6b is the seawater lift pump
  • 6d is the clean seawater.
  • Inlet switch valve 6e is the sewage valve of seawater sterilizing clarifier 6 (open 6d, 6e can input clean seawater for flushing sediment at bottom 6, 6e outlet pipe leading to sewage treatment plant)
  • 7 is multi-stage ultrafiltration tank
  • 7b is activated carbon filter layer
  • 7c is multi-fiber filter core layer
  • 7d is backwashing clean seawater input switch valve
  • 7e is backwashing drain valve (regularly open 7d, 7e can input clean seawater for flushing 7 filter layers) , to restore the clean filter function of each filter layer)
  • 8 is a clean sea pool
  • 9 is an oxygen removal decarbonization tower
  • 7a, 8a is a seawater transfer pump
  • 9a is a clean sea water pump.
  • 6b is a seawater lift pump, and 6a is a seawater extraction well.
  • 6a1 is a seaside beach
  • 6a2 is the highest tide line of sea water
  • 6a3 is the lowest sea level line of sea water
  • 6a4 is a porous concrete shaft wall with holes
  • 6a5 is gravel
  • 6a6 is bottom sand
  • bottom sand will be with time Gradually pile up, need to be cleaned out of the well regularly.
  • the utility model is composed of a seawater purification system and a seawater desalination system; the seawater desalination system mainly comprises a solar concentrating heat collecting device, a solar thermal storage tank 2, a clean seawater heater 3, and at least a first-stage seawater flasher, and the seawater flashing
  • the steamer is mainly composed of a flasher body 4 and a seawater cooler 4e; wherein, the heat transfer medium chamber of the solar concentrating heat collecting device 1 and the solar heat storage tank 2, and the heat transfer medium heat exchanger 3b in the clean sea water heater 3 are sequentially
  • the closed communication constitutes a heat transfer medium circulation path;
  • the clean seawater outlet mother pipe of the clean seawater transfer pump 9a in the seawater purification system is connected to the inlet of the clean seawater heater 3 and the seawater cooler 4e respectively; the seawater outlet of the clean seawater heater 3 passes through the hot seawater
  • the pump 3a is in communication with the inlet
  • the outlets are collected together in the fresh water main pipe, and the closed fresh water storage tank 5 at the end of the fresh water main pipe is connected with the vacuum pump 5a, and the concentrated brine outlet is connected to the salt plant pipeline through the concentrated brine pump 5b.
  • the seawater outlet of the seawater cooler 4e is connected to the input mother pipe of the seawater heater 3 through the body condenser 4d in the flasher body 4; when there is at least two-stage seawater flasher, the seawater removal pump 9a of the seawater purification system
  • the net seawater outlet mother pipe is respectively connected with the seawater outlets of the body condensers 4d of the respective flashers; the brine outlet of the front stage flasher body 4 is connected to the inlet of the throttle device 4a of the lower flasher body 4, and the final stage flasher body
  • the concentrated brine outlet of 4 is connected to the salt making pipeline through the concentrated brine pump 5b; the pressure in the flasher body 4 of each stage is gradually reduced to form a negative pressure.
  • the seawater purification system is a multi-stage purification system, which includes, in order, a coarse filtration extraction seawater well 6a, a seawater sterilization clarification tank 6, a multi-stage ultrafiltration tank equipped with an activated carbon filter layer and a multi-fiber filter layer, and a seawater deaerator decarbonization tower 9 for deoxygenation and decarbonization; a clean sea pool 8 between the multistage ultrafiltration tank 7 and the seawater oxygen removal and decarbonization tower 9;
  • the seawater deoxygenation decarbonization tower 9 is connected to the total clean seawater outlet;
  • the extracted seawater well 6a is connected to the seawater sterilization clarifier 6 through the seawater lift pump 6b, and the seawater sterilization clarifier 6 is passed through a seawater transfer pump 7a and multistage ultrafiltration
  • the pool 7 is connected, and the multistage ultrafiltration tank 7 is connected to the clean sea water tank 8 through another seawater transfer pump 8a.
  • the clean sea water tank 8 is connected to the seawater oxygen removal and decarbonization tower 9 through the third sea water pump 8a, and the seawater is deaerated and decarbonized.
  • the tower 9 is connected to the total clean seawater outlet through the clean sea water pump 9a; the seawater sterilization clarifier 6 is filled with a sterilizing agent and a flocculating agent.
  • the seawater desalination method adopting the above seawater desalination device is characterized in that seawater is purified into a clean seawater through multi-stage purification; the solar concentrating heat collecting device collects sunlight to heat the heat conductive medium, converts the solar energy into heat energy of the heat conduction medium, and heat energy through the heat conduction medium Continuously heating the purified clean seawater to a set temperature, and then heating the heated clean seawater to at least one flash evaporator for flashing.
  • the pressure in the flasher body is gradually decreased step by step. Forming a negative pressure; the steam after flashing separates fresh water by condensation, and some of the steam that has not once condensed becomes fresh water after being exchanged by the seawater cooler;
  • the concentrated brine at the bottom of the flasher flows into the subsequent secondary flashers in sequence, and then condenses and separates the fresh water during the flashing process.
  • the concentrated brine without gasification is finally sent to the salt production plant; the solar concentrating collector collects the solar thermal energy and uses the heat transfer medium to heat the clean sea water while storing the heat transfer medium heat energy in the solar heat storage tank at night or overcast.
  • the seawater is continuously heated by the stored heat transfer medium.
  • the heat transfer medium sets the set temperature of the clean sea water to 55 ° C to 70 ° C or 70 ° C to 120 ° C, and the solar heat collector heats the heat transfer medium to 178 ° C to 600 ° C.
  • the heat transfer medium sets the set temperature of the clean sea water to ⁇ 70 ° C, and the solar heat collector heats the heat transfer medium to 275 ° C to 395 ° C.
