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WO2015035929A1 - 高效热能回收利用方法、系统及基于其的高纯碳酸锂制备方法及系统 - Google Patents

高效热能回收利用方法、系统及基于其的高纯碳酸锂制备方法及系统 Download PDF

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Publication number
WO2015035929A1
WO2015035929A1 PCT/CN2014/086344 CN2014086344W WO2015035929A1 WO 2015035929 A1 WO2015035929 A1 WO 2015035929A1 CN 2014086344 W CN2014086344 W CN 2014086344W WO 2015035929 A1 WO2015035929 A1 WO 2015035929A1
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WIPO (PCT)
Prior art keywords
heat
tank
water
temperature
energy recovery
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.)
Ceased
Application number
PCT/CN2014/086344
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English (en)
French (fr)
Inventor
朱彬元
余昊
彭福明
吴太林
彭浩
朱睿
洪瑞徽
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
DONGGUAN YONGGAN ENERGY TECHNOLOGY Co Ltd
GUANGZHOU RUISHI TIANQI ENERGY TECHNOLOGY Co Ltd
TIBET JINRUI ASSET MANAGEMENT Co Ltd
Original Assignee
DONGGUAN YONGGAN ENERGY TECHNOLOGY Co Ltd
GUANGZHOU RUISHI TIANQI ENERGY TECHNOLOGY Co Ltd
TIBET JINRUI ASSET MANAGEMENT Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from CN201310417287.3A external-priority patent/CN103482660B/zh
Priority claimed from CN201310619547.5A external-priority patent/CN103626209B/zh
Priority claimed from CN201420055996.1U external-priority patent/CN203731713U/zh
Priority claimed from CN201420272850.2U external-priority patent/CN203891565U/zh
Application filed by DONGGUAN YONGGAN ENERGY TECHNOLOGY Co Ltd, GUANGZHOU RUISHI TIANQI ENERGY TECHNOLOGY Co Ltd, TIBET JINRUI ASSET MANAGEMENT Co Ltd filed Critical DONGGUAN YONGGAN ENERGY TECHNOLOGY Co Ltd
Priority to US15/021,385 priority Critical patent/US20160221833A1/en
Publication of WO2015035929A1 publication Critical patent/WO2015035929A1/zh
Priority to US15/067,812 priority patent/US20160193545A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D15/00—Lithium compounds
    • C01D15/08—Carbonates; Bicarbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0018—Evaporation of components of the mixture to be separated
    • B01D9/0031—Evaporation of components of the mixture to be separated by heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/004—Fractional crystallisation; Fractionating or rectifying columns
    • B01D9/0045—Washing of crystals, e.g. in wash columns
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
    • C22B26/10—Obtaining alkali metals
    • C22B26/12—Obtaining lithium
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/02—Apparatus therefor
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24S—SOLAR HEAT COLLECTORS; SOLAR HEAT SYSTEMS
    • F24S23/00—Arrangements for concentrating solar-rays for solar heat collectors
    • F24S23/70—Arrangements for concentrating solar-rays for solar heat collectors with reflectors
    • F24S23/74—Arrangements for concentrating solar-rays for solar heat collectors with reflectors with trough-shaped or cylindro-parabolic reflective surfaces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24S—SOLAR HEAT COLLECTORS; SOLAR HEAT SYSTEMS
    • F24S30/00—Arrangements for moving or orienting solar heat collector modules
    • F24S30/40—Arrangements for moving or orienting solar heat collector modules for rotary movement
    • F24S30/45—Arrangements for moving or orienting solar heat collector modules for rotary movement with two rotation axes
    • F24S30/452—Vertical primary axis
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E10/00—Energy generation through renewable energy sources
    • Y02E10/40—Solar thermal energy, e.g. solar towers
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E10/00—Energy generation through renewable energy sources
    • Y02E10/40—Solar thermal energy, e.g. solar towers
    • Y02E10/47—Mountings or tracking
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a high-efficiency heat energy recycling method and system suitable for use in a plateau region, especially in a remote plateau region.
  • Plateau areas especially those with remote geographical locations, are generally sparsely populated, with large temperature differences between day and night, weak infrastructure, inconvenient transportation, and severe shortage of water and electricity supply. At the same time, however, a large amount of mineral resources have been stored in the plateau area to be developed.