  • the seawater lifting pump 6b is first started, and the seawater is extracted from the extracted seawater well 6a and injected into the seawater sterilization clarification tank 6, since the seawater well 6a is built on the highest tide line on the beach. Above the 6a2, the well depth is lower than the sea level 6a3 at the lowest tide, which makes the seawater in the well have been initially natural filtered by the sand of the beach, eliminating most of the marine life and impurities, and the beach is rising every day, The tidal waters are washed away, and the beach can naturally maintain a certain degree of clean filtration capacity every day.
  • the method of drilling wells on the beach: the borehole wall may adopt a porous concrete structure 6a4 with a hole, the outside of the well wall is a gravel 6a5, and the gravel is filled with sand grains of the beach to fill the structure.
  • the multi-stage ultrafiltration tank 7 is input into the multi-stage ultrafiltration tank 7 through the transfer pump 7a, and is purified by multi-stage ultrafiltration to be stored in the clean sea water tank 8 for use.
  • the sediment at the bottom of the sterilizing clarifier 6 (below the inlet of 7a) is cleaned regularly (using a small amount of clean sea water) and discharged to a sewage treatment plant.
  • the multi-stage ultrafiltration tank 7 also needs to periodically use clean sea water for backwashing to restore the clean filtration capacity of each filter layer.
  • the clean seawater in the deaerator decarbonization tower 9 driven by the 8a seawater pump needs to further remove oxygen and CO 2 gas. Because the seawater contains about 3.5% of salt, it is highly corrosive. The oxygen and CO 2 gas contained in the sea water will accelerate the corrosion of the equipment and must be removed as much as possible.
  • the solar heat collecting field 1 collects the heat energy of the sunlight into the heat medium in 1a, and stores the heat energy in the heat storage tank 2 through the heat medium, and the heat pump 2a drives the heat medium to flow from 2 to the seawater heater 3
  • the temperature of the clean seawater is increased (usually 55 ° C to 120 ° C), and the embodiment is set to 70 ° C, and the hot sea water is driven by the adjustable speed sea water pump 3a.
  • the speed of the hot sea water pump 3a is adjusted to control the flow rate of the seawater sent to the first-stage flasher 4, thereby controlling the level of the seawater level of 4
  • the pressure suddenly drops, the water in the hot sea water vaporizes a lot, and the steam rises.
  • the large sea water droplets entrained in the steam are blocked by the defoamer, falling into the bottom of the flasher, and the steam rises to the top of the flasher.
  • the concentrated brine enters the Class 2 flasher and repeats the whole process of 4a to 4f to produce fresh water.
  • the final stage of this embodiment is a 9-stage flasher.
  • the concentrated brine of the final stage flasher is finally driven by the brine pump 5b to the salt processing plant for further processing and utilization.
  • the seawater entering the first-stage flasher undergoes a 9-stage distillation process, and about 40% of it is vaporized and condensed and converted into fresh water.
  • the seawater desalination is not heated. The higher the sea temperature, the better.
  • the salt in the seawater sodium ions and calcium, magnesium ions
  • the preferred temperature parameter for seawater desalination to avoid fouling in the present embodiment should be about 70 ° C or ⁇ 70 ° C, and of course, in other temperatures ranging from 55 ° C to 70 ° C and 70 ° C to 120 ° C.
  • the seawater desalination of the invention is only better than the comprehensive efficiency of ⁇ 70 °C.
  • the invention has the advantages that the optimal temperature parameter (the optimal operating parameter of the current solar concentrating heat collecting field) is 275 ° C to 395 ° C (with heat conducting oil as medium) or 178 ° C due to the high efficiency operation of the solar heat collector. ⁇ 610 ° C (using molten salt as medium), for this reason, the invention uses a high-efficiency solar heat collector to heat the heat-conducting medium (such as heat-conducting oil, silicone oil, paraffin, molten salt) to meet the temperature operating parameters of the above-mentioned solar heat collector, and then Using a heat-conducting medium to heat seawater to about 70 °C can avoid the scaling problem of the solar water heater directly heating the seawater, so that the seawater flash desalination equipment can operate at the optimal temperature parameter and the solar heat collecting equipment can operate at the best. Parameters to maximize the benefits of collecting solar heat.
  • the optimal temperature parameter is 275 ° C to 395 ° C (with heat conducting oil as medium) or 178 ° C
  • heat-conducting media such as heat-conducting oil, silicone oil, paraffin, and molten salt
  • the high-efficiency solar concentrating heat collecting device since the high-efficiency solar concentrating heat collecting device is adopted, the relatively dispersed solar energy can be efficiently collected, the heating and evaporation of seawater can be completed, the seawater desalination rate is up to 40%, and the solar energy can be stored. Continuous operation of fresh water at night without sunlight, producing fresh water with good quality and meeting drinking water standards. Moreover, the main use of clean energy solar energy, the desalination process is environmentally friendly, efficient, and large in output.