  • salt lakes in the plateau contain a variety of high-value mineral salts, such as lithium, potassium and other strategic salts.
  • the mineral salt content in the salt lake is generally low, and it is difficult to use it in large-scale mining.
  • the mining process in recent years is mainly the salt lake water salt method, mineral deposit mining and other methods, of which the salt drying method is the most environmentally friendly mining method.
  • the crystallization operation directly affects the mining efficiency.
  • salt lake brines have to undergo multiple processes such as halogen production, concentration, and crystallization. The production cycle is 10 months long and the production efficiency is slow. Accelerating the crystallization of mineral salts is beneficial to shorten mining time and increase productivity.
  • the current accelerated crystallization method is mainly the natural evaporation of the solar pool. This method concentrates on the use of sunshine to raise the temperature of the brine and accelerate the precipitation of mineral salts. However, this method relies heavily on natural weather and is affected by factors such as sunshine intensity and wind and rain. The limitations have not fundamentally changed the situation of "depending on the heavens.”
  • Solar energy is a clean energy source, and solar energy is more abundant in areas with sufficient sunshine. Rational use of solar energy can help solve the problem of energy shortage.
  • lithium is an extremely important one.
  • Lithium has strong electrochemical activity and is a light metal with a wide range of uses.
  • the application fields of lithium include: ceramics and glass, synthetic rubber, aluminum production, plastics, pharmaceuticals, lubricants, air conditioners, televisions (fluorescent screens), lithium batteries, lithium alloys and nuclear industries; consumption reaches tens of thousands of tons per year. And is still growing.
  • lithium brine mine accounts for about 75%
  • hard rock lithium mine accounts for 25%
  • brine lithium ore accounts for about 72%
  • hard rock lithium mine accounts for 28%.
  • lithium resources were mainly derived from hard salt lithium ore.
  • the cost of lithium extraction from salt lakes is 1-1.5 times lower than that of hard rock.
  • the lithium salt produced from salt lakes has exceeded that of hard rock lithium mines. Extracting lithium salts from salt lake brines has become a major trend.
  • lithium extraction methods from brines include organic ion (TBP, ie, tributyl phosphate) exchange resin method, inorganic ion exchanger method, aluminate method, hydrogen chloride salting method, aluminate method, and Precipitation method (ie, phosphate method) and carbon method.
  • TBP organic ion
  • tributyl phosphate organic ion exchange resin method
  • inorganic ion exchanger method aluminate method
  • hydrogen chloride salting method aluminate method
  • Precipitation method ie, phosphate method
  • carbon method Precipitation method
  • the sulphated lakes such as Atacama Lake in Chile and Yinfeng Lake in the United States are pre-concentrated by the salt field method and then transported to the factory for processing; however, since the main salt lake in China is a carbonate lake, the above-mentioned salt field suitable for the sulphate lake The law is not suitable for China's carbonated salt lakes.
  • some experts in China proposed a salt field method suitable for extracting lithium from carbonate lakes, and applied it to the extraction of lithium salts.
  • the technology has the following disadvantages, resulting in losses:
  • the obtained lithium salt has low purity and many impurities, and needs to be transported to the factory for further processing; thus, the transportation cost is very high; and most of them are “useless transportation” for transporting impurities;
  • the existing salt lakes are basically in remote areas, with inconvenient transportation, lack of energy, fresh water, etc., further increasing the difficulty of purification.
  • Another object of the present invention is to provide a method and system for preparing lithium carbonate.
  • Efficient heat energy recycling method including the following steps:
  • the high temperature heat pump absorbs heat from the cold end of the water tank, releases heat to the warming tank through the hot end of the water tank, and heats the brine in the warming kettle to a desired temperature;
  • the normal temperature rinse liquid is returned to the lake after recovering the heat energy in the rinse liquid.
  • the liquid heat transfer medium contained in the hot end of the water tank and the hot end of the water tank is independently water and heat transfer oil.
  • High-efficiency heat energy recovery system for highland areas including: preheating tank, heating kettle, reactor, cold-end crystallization kettle, scrubbing tank and supernatant sedimentation tank; preheating tank, heating kettle, reactor, cold Both the end crystallizer and the distilled water tank are provided with a heat exchanger, and the scrubbing liquid holding tank is provided with a thermostat; the preheating tank is connected to the riser
  • the pipeline of the warm kettle is provided with a pipeline connected to the reaction kettle, and the reaction vessel is provided with a pipeline connected to the cold end crystallizer and the scrubbing liquid holding kettle, and the cold end crystallizer is connected to the supernatant liquid sedimentation tank.
  • the system is further provided with a heat-conducting oil tank, the heat-conducting oil tank is connected with a concentrating solar thermal device for heating the heat-conducting oil, and a closed heat-conducting oil pipeline connected to the heat exchanger in the reaction vessel and the distillation water tank heat exchanger;
  • a solar thermal device for supplying heat to the hot end of the water tank and the preheating pool is connected;
  • a high-temperature heat pump is arranged between the hot end of the water tank and the cold end of the water tank, and a heat exchanger is arranged between the hot end of the water tank and the warming kettle; a heat exchanger is arranged between the cold end of the water tank and the cold end crystallizing kettle;
  • the reaction kettle is connected with a vacuuming device provided with a heat exchanger for introducing steam into the preheating tank and extending to the distillation water tank; the distillation water tank is provided with a pipeline for introducing distilled water into the reaction vessel and the scrubbing liquid holding vessel.
  • the preheating pool is formed by connecting at least two preheating tanks in series.
  • the hot end of the water tank is connected with an electric heating device for assisting the supply of heat thereto.
  • the high temperature heat pump used in the above system has:
  • a multi-point heat balance heat exchanger that realizes heat exchange to generate hot water, which has a cold water input end, and the hot water outputted at the outlet end passes through the water pump and the check valve and is connected to the hot end of the water tank;
  • the heat pump compressor the compressed output refrigerant is sequentially supplied to the multi-point heat balance heat exchanger through the evaporator and the throttle device, and the refrigerant is discharged from the multi-point heat balance heat exchanger and then sucked and circulated by the heat pump compressor;
  • the multi-point heat balance heat exchanger is formed by connecting a plurality of sets of heat exchangers in series, and a cross flow channel is arranged between each group of heat exchangers.
  • the hot water outlet end of the multi-point heat balance heat exchanger is provided with a temperature regulating valve, and the output of the temperature regulating valve is connected to the water pump.
  • a gas-liquid separator is provided between the heat pump compressor and the evaporator.
  • the cold water input end of the multi-point heat balance heat exchanger is provided with a decontamination apparatus.
  • a high-temperature concentrating solar collector that can be used with the above system or used alone, including a curved concentrating reflector and a bracket for fixing the reflector, the front surface of the reflector is fixed with a light-transmitting plate, and two of the reflectors
  • the end plate is provided with an end plate, and the reflector, the light-transmitting plate and the end plate form a cavity together, and a heat collecting tube is arranged in a parallel direction in the cavity, and a liquid inlet port and a liquid outlet port are arranged in the heat collecting tube.
  • the heat collecting tube jacket in the above collector is provided with a transparent heat insulating tube.
  • the surface of the heat collecting tube in the above collector is black.
  • the heat insulating tube in the above collector is a double-layer vacuum glass tube.
  • the surface of the heat collecting tube in the above collector is a matte surface.
  • the bracket in the above collector is provided with a rotating shaft for adjusting the rotation of the reflector.
  • the rotating shaft in the above collector is provided with an angle meter.
  • the high temperature concentrating solar collector in the above collector is provided with a driver for driving the rotation of the rotating shaft.
  • the bottom of the reflector in the above collector is provided with a liquid discharge port.
  • the surface of the light-transmitting plate in the above-mentioned heat collector is provided with an antistatic coating or a conductive layer.
  • the preparation method of high-purity lithium carbonate includes the following steps:
  • the salt lake brine is concentrated by evaporation under reduced pressure, and then the temperature is raised to 60 ° C or higher, preferably 65 ° C or higher to allow the lithium carbonate to crystallize.
  • the lithium carbonate salt is washed with distilled water recovered by evaporation of the brine and concentrated until the mass remains substantially unchanged.
  • the flushing direction is periodically switched during flushing.
  • the distilled water recovered by evaporation and concentration of brine is used for the preparation of high-purity lithium carbonate derived from the condensed water obtained by evaporation and concentration of brine.