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Abstract

一种太阳能连续供热的海水淡化装置，包括海水净化系统、海水除盐系统；海水净化系统是由抽提海水井（6a）、海水灭菌澄清池（6）、多级超滤池（7）、净海水池（8）组成的。海水除盐系统是由太阳能聚光集热装置（1）、太阳能蓄热罐（2）、净海水加热器（3）及海水多级闪蒸器组成的。太阳能聚光集热装置（1）通过导热工质白天收集太阳光热能，存储于太阳能蓄热罐（2）内，再用导热工质来加热净海水到一定温度，热海水输往多级闪蒸器，逐级喷蒸，分离出淡水及盐卤水。还公开了一种太阳能连续供热的海水淡化方法。太阳能持续供热的海水淡化装置可高效收集相对分散的太阳能对海水加热蒸发，产出淡水品质达到饮用水标准，存储太阳能可连续运转生产淡水。

Description

一种太阳能连续供热的海水淡化装置及方法 技术领域
本发明涉及一种太阳能连续供热的海水淡化装置及方法，属于海水淡化（含内陆苦咸水淡化）技术领域。该发明还可用于污水处理领域。
背景技术
随着我国经济的高速发展在东南沿海经济比较发达地区，淡水资源紧缺问题突显，北京、上海、天津、青岛等地因过度抽采地下水已发生地面沉降问题。为此从80年代开始，国家先后开展了引滦入津、引黄济青、南水北调等远程调水工程。
远程引水工程，除了巨额的投资之外，还要占用大量耕地，还存在被引水地区的环境危害等问题。如引黄济青（岛）工程，占地达6.2万亩，还会造成黄河断流、植被破坏等生态环境问题，而生态环境的破坏在经济上是难以估量的。
一些沿海城市诸如青岛、海口、陵水等，城市的形成源于其靠近淡水河，但由于海潮的漲落，台风的光临，海水往往浸入河口内约30-50公里，海边城市旁的淡水河内实质是稀释海水，是质量打折扣的淡水。
21世纪，除去能源危机，CO2减排的环保压力，还会有淡水资源匮乏的危机，以科学、环保的方法掌握更多淡水资源意味着国民经济的可持续发展，也意味着国民的生活富裕程度。
长期以来，利用各种热能对海水加热，产生蒸汽，再使蒸汽冷凝为淡水，一直是海岛、沿海岸居民，乃至远洋船舶获取淡水的重要方法。太阳能具有分布广泛、储量无限、收集利用清洁、CO2零排放，属可再生能源的优点也引起人们广泛关注；但其分散，受天气影响较大，能量汇集不稳定、不连续等，又在利用上存在种种问题。
因此寻找技术途径，高效地收集太阳能热并昼夜连续运行来进行海水淡化，就成为解决淡水资源匮乏的有效方法。
 技术问题
本发明要解决的技术问题是： 提供一种太阳能连续供热的海水淡化装置及方法，能够在沿海地区、内陆苦咸水地区，昼夜不间断地、更环保地生产淡水，解决该地区的淡水匮乏问题。
技术解决方案
为解决上述技术问题，本发明所采用的技术方案是：
一种太阳能连续供热的海水淡化装置，由海水净化系统、海水除盐系统组成；其特征在于：海水除盐系统主要包括太阳能聚光集热装置、太阳能蓄热罐、净海水加热器以及至少一级海水闪蒸器，海水闪蒸器主要由闪蒸器本体与海水冷却器构成；其中，太阳能聚光集热装置的导热介质腔与太阳能蓄热罐、以及净海水加热器中的导热介质换热器顺次封闭连通构成导热介质循环路径；海水净化系统的总净海水出口与净海水加热器和海水冷却器分别连通；净海水加热器的海水出口与闪蒸器本体连通；闪蒸器本体设置浓盐水出口、淡水出口和蒸汽出口，蒸汽出口经海水冷却器中的蒸汽换热器后同淡水出口一同汇集于淡水总管，淡水总管末端的密闭式淡水储罐与真空泵连通，浓盐水出口与制盐厂管道连通；海水冷却器的海水出口经闪蒸器本体中的本体冷凝器后与海水加热器连通；存在至少两级海水闪蒸器时，前级闪蒸器本体的浓盐水出口与下级闪蒸器本体连通，最后一级闪蒸器本体的浓盐水出口与制盐厂管道连通；各级闪蒸器本体内压力依次逐级降低形成负压。
按上述技术方案，在净海水加热器海水出口与闪蒸器本体之间设置转速可调的热海水泵，净海水加热器海水出口经热海水泵后与闪蒸器本体上的节流装置连通，节流装置位于液面之上；闪蒸器本体内部，节流装置上方设置消沫器，消沫器上方设置淡水储盘，淡水储盘上设置本体冷凝器；蒸汽出口位于闪蒸器本体顶部，淡水出口位于淡水储盘之上，浓盐水出口位于节流装置之下。
按上述技术方案，净海水加热器内还设置海水温度传感器和备用换热器，所述备用换热器的热源为热油炉、电加热炉、锅炉烟气余热、或汽机乏汽余热。
按上述技术方案，在太阳能蓄热罐和净海水加热器中的换热器间设置热液泵。
按上述技术方案，太阳能聚光集热装置是塔式太阳能集热器、或抛物面槽式真空管集热器、或全玻璃真空管集热器、或热管式真空管集热器。
按上述技术方案，海水净化系统为多级净化系统，顺次包括进行粗过滤的抽提海水井、海水灭菌澄清池、装设有活性碳滤层和多纤维滤芯层的多级超滤池、以及用于除氧脱碳的海水除氧脱碳塔；多级超滤池与海水除氧脱碳塔之间设置净海水池； 海水除氧脱碳塔与总净海水出口连通；抽提海水井通过海水提升泵与海水灭菌澄清池连通，海水灭菌澄清池通过一个海水转运泵与多级超滤池连通，多级超滤池通过另一个海水转运泵与净海水池连通，净海水池通过第三个海水泵与海水除氧脱碳塔连通，海水除氧脱碳塔通过净海水泵与总净海水出口连通；海水灭菌澄清池中添加有灭菌剂和絮凝剂。
按上述技术方案，抽提海水井建于沙滩上，井口位于海水最高潮水线上方，井底面位于低潮时海平面下方数米；井壁采用多孔混凝土结构，井壁外为碎石，碎石外由沙滩的砂粒填充。
采用上述海水淡化装置的海水淡化方法，其特征在于：海水经过多级净化成为净海水；太阳能聚光集热装置收集太阳光对导热介质进行加热，使太阳能转化为导热介质热能，通过导热介质热能持续不断地加热净化后的净海水到设定温度，然后加热后的热净海水输往至少一级闪蒸器中进行闪蒸，闪蒸过程中，保持各级闪蒸器本体内压力依次逐级降低形成负压；闪蒸后的蒸汽经冷凝分离出淡水，部分没有一次冷凝的蒸汽经海水冷却器换热后成为淡水；
闪蒸器底部没有气化的浓盐水输往制盐厂；存在多级闪蒸器时，闪蒸器底部的浓盐水依次流入后续各次级闪蒸器中，逐级闪蒸过程中再冷凝分离出淡水，没有气化的浓盐水最终输往制盐厂；太阳能聚光集热装置收集太阳光热能且利用导热介质加热净海水的同时，还将导热介质热能储存在太阳能蓄热罐中，在夜晚或阴天时利用储存的导热介质对净海水进行持续加热。
按上述技术方案，导热介质将净海水加热的设定温度为55℃～70℃或为70℃～120℃，太阳能聚热器将导热介质加热到178℃～600℃。
按上述技术方案，导热介质将净海水加热的设定温度为±70℃，太阳能聚热器将导热介质加热到275℃～395℃。
 有益效果
本发明采用高效太阳能聚热器加热导热介质（如导热油、硅油、石腊、熔融盐），再用导热介质去加热净海水到设定温度，既可避免太阳能聚热器直接加热海水的设备结垢问题，使海水闪蒸淡化设备运行在最佳温度参数，又可使太阳能聚热设备也运行在其最佳参数（将导热介质加热到275℃～395℃，或178℃～600℃），达到收集太阳能热的效益最大化。
同时，一般淡水厂需24小时不间断供应淡水，通过导热介质存储太阳光热能，就可以使晚上也能加热海水，不间断生产淡水。
设置太阳能蓄热罐的作用；一是为了夜晚多云天气维持太阳能热的输出稳定性，其次对于淡水供应中心无论是民用还是工业用都要求24小时不间断供水，蓄热罐的作用就是为了尽可能多的存储白天的太阳能用于晚上使用。
抽提海水井建于沙滩上海水最高潮水线上方，井深低于低潮时海平面下方数米，井直径大小应满足抽取海水量即可。这使得井中的海水已经由沙滩的砂粒进行了一定的初步自然过滤，排除了大部分的海洋生物及杂质，而沙滩经每天的潮起、潮落海水冲刷，沙滩每天可自然地保持一定的清洁过滤能力。而在沙滩上打井的方法：井壁可采用多孔混凝土结构，井壁外为碎石，碎石外由沙滩的砂粒来填充构造。
在海水灭菌澄清池中添加灭菌剂（如氯气），杀灭海水中的浮游生物及微生物、菌类，再添加絮凝剂（如FeCl2，或明矾均可），使海水静置清澈，池上部的澄清液经转运泵输入多级超滤池中，经多级超滤成为净海水储存在净海水池中待用。灭菌澄清池底部（海水转运泵入口的下方）的沉渣，需定期冲洗（使用少量净海水）清理，排往污水处理厂。多级超滤池也需定期使用净海水，进行反冲洗，以恢复各级过滤层的清洁过滤能力。
海水除盐系统启动时，在海水转运泵的驱动下净海水在除氧脱碳塔中还需进一步脱除氧气及CO2气，因海水约含有3.5%的盐分，具有很强的腐蚀性，海水中含有的氧气及CO2气会加快设备的锈蚀，必需尽力脱除。
净海水加热器是由加热器容器，及容器内设置的导热介质换热器、备用导热介质换热器组成的。这其中设置导热介质换热器是为了加热海水到一定温度（为此在净海水加热器内设置了海水温度传感器，用于测量被加热的海水温度），但如果遇到连阴雨天无阳光时，淡水供应中心的24小时不间断供水将受到挑战，为此净海水加热器中还设置了备用换热器，在遇到连阴雨季时可以利用各种辅助热源（如热油炉、电加热炉、锅炉烟气余热、汽机乏汽余热等）来加热海水，使淡水不间断生产。
闪蒸器是由闪蒸器本体及海水冷却器组成的。闪蒸器本体内从下到上设置有节流装置、消沫器、淡水储盘、本体冷凝器。闪蒸器本体设置的节流装置使得热海水进入闪蒸器内压力突降，大量海水汽化，蒸汽上升，其中夹带的较大海水液滴遇到消沫器（消沫器由网眼很细的丝网作成，如200目、或300目、或400目丝网，材质为耐腐蚀材料，如：不锈钢丝、或钛合金丝、或碳纤维丝……）被栏阻，通过消沫器的蒸汽遇到本体冷凝器，一部分冷凝为淡水落在淡水储盘内，输往淡水罐，一部分蒸汽从闪蒸器顶部进入海水冷却器内，因冷海水在冷却器内喷淋到蒸汽换热器上，使蒸汽再次冷却，释放出潜热，凝结为淡水输往淡水罐。
多级闪蒸器是由N个相同的单级闪蒸器组成，N为正整数，每个单级闪蒸器的淡水输出管通过淡水母管相联，通往密闭的淡水储罐，真空泵入口管道连接储水罐顶，真空泵运转时可使各级闪蒸器内压力依次逐级降低形成负压，这使得每级闪蒸器内均可使热海水容易汽化形成蒸汽，遇冷释放出潜热，凝结为淡水。闪蒸器底部的浓海水也可依次逐级降低温度流入各次级闪蒸器中闪蒸，再凝结为淡水，而没有汽化的浓盐海水最终输往制盐厂。
 附图说明
下面结合附图和实施例来说明本发明。
图1是本发明的太阳能连续供热的海水淡化装置结构示意图。
图2是本发明的海水抽提井局部构造示意图。
图1中，1是太阳能聚热场，1a是太阳能聚热场的导流母管，母管内有导热介质，2是太阳能蓄热罐，2a是热液泵，3是海水加热器，3b是导热介质换热器，3c是备用换热器，3a是转速可调的热海水泵，T3e是设置在海水加热器中的温度传感器，4是单级闪蒸器，其中N为正整数，N=1时，闪蒸器称为1级闪蒸器，N=2时闪蒸器称为2级闪蒸器，依此类推直到N级闪蒸器，通常N=3～9，最佳实施方式中取N=9，最右侧的末级为9级闪蒸器，4a是节流装置，装于闪蒸器底部，4b是消沫器，4c是淡水储盘，4d是本体冷凝器，4e是海水冷却器，其内设置蒸汽换热器4f，5是密闭淡水储罐，罐顶通过管道联接有真空泵5a，5b是末级闪蒸器浓盐水出口管道上设置的盐水泵，6是海水灭菌澄清池， 6a是抽提海水井，其建于沙滩上最高潮水线上方，井深低于低潮时海平面下方数米，井直径适度（满足抽取海水量即可），6b是海水提升泵，6d是净海水入口开关阀，6e是海水灭菌澄清池6的排污阀（打开6d、6e可输入净海水用于冲洗6底部的沉渣，6e的出口管道通往污水处理厂），7是多级超滤池，7b是活性碳滤层，7c是多纤维滤芯层，7d是反冲洗净海水输入开关阀，7e是反冲洗排污阀（定期打开7d、7e可输入净海水用于冲洗7的各过滤层，恢复各过滤层的清洁滤污功能），8是净海水池，9是除氧脱碳塔，7a、8a是海水转运泵，9a是净海水泵。
图2中6b是海水提升泵，6a是海水抽提井， 6a1是海边沙滩，6a2是海水最高潮水线，6a3是海水最低海平面线，6a4是有孔洞的多孔混凝土井壁，6a5是碎石砾，6a6是井底海砂，井底海砂会随时间逐步堆高，需定期清理出井外。
 本发明的实施方式