  • a high-purity lithium carbonate preparation system the system comprises a brine concentrating crystallizer and a refiner, the brine concentrating crystallizer is provided with a heat storage tank and a heating tank, and the heat storage tank and the heating tank are independently provided with a heat exchange device, a heat storage tank and heating The heat exchange device of the tank is respectively connected to the heat absorption end of the heat pump and the heat release end, the heating tank is provided with a brine inlet and a tail halogen discharge port, and the tail halogen discharge port is connected to the heat storage tank through a pipeline; the refiner includes a pure tank, and the pure The tank is provided with a water outlet and a water inlet, and a radial filter for supporting the crystal of lithium carbonate is provided in the lower part of the pure tank.
  • the upper portion of the purified tank is provided with a detachable radial screen for preventing the outflow of lithium carbonate crystals.
  • the brine concentrating crystallizer is connected to a vacuuming device, the vacuuming device is connected to the water vapor condenser, and the water vapor condenser is connected to the distilled water temporary storage tank.
  • the vacuuming device extracts water vapor and reduces the pressure on the surface of the liquid, which helps to accelerate the concentration of the liquid.
  • the extracted water vapor is condensed and the by-product distilled water is especially suitable for remote areas lacking pure water.
  • the distilled water temporary storage tank recovered upon evaporation and concentration of the brine is provided with a water inlet connected to the pure tank.
  • a screen is provided in front of the tail halogen discharge port.
  • a circulation pump is provided between the water outlet of the purified tank and the water inlet.
  • the refiner is provided with a heat exchange device.
  • a detachable inner screen layer is provided in the heating tank.
  • the pure tank is provided with a hot air drying device.
  • the hot air drying device can be simply placed in the hot air inlet and outlet of the pure tank.
  • the water outlet of the purified tank is provided with a three-way valve, and one end of the three-way valve is connected to the heat storage tank through a pipe.
  • a filter screen is provided in front of the water outlet and the water inlet of the purified tank.
  • Applicable to high-altitude industrial buildings including side walls, with a top cover fixed on the side wall, the top cover is arched, the top cover is provided with insulation layer, and the underside of the top cover is separated by the inner wall into the inner production area and the outer cover
  • auxiliary area there is a thermal insulation board above the production area, and a ditches are arranged in the auxiliary area.
  • a reservoir is connected, and at least one of the reservoirs is located in the auxiliary zone.
  • the ends of the trench have a certain slope.
  • a venting cover is provided above the further ditch.
  • a part of the top cover above the auxiliary area in the above industrial building is light transmissive, and the auxiliary area is planted with plants.
  • a heat exchanger is provided in the reservoir in the above industrial building.
  • a condensed water collecting pipe is provided under the top cover in the above industrial building.
  • the side wall in the above industrial building is provided with an inlet.
  • the production area in the above industrial building is provided with a gate, and the wall on the opposite side of the door is provided with a ventilation window.
  • a living area is provided in the auxiliary area in the above industrial building.
  • the thermal energy utilization method of the invention can efficiently recover heat energy, and has the advantages of rapid heat exchange capacity and slow heat exchange capacity, meets different demands of heat of industrial production, and can be widely applied to various industrial production processes requiring heating and cooling, especially Suitable for the extraction of salt lake mineral salts.
  • the thermal energy utilization system of the present invention can fully utilize the abundant sun in the plateau region, efficiently recover thermal energy, and provide stable heating for production to meet the needs of production. At the same time, the system of the present invention can produce fresh water by-product to further meet the production and living needs.
  • the thermal energy utilization system of the invention is rationally designed, and uses a liquid and a heat pump for heat exchange, so that the brine is crystallized only in various kettles, and the brine delivery pipeline is not scaled.
  • the use of high-temperature heat-conducting oil to rapidly replenish the brine can meet the heat required for large-scale evaporation of water under reduced pressure, and can realize standardized operation.
  • a batch of brine can be completed in about 1-2 hours.
  • the concentrated crystallization in the case of sufficient heat in the afternoon, can complete the concentration and crystallization of a batch of brine in 10 to 30 minutes, greatly speeding up the concentration of brine, and extracting various mineral salts from the brine, making the production more controllable and avoiding. "Don't eat by the sky.”