图1、图2为根据本发明实施的太阳能连续供热的海水淡化装置, 由海水净化系统、海水除盐系统组成；其特征在于：海水除盐系统主要包括太阳能聚光集热装置1、太阳能蓄热罐2、净海水加热器3以及至少一级海水闪蒸器，海水闪蒸器主要由闪蒸器本体4与海水冷却器4e构成；其中，太阳能聚光集热装置1的导热介质腔与太阳能蓄热罐2、以及净海水加热器3中的导热介质换热器3b顺次封闭连通构成导热介质循环路径；海水净化系统中净海水转运泵9a的净海水出口母管与净海水加热器3的入口和海水冷却器4e分别连通；净海水加热器3的海水出口经热海水泵3a后与第1级闪蒸器本体的节流装置4a入口连通；闪蒸器本体4设置浓盐水出口、淡水出口和蒸汽出口，蒸汽出口经海水冷却器4e中的蒸汽换热器4f后同淡水出口一同汇集于淡水总管，淡水总管末端的密闭淡水储罐5与真空泵5a连通，浓盐水出口经浓盐水泵5b后与制盐厂管道连通；海水冷却器4e的海水出口经闪蒸器本体4中的本体冷凝器4d后与海水加热器3的输入母管连通；存在至少两级海水闪蒸器时，海水净化系统中净海水转运泵9a的净海水出口母管与各闪蒸器的本体冷凝器4d的海水出口分别连通；前级闪蒸器本体4的浓盐水出口与下级闪蒸器本体4的节流装置4a入口连通，最后一级闪蒸器本体4的浓盐水出口经浓盐水泵5b后与制盐厂管道连通；各级闪蒸器本体4内压力依次逐级降低形成负压。
海水净化系统为多级净化系统，顺次包括进行粗过滤的抽提海水井6a、海水灭菌澄清池6、装设有活性碳滤层和多纤维滤芯层的多级超滤池7、以及用于除氧脱碳的海水除氧脱碳塔9；多级超滤池7与海水除氧脱碳塔9之间设置净海水池8； 海水除氧脱碳塔9与总净海水出口连通；抽提海水井6a通过海水提升泵6b与海水灭菌澄清池6连通，海水灭菌澄清池6通过一个海水转运泵7a与多级超滤池7连通，多级超滤池7通过另一个海水转运泵8a与净海水池8连通，净海水池8通过第三个海水泵8a与海水除氧脱碳塔9连通，海水除氧脱碳塔9通过净海水泵9a与总净海水出口连通；海水灭菌澄清池6中添加有灭菌剂和絮凝剂。
采用上述海水淡化装置的海水淡化方法，其特征在于：海水经过多级净化成为净海水；太阳能聚光集热装置收集太阳光对导热介质进行加热，使太阳能转化为导热介质热能，通过导热介质热能持续不断地加热净化后的净海水到设定温度，然后加热后的热净海水输往至少一级闪蒸器中进行闪蒸，闪蒸过程中，保持各级闪蒸器本体内压力依次逐级降低形成负压；闪蒸后的蒸汽经冷凝分离出淡水，部分没有一次冷凝的蒸汽经海水冷却器换热后成为淡水；
闪蒸器底部没有气化的浓盐水输往制盐厂；存在多级闪蒸器时，闪蒸器底部的浓盐水依次流入后续各次级闪蒸器中，逐级闪蒸过程中再冷凝分离出淡水，没有气化的浓盐水最终输往制盐厂；太阳能聚光集热装置收集太阳光热能且利用导热介质加热净海水的同时，还将导热介质热能储存在太阳能蓄热罐中，在夜晚或阴天时利用储存的导热介质对净海水进行持续加热。
按上述技术方案，导热介质将净海水加热的设定温度为55℃～70℃或为70℃～120℃，太阳能聚热器将导热介质加热到178℃～600℃。
按上述技术方案，导热介质将净海水加热的设定温度为±70℃，太阳能聚热器将导热介质加热到275℃～395℃。
利用太阳能连续供热的海水淡化装置进行海水淡化时，首先启动海水提升泵6b，从抽提海水井6a中抽取海水注入海水灭菌澄清池6中，由于海水井6a建于沙滩上最高潮水线6a2的上方，井深低于最低潮时海平面6a3，这使得井中的海水已经由沙滩的砂粒进行了一定的初步自然过滤，排除了大部分的海洋生物及杂质，而沙滩经每天的潮起、潮落海水冲刷，沙滩每天可自然地保持一定的清洁过滤能力。而在沙滩上打井的方法：井壁可采用有孔洞的多孔混凝土结构6a4，井壁外为碎石6a5，碎石外由沙滩的砂粒来填充构造。
在海水灭菌澄清池6中添加灭菌剂（如氯气），杀灭海水中的浮游生物及微生物、菌类，再添加絮凝剂（如FeCl2，或明矾均可），使海水静置清澈，池上部的澄清液经转运泵7a输入多级超滤池7中，经多级超滤成为净海水储存在净海水池8中待用。灭菌澄清池6底部（7a入口的下方）的沉渣，需定期冲洗（使用少量净海水）清理，排往污水处理厂。多级超滤池7也需定期使用净海水，进行反冲洗，以恢复各级过滤层的清洁过滤能力。
海水除盐系统启动时，在8a海水泵的驱动下净海水在除氧脱碳塔9中还需进一步脱除氧气及CO2气，因海水约含有3.5%的盐分，具有很强的腐蚀性，海水中含有的氧气及CO2气会加快设备的锈蚀，必需尽力脱除。
海水淡化时，白天太阳能聚热场1收集太阳光转化为1a中导热介质的热能，并通过导热介质存储热能在储热罐2中，热液泵2a驱动导热介质从2中流向海水加热器3中的换热器3b中，使净海水的温度升高（通常为55℃～120℃均可），本实施例设定为70℃，热海水在可调速海水泵3a的驱动下，输往1级闪蒸器4中（调节热海水泵3a的速度可控制输往1级闪蒸器4的海水流量，从而可控制4的海水液面高低），热海水经过节流装置4a时，4中为负压，压力突然降低，热海水中的水大量汽化，变为蒸汽上升，蒸汽中夹带的大粒海水滴，遇到消沫器被阻隔，落入闪蒸器底部，蒸汽上升到闪蒸器顶部，遇到本体冷凝器4d释放出潜热，一部分冷凝为淡水，落入到淡水储盘4c中，经管道汇流到淡水罐，另一部分未冷凝的蒸汽进入到海水冷却器4e中的4f换热器中，蒸汽再次被低温海水冷却，释放出潜热，冷凝为淡水汇流入淡水母管输往淡水罐。与此同时，1级闪蒸器底部的浓盐水，会自动进入2级闪蒸器，这是由于淡水罐5顶部设置的真空泵5a的运转，使得1、2级闪蒸器间存在压力差而形成的，浓盐水进入2级闪蒸器中又会重复4a到4f的全过程产出淡水。依上述重复过程一直到最末级闪蒸器，本实施例末级为9级闪蒸器。末级闪蒸器的浓盐水，最终经盐水泵5b驱动输往制盐厂进一步加工利用。这一过程中进入1级闪蒸器的海水，历经9级蒸馏过程，约有40%汽化并冷凝转化为淡水。
海水淡化中并非加热海水温度越高越好，当海水被加热到75℃～78℃时海水中的盐分（钠离子及钙、镁离子）会急剧在设备上结垢，影响设备的传热，降低效率。如果海水中添加阻垢剂后可以加热到120℃不结垢，但后期脱除这些物质又需费用。因此本实施例中优选的海水淡化避免结垢的最佳温度参数应是70℃左右或±70℃，在55℃～70℃以及70℃～120℃范围内的其他温度内当然也可以进行本发明的海水淡化，只是综合效益不如±70℃好。
本发明的优点：其一因太阳能聚热器高效率的运行最佳温度参数（目前太阳能聚光集热场的最佳运行参数）为275℃～395℃（以导热油为介质）或178℃～610℃（以熔融盐为介质），为此本发明采用高效太阳能聚热器加热导热介质（如导热油、硅油、石腊、熔融盐）可满足上述太阳能聚热器的温度运行参数，再用导热介质去加热海水到70℃左右，既可避免太阳能聚热器直接加热海水的设备结垢问题，使海水闪蒸淡化设备运行在最佳温度参数又可使太阳能聚热设备运行在最佳参数，达到收集太阳能热的效益最大化。
其二，一般淡水厂需24小时不间断供应淡水，通过导热介质（如导热油、硅油、石腊、熔融盐）存储太阳光热能，就可以使晚上也能加热海水，不间断生产淡水。
采用本实施例的多级闪蒸结构，由于采用了高效的太阳能聚光集热设备，可以高效收集相对分散的太阳能，完成对海水的加热蒸发，海水淡化率高达40%，并且可存储太阳能用于夜晚无阳光时连续运转生产淡水，产出淡水品质好，达到饮用水标准。而且主要大量使用清洁能源太阳能，海水淡化过程对环境友好，高效、产量大。
以上所揭露的仅为本发明的较佳实施例而已，当然不能以此来限定本发明之权利范围，因此依本发明申请专利范围所作的等效变化，仍属本发明的保护范围。

Claims (10)

  1. 一种太阳能连续供热的海水淡化装置，由海水净化系统、海水除盐系统组成；其特征在于：海水除盐系统主要包括太阳能聚光集热装置、太阳能蓄热罐、净海水加热器以及至少一级海水闪蒸器，海水闪蒸器主要由闪蒸器本体与海水冷却器构成；其中，太阳能聚光集热装置的导热介质腔与太阳能蓄热罐、以及净海水加热器中的导热介质换热器顺次封闭连通构成导热介质循环路径；海水净化系统的总净海水出口与净海水加热器和海水冷却器分别连通；净海水加热器的海水出口与闪蒸器本体连通；闪蒸器本体设置浓盐水出口、淡水出口和蒸汽出口，蒸汽出口经海水冷却器中的蒸汽换热器后同淡水出口一同汇集于淡水总管，淡水总管末端的密闭式淡水储罐与真空泵连通，浓盐水出口与制盐厂管道连通；海水冷却器的海水出口经闪蒸器本体中的本体冷凝器后与海水加热器连通；存在至少两级海水闪蒸器时，前级闪蒸器本体的浓盐水出口与下级闪蒸器本体连通，最后一级闪蒸器本体的浓盐水出口与制盐厂管道连通；各级闪蒸器本体内压力依次逐级降低形成负压。
  2. 根据权利要求1所述的海水淡化装置，其特征在于：在净海水加热器海水出口与闪蒸器本体之间设置转速可调的热海水泵，净海水加热器海水出口经热海水泵后与闪蒸器本体上的节流装置连通，节流装置位于液面之上；闪蒸器本体内部，节流装置上方设置消沫器，消沫器上方设置淡水储盘，淡水储盘上设置本体冷凝器；蒸汽出口位于闪蒸器本体顶部，淡水出口位于淡水储盘之上，浓盐水出口位于节流装置之下。
  3. 根据权利要求1或2所述的海水淡化装置，其特征在于：净海水加热器内还设置海水温度传感器和备用换热器，所述备用换热器的热源为热油炉、电加热炉、锅炉烟气余热、或汽机乏汽余热。
  4. 根据权利要求1所述的海水淡化装置，其特征在于：在太阳能蓄热罐和净海水加热器中的换热器间设置热液泵。
  5. 根据权利要求1或4所述的海水淡化装置，其特征在于：太阳能聚光集热装置是塔式太阳能集热器、或抛物面槽式真空管集热器、或全玻璃真空管集热器、或热管式真空管集热器。
  6. 根据权利要求1所述的海水淡化装置，其特征在于：海水净化系统为多级净化系统，顺次包括进行粗过滤的抽提海水井、海水灭菌澄清池、装设有活性碳滤层和多纤维滤芯层的多级超滤池、以及用于除氧脱碳的海水除氧脱碳塔；多级超滤池与海水除氧脱碳塔之间设置净海水池； 海水除氧脱碳塔与总净海水出口连通；抽提海水井通过海水提升泵与海水灭菌澄清池连通，海水灭菌澄清池通过一个海水转运泵与多级超滤池连通，多级超滤池通过另一个海水转运泵与净海水池连通，净海水池通过第三个海水泵与海水除氧脱碳塔连通，海水除氧脱碳塔通过净海水泵与总净海水出口连通；海水灭菌澄清池中添加有灭菌剂和絮凝剂。
  7. 根据权利要求1或6所述的海水淡化装置，其特征在于：抽提海水井建于沙滩上，井口位于海水最高潮水线上方，井底面位于低潮时海平面下方数米；井壁采用多孔混凝土结构，井壁外为碎石，碎石外由沙滩的砂粒填充。
  8. 采用上述权利要求1-7之一所述海水淡化装置的海水淡化方法，其特征在于：海水经过多级净化成为净海水；太阳能聚光集热装置收集太阳光对导热介质进行加热，使太阳能转化为导热介质热能，通过导热介质热能持续不断地加热净化后的净海水到设定温度，然后加热后的热净海水输往至少一级闪蒸器中进行闪蒸，闪蒸过程中，保持各级闪蒸器本体内压力依次逐级降低形成负压；闪蒸后的蒸汽经冷凝分离出淡水，部分没有一次冷凝的蒸汽经海水冷却器换热后成为淡水；闪蒸器底部没有气化的浓盐水输往制盐厂；存在多级闪蒸器时，闪蒸器底部的浓盐水依次流入后续各次级闪蒸器中，逐级闪蒸过程中再冷凝分离出淡水，没有气化的浓盐水最终输往制盐厂；太阳能聚光集热装置收集太阳光热能且利用导热介质加热净海水的同时，还将导热介质热能储存在太阳能蓄热罐中，在夜晚或阴天时利用储存的导热介质对净海水进行持续加热。
  9. 根据权利要求8所述的海水淡化方法，其特征在于：导热介质将净海水加热的设定温度为55℃～70℃或为70℃～120℃，太阳能聚热器将导热介质加热到178℃～600℃。
  10. 根据权利要求8所述的海水淡化方法，其特征在于：导热介质将净海水加热的设定温度为±70℃，太阳能聚热器将导热介质加热到275℃～395℃。
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111018026A (zh) * 2020-01-08 2020-04-17 浙江工业大学 一种蒸发器冷凝器双侧利用的热泵海水淡化装置
CN112551752A (zh) * 2020-12-10 2021-03-26 山东核电有限公司 一种基于反渗透海水淡化和核能供热的水热同传系统