  • the system of the present invention can increase the heating capacity by 2 to 3 times under the premise of the same power consumption, and at the same time recover most of the heat energy in the production process, realizing the plateau region.
  • the efficient heat recovery and utilization have greatly reduced the energy required for industrialized extraction devices in the plateau, greatly reducing the amount of fixed investment and environmental protection.
  • the heat energy utilization system uses a high-temperature heat pump, and the heat exchange efficiency is high.
  • the temperature of the hot end of the water tank can be increased by 85 ° C in the plateau region by the first-stage heat pump, and the heat exchange efficiency is high.
  • the heat pump does not directly contact the corrosive brine, and has a long service life and stable operation.
  • the high-temperature solar collector of the invention is completely enclosed, has no air convection with the outside, no convective heat loss, high light-heat conversion efficiency, and can heat the heat-conducting medium to above 200 ° C to meet the needs of special industrial production. It can be well applied to the heating of other media, such as water, antifreeze, heat transfer oil, etc.
  • the high-temperature solar collector of the invention has the advantages of simple structure, easy manufacture, easy installation, no need to consider the construction impact of seasonal frozen soil, strong interchangeability, convenient maintenance, and can effectively resist dust, wind, rain, snow and ultraviolet rays. Unfavorable natural conditions such as aging of equipment, especially suitable for highland areas.
  • the lithium carbonate purification process of the invention does not require the use of chemical reagents, and the purity of lithium carbonate can be completed by physical operation, and the purity of the purified lithium carbonate is as high as 95% or more, which helps to reduce the transportation cost in the later stage to further purification. cost.
  • the process of the invention has extremely low transportation requirements and does not pollute the environment.
  • the lithium carbonate purification process of the present invention can fully recover the water vapor generated by evaporation and concentration of the salt lake brine, and condense it into pure distilled water. After the distilled water is used, it can re-enter the salt lake and effectively replenish the salt lake to avoid the ecological problems caused by the drop of the salt lake water level.
  • distilled water can be produced by condensing water vapor while accelerating the concentration of brine.
  • the obtained distilled water can be further used for the purification of the lithium carbonate salt. It effectively solves the problem of lack of fresh water (distilled water) in the remote salt lake area, further reducing the cost of purification.
  • the distilled water After the distilled water is used, it can re-enter the salt lake and effectively replenish the salt lake to avoid or reduce the ecological problems caused by the drop of the salt lake water level.
  • the lithium carbonate purification system of the present invention is convenient to use, and can obtain lithium carbonate of high purity. At the same time, sodium and potassium salts can be produced by-product in the heat storage tank.
  • the lithium carbonate purification system of the invention does not require additional chemical supplements and has high energy efficiency.
  • the industrial building of the invention has an arched top cover extending from top to bottom to the side wall, covering the entire production area and the auxiliary area, having good airtightness, greatly reducing the use of the internal thermal insulation material, and reducing the difficulty of the internal thermal insulation design. .
  • the industrial building of the invention can well retain moisture and heat, has excellent heat preservation and moisture retention, and helps to improve the air humidity and temperature in the building, and makes people feel more comfortable.
  • an additional insulation board is arranged above the production area, which can effectively reduce the loss of heat from the top, and greatly reduce the adverse effects of excessive temperature difference between day and night on the equipment.
  • the increase in humidity is also conducive to reducing dust in the building, while effectively avoiding the accumulation of static electricity, which is conducive to safe production.
  • the industrial building of the invention has a small overall wind resistance and excellent wind resistance. It can ensure that the snow can slide down the top cover faster, avoid excessive accumulation, and has better weather resistance, which can meet the special requirements of high altitude.
  • the industrial building of the invention can realize modular design, is easy to be assembled in situ, greatly reduces construction difficulty and improves construction efficiency.
  • Water or salt lake brine can be added to the ditch.
  • the water evaporates under the action of heat, which improves the humidity of the auxiliary area and provides a more comfortable living and working environment for the people in the living area.
  • a higher temperature liquid can be introduced into the ditch to further reduce the temperature difference between the inside and outside of the building.
  • the higher temperature liquid can be a liquid produced during the day and stored in the reservoir.