Families Citing this family (31)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102976427B (zh) * 2012-12-25 2014-05-28 中盈长江国际新能源投资有限公司 一种太阳能连续供热的海水淡化装置及方法
WO2016001369A1 (en) * 2014-07-04 2016-01-07 Aalborg Csp A/S System of a desalination plant driven by a solar power plant
KR101658840B1 (ko) * 2014-11-12 2016-09-22 박용희 입체 구조 증발지에 의한 소금 생산 자동화 시스템
US20170189830A1 (en) * 2016-01-06 2017-07-06 John Markham Cody System for desalinating saltwater
CN105753104B (zh) * 2016-04-08 2018-04-17 天津融渌众乐科技有限公司 一种利用地热资源同时进行海水淡化和发电的系统及其工艺
CN107304055B (zh) * 2016-04-22 2023-06-02 天津华赛尔传热设备有限公司 一种利用蒸氨废液闪蒸卤水的氨法制碱系统
CN106006809B (zh) * 2016-07-15 2022-07-29 山东绿动力能源科技有限公司 太阳能热驱动喷射溅射多效复合式海水淡化系统
US20190240624A1 (en) * 2016-07-25 2019-08-08 Qatar Foundation For Education, Science And Community Development Hybrid desalination system
CN106277117A (zh) * 2016-08-27 2017-01-04 闫三朋 氯化铵废水双逆流独立低温双效蒸发方法及设备
CN106587234A (zh) * 2017-01-11 2017-04-26 江苏科技大学 一种基于压差的液体传输装置及工作方法
CN106745428B (zh) * 2017-01-11 2020-05-01 江苏科技大学 一种集热式太阳能多级闪蒸海水淡化装置及方法
CN108002475B (zh) * 2017-10-18 2024-01-12 浙江明烁节能科技股份有限公司 污水可再生能源的净化系统
CN108408804A (zh) * 2017-11-23 2018-08-17 中石化石油工程技术服务有限公司 盐水淡化和制备干蒸汽的一体化设备
CN109928561A (zh) * 2017-12-19 2019-06-25 云南师范大学 一种由太阳能电池供能的海水淡化除菌系统
US20180257950A1 (en) * 2018-03-22 2018-09-13 William Prichard Taylor Salt, potable water, and energy from saline water source
CN108633541B (zh) * 2018-04-20 2022-07-01 北京理工大学 一种可用海水直接灌溉的太阳能自产淡水种植装置
EP3801800B1 (en) * 2018-06-08 2023-08-30 EvCon GmbH Multistage membrane distillation apparatus
CN109319863A (zh) * 2018-08-30 2019-02-12 安庆船用电器有限责任公司 一种低能耗的防爆海水加热器
CN109734240A (zh) * 2019-03-26 2019-05-10 顾晓凡 一种海水淡化系统及淡化方法
CN110332086A (zh) * 2019-05-22 2019-10-15 大连海水淡化工程研究中心有限公司 一种太阳能光热水电联产工艺
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JP7421288B2 (ja) * 2019-09-02 2024-01-24 株式会社Ｅｎｅｏｓマテリアル クエンチ塔およびガスの冷却方法
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CN111533359A (zh) * 2020-06-14 2020-08-14 翟久香 一种节能环保型水净化再处理装置
CN112591835A (zh) * 2020-12-17 2021-04-02 中国科学院上海应用物理研究所 太阳能聚光集热装置及包含其的太阳能海水淡化系统
CN114988590B (zh) * 2022-07-08 2023-08-08 华北电力科学研究院有限责任公司西安分公司 一种以新能源为动力的海水去除硬度同步固碳系统及方法
CN115715888B (zh) * 2022-10-25 2023-11-28 浙江大学 多组集热轮启蒸发水盐分离系统及方法
CN116768310A (zh) * 2023-08-22 2023-09-19 山东省科学院能源研究所 一种太阳能联合热化学电池全时段多级闪蒸海水淡化系统

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001072638A1 (fr) * 2000-03-31 2001-10-04 Ebara Corporation Dispositif de dessalement
CN201620052U (zh) * 2009-12-24 2010-11-03 青岛理工大学 基于超声波和节流技术的太阳能海水淡化装置
CN201999824U (zh) * 2010-11-26 2011-10-05 中国科学院广州能源研究所 太阳能热泵联合空调海水淡化系统