  • the ditch can be further used for preliminary warming and concentration treatment of the salt lake brine to reduce energy consumption.
  • the salt crystals therein can be further concentrated at the bottom for collection.
  • Plants planted in the auxiliary area can use the condensed water produced during production and life to grow, and at the same time release enough oxygen to better supply oxygen to the living area, improve air quality, and create a more suitable ecological environment for human habitation.
  • the production of a large amount of primary condensate in the production area can partially provide a living fresh water and medical pure water raw material of about 60 ° C in the living area, which can solve the long-term medical and health problems of local people.
  • the surrounding soil Due to the long-term air condensate entering the soil, the surrounding soil is continuously moistened, extracting the necessary water for plant growth around the plant, and further improving the small environment around the building.
  • FIG. 1 is a schematic structural view of a heat recovery utilization system of the present invention
  • FIG. 2 is a schematic structural view of a high temperature heat pump of the heat recovery utilization system of the present invention
  • FIG. 3 is a schematic structural view of a multi-point heat balance heat exchanger of the heat recovery utilization system of the present invention.
  • FIGS. 4 and 5 are schematic structural views of a heat collector of the present invention.
  • FIG. 6 is a schematic structural view of a concentrated crystallizer of a high-purity lithium carbonate preparation system of the present invention.
  • FIG. 7 is a schematic structural view of a refiner of a high-purity lithium carbonate preparation system of the present invention.
  • Figure 8 is a schematic cross-sectional structural view of an industrial building of the present invention.
  • Figure 9 is a plan view showing the planar structure of the industrial building of the present invention.
  • Efficient heat energy recycling method including the following steps:
  • the high temperature heat pump absorbs heat from the cold end of the water tank, releases heat to the warming tank through the hot end of the water tank, and heats the brine in the warming kettle to a desired temperature;
  • the heat transfer oil is heated to 120 ° C or higher, preferably to 150 ° C or lower, and more preferably to 200 ° C or higher, using a concentrating solar thermal device.
  • the hot end of the water tank needs to exchange heat with the heating chamber to heat the brine in the heating pot.
  • the temperature of the liquid heat transfer medium is generally 70-80 °C.
  • the liquid heat transfer medium in the hot end of the tank is required to have a higher temperature.
  • the price of water is low, the safety is high, and there is no pollution, but its boiling point is low; the price of heat transfer oil is higher, the boiling point is high, and the safety is good, but its specific heat capacity is lower.
  • the liquid heat transfer medium can be selected from water or heat transfer oil, or other liquid heat transfer medium.
  • the cold end of the water tank needs to exchange heat with the cold end crystallizer, and the medium temperature generally does not exceed 40 °C. It is more economical to use water having a higher heat capacity, lower cost, and higher safety as a heat transfer medium. Of course, if you have special requirements, you can also use heat transfer oil or other liquid heat transfer medium.
  • a high-efficiency heat energy recovery system suitable for use in a plateau region, including a preheating tank 1, a warming kettle 8, a reaction kettle 2, a cold-end crystallizer 4, a scrubbing liquid holding tank 3, and a supernatant sedimentation tank 5;
  • the preheating tank 1, the heating tank 8, the reaction kettle 2, and the cold end crystallizing kettle 4 are each provided with a heat exchanger, and the scrubbing liquid holding tank 3 is provided with a thermostat;
  • the preheating tank 1 is provided with a heating chamber 8
  • the pipeline, the temperature riser 8 is provided with a pipeline connected to the reaction vessel 2, the reactor 2 is provided with a pipeline connected to the cold end crystallizer 4 and the scrubbing liquid heat tank 3, and the cold end crystallizer 4 is provided with a supernatant liquid.
  • the pipeline of the sedimentation tank 5 is provided with a supernatant liquid.
  • the system is further provided with a heat transfer oil tank 60 connected with a concentrating solar thermal device for heating the heat transfer oil, and a closed heat transfer oil line connected to the heat exchanger in the reaction kettle and the distillation water tank heat exchanger;
  • a hot water heater 61 and a preheating tank 1 are connected to a solar thermal device for supplying heat thereto;
  • a high temperature heat pump is disposed between the hot end 61 of the water tank and the cold end 62 of the water tank, and a heat exchanger is disposed between the hot end 61 of the water tank and the warming tank 1; a heat exchanger is disposed between the cold end 62 of the water tank and the cold crystallizer 4;
  • the reaction vessel 2 is connected to a vacuuming device 21 which is provided with a pipe for introducing steam into the heat exchanger in the preheating tank 1 and extending to the distillation water tank 22; the distillation water tank 22 is provided with water to be introduced into the distilled water heater and The piping extends to the reaction vessel 2 and the scrubbing liquid holding tank 3.