CN102345576A (zh) * 2011-08-22 2012-02-08 杭州电子科技大学 高效率太阳能光热塔式发电与海水淡化一体化系统
CN102531256A (zh) * 2010-12-24 2012-07-04 中国石油天然气股份有限公司 一种低温海水淡化工艺方法及装置
CN102976427A (zh) * 2012-12-25 2013-03-20 中盈长江国际新能源投资有限公司 一种太阳能连续供热的海水淡化装置及方法
CN203006975U (zh) * 2012-12-25 2013-06-19 中盈长江国际新能源投资有限公司 一种太阳能连续供热的海水淡化装置

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS504195B1 (zh) * 1970-01-27 1975-02-15
JPS5344420B2 (zh) * 1972-04-07 1978-11-29
JPS5218472A (en) * 1975-08-04 1977-02-12 Toa Kogyo Kk Evaporating apparatus
US4110174A (en) * 1976-12-16 1978-08-29 Uop Inc. Power generation and potable water recovery from salinous water
JPS5429879A (en) * 1977-08-10 1979-03-06 Tomimaru Iida Apparatus for obtaining fresh water from sea water by utilizing solar heat
JPS5821557B2 (ja) * 1980-03-04 1983-04-30 株式会社 日本ケミカル・プラント・コンサルタント 海水淡水化装置
JPS56139188A (en) * 1980-03-31 1981-10-30 Sasakura Eng Co Ltd Distillation method of salt water using solar heat
JPS59110087U (ja) * 1983-01-14 1984-07-25 三井造船株式会社 太陽熱利用造水装置
RU2184592C2 (ru) * 2000-05-22 2002-07-10 Бажанов Владимир Михайлович Способ получения пресной воды и опреснитель для его осуществления
JP3766309B2 (ja) * 2001-10-22 2006-04-12 賢士 宍戸 太陽熱エネルギー利用の海水淡水化プラント
CN1307869C (zh) * 2003-10-22 2007-04-04 海阳市黄海水产有限公司 一种沙质海滩养殖用水取水方法及其装置
CN100357202C (zh) * 2004-07-08 2007-12-26 上海大学 液流式电容法海水淡化的预处理方法
RU2412909C1 (ru) * 2009-09-01 2011-02-27 Борис Алексеевич Зимин Опреснительная установка
CN102190340A (zh) * 2010-03-02 2011-09-21 孙元新 太阳能海水加热式多级双效蒸馏海水淡化工艺
CN201908793U (zh) * 2010-12-23 2011-07-27 河北新能电力集团有限公司 与海水淡化相结合的太阳能电水联供装置
CN202170852U (zh) * 2011-08-22 2012-03-21 杭州电子科技大学 一种高效率太阳能光热塔式发电与海水淡化一体化系统

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001072638A1 (fr) * 2000-03-31 2001-10-04 Ebara Corporation Dispositif de dessalement
CN201620052U (zh) * 2009-12-24 2010-11-03 青岛理工大学 基于超声波和节流技术的太阳能海水淡化装置
CN201999824U (zh) * 2010-11-26 2011-10-05 中国科学院广州能源研究所 太阳能热泵联合空调海水淡化系统
CN102531256A (zh) * 2010-12-24 2012-07-04 中国石油天然气股份有限公司 一种低温海水淡化工艺方法及装置
CN102345576A (zh) * 2011-08-22 2012-02-08 杭州电子科技大学 高效率太阳能光热塔式发电与海水淡化一体化系统
CN102976427A (zh) * 2012-12-25 2013-03-20 中盈长江国际新能源投资有限公司 一种太阳能连续供热的海水淡化装置及方法
CN203006975U (zh) * 2012-12-25 2013-06-19 中盈长江国际新能源投资有限公司 一种太阳能连续供热的海水淡化装置

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP2939981A4 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111018026A (zh) * 2020-01-08 2020-04-17 浙江工业大学 一种蒸发器冷凝器双侧利用的热泵海水淡化装置
CN112551752A (zh) * 2020-12-10 2021-03-26 山东核电有限公司 一种基于反渗透海水淡化和核能供热的水热同传系统

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