  • the preheating pool is formed by connecting at least two preheating tanks in series.
  • the different preheating tanks are relatively independent, and the brine contained therein can be heated step by step to ensure that the brine at the preheating end can reach the required temperature faster.
  • the hot end of the water tank is connected with an electric heating device for assisting the supply of heat thereto.
  • an electric heating device for assisting the supply of heat thereto.
  • surplus power can be converted into heat energy to accelerate production.
  • direct heating of the brine causes the fouling of the heating device and affects the heating efficiency.
  • the high temperature heat pump 7 used in the above system has:
  • a multi-point heat balance heat exchanger 71 for heat exchange to generate hot water, having a cold water input end, the hot water outputted at the outlet end thereof is passed through the water pump 713 and the check valve 714 and then connected to the hot end 61 of the water tank;
  • the heat pump compressor 72, the compressed output refrigerant is sequentially supplied to the multi-point heat balance heat exchanger 71 through the evaporator 721 and the throttle 722, and the refrigerant is discharged from the multi-point heat balance heat exchanger 71 and then sucked and circulated by the heat pump compressor 72. ;
  • the multi-point heat balance heat exchanger 71 is formed by connecting a plurality of sets of heat exchangers 715 in series, and a cross flow channel 716 is disposed between each set of heat exchangers 715.
  • the hot water outlet end of the multi-point heat balance heat exchanger 71 is provided with a temperature regulating valve 717, and the output of the temperature regulating valve 717 is connected to the water pump 713.
  • a gas-liquid separator 723 is provided between the heat pump compressor 72 and the evaporator 721.
  • the cold water input end of the multi-point heat balance heat exchanger 71 is provided with a decontamination apparatus 718.
  • the composite refrigerant has an exhaust pressure of 23 to 24 kg, a return pressure of 2 to 3 kg, a condensation temperature of 115 to 120 ° C, and an altitude of 3500 to 4500 m to ensure that the hot water temperature reaches 85 ° C, which satisfies the plateau industrial production application. .
  • the method for extracting lithium carbonate by high-efficiency heat energy recovery comprises the following steps:
  • the steam generated in the concentration under reduced pressure is cooled into the heat exchanger in the preheating tank through the pipeline to be cooled, and the released heat is first heated to the secondary preheating tank (high temperature), after condensation
  • the hot water is introduced into the heat exchanger of the first preheating tank (low temperature), so that the counter temperature heat exchange maintains a large temperature difference between the brine and the steam (hot water), and the brine in the secondary preheating temperature can be Effectively preheating, and can fully recover the latent heat in the steam;
  • the distilled water obtained is collected in a distilled water tank for use;
  • the high-temperature supernatant after crystallization in the reaction vessel is introduced into the cold-end crystallizer via a pipeline, and the liquid heat-conducting medium in the cold end of the water tank is circulated into the heat exchange coil in the cold-end crystallizer, and the cold-end crystallizer is The high temperature supernatant is cooled, and after the temperature is lowered, the salt in the supernatant is saturated and crystallized to obtain K and Na salts; the normal temperature or low temperature supernatant after cooling and crystallization is introduced into the supernatant sedimentation tank for further recovery treatment or supplementation.
  • the salt lake reduce its damage to the ecology of the salt lake;
  • a batch of brine can be concentrated and crystallized in about 1 to 2 hours. Under the condition of sufficient heat in the afternoon, a batch of brine can be concentrated and crystallized in 10 to 30 minutes. Calculated according to the working time of 8-10 hours a day, the concentrated crystallization of multiple batches of brine can be completed on the same day.
  • the collected lithium carbonate can be uniformly concentrated in the scrubbing liquid holding kettle for overnight. After the crystal grows up, the post-treatment can be processed to obtain high purity. More than 90% of the lithium carbonate crystals completely escape the traditional production process of “depending on the sky”.
  • the heat energy recycling and utilization method and system of the invention can recycle nearly 60 to 70% of the heat energy in the system, and can reduce the installed capacity of the supporting solar photovoltaic power generation station to 25 to 33% of the original machine capacity, thereby greatly reducing the fixed investment.
  • the test data shows that in the plateau area above 3700 above sea level, the concentrating solar thermal device is used, generally reach the temperature above 100 °C at around 10:00 am, until the temperature is still around 18:30, the temperature can still be protected at 120. Above °C, it can completely realize industrial production and completely change the production of existing salt lakes. Process.
  • the high-temperature concentrating solar collector includes an arc-shaped concentrating reflector A1 and a bracket A2 for fixing the reflector A1.
  • the front surface of the reflector A1 is fixed with a transparent board A3 and a reflector.
  • An end plate A4 is arranged at both ends of the A1, and the reflecting plate A1, the translucent plate A3 and the end plate A4 form a cavity together, and a heat collecting tube A5 is arranged in a parallel direction in the cavity, and a liquid inlet port and a liquid outlet port are arranged in the heat collecting tube A5. .
  • the curved concentrating reflector has a trough shape as a whole, and the parallel direction is the direction of the axis of the reflector. In this way, the sunlight that is irradiated at different angles can be focused on a straight line, and the angle of the reflector is not frequently adjusted, which is advantageous for reducing equipment maintenance.
  • the heat collecting tube A5 in the above-mentioned heat collector is provided with a transparent heat insulating tube A6.
  • the insulation tube can both transmit light and block air convection. This can further reduce the heat exchange between the heat collecting tube and the external environment, and improve the efficiency of photothermal conversion.
  • the surface of the heat collecting tube in the above collector is black.
  • the black surface can absorb all kinds of light more fully and improve the light-to-heat conversion efficiency.
  • the heat insulating tube in the above collector is a double-layer vacuum glass tube.
  • the double-layer vacuum glass tube has good light transmittance and good heat preservation performance, and is more helpful for improving the light-to-heat conversion efficiency.
  • the surface of the heat collecting tube in the above collector is a matte surface.
  • the matte finish further reduces light reflection, which in turn increases photothermal conversion efficiency.
  • the bracket A2 in the above-mentioned heat collector is provided with a rotating shaft A21 for adjusting the rotation of the reflecting plate A1, which is convenient for adjustment in the case where the sun irradiation angle is excessively changed.
  • the rotating shaft in the above collector is provided with an angle meter for quick and accurate adjustment.
  • the high-temperature concentrating solar collector in the above-mentioned heat collector is provided with a drive for driving the rotating shaft to facilitate automatic regulation.
  • the bottom of the reflector in the above collector is provided with a liquid discharge port A11, which can balance the pressure inside and outside the cavity and prevent water from accumulating in the cavity.
  • the surface of the light-transmitting plate in the above-mentioned heat collector is provided with an antistatic coating or a conductive layer A31 to eliminate static electricity on the surface and prevent the surface from adsorbing dust to affect light transmission.
  • the thermal fluid When using, the thermal fluid is introduced through the liquid inlet, and the liquid outlet is exported. If necessary, multiple collectors can be connected in series to obtain a higher temperature, or the temperature of the thermal fluid can be adjusted by adjusting the speed of the liquid. Convenient to get the temperature you need.
  • the preparation method of high-purity lithium carbonate includes the following steps:
  • the salt lake brine is concentrated by evaporation under reduced pressure, and then the temperature is raised to 60 ° C or higher, preferably 65 ° C or higher to allow the lithium carbonate to crystallize.
  • the flushing direction is periodically switched during flushing. If the washing direction is changed every 10 seconds or 20 seconds, it is more beneficial to improve the washing efficiency and prevent the crystal from clogging the filter.
  • the distilled water comes from the condensed water obtained when the brine is concentrated or evaporated.
  • a preparation system of high-purity lithium carbonate includes a brine concentrating crystallizer and a refiner, and the brine concentrating crystallizer is provided with a heat storage tank B1 and a heating tank B2, and the heat storage tank B1 and the heating tank B2 are independently provided.
  • the heat exchange device B41, the heat exchange device of the heat storage tank B1 and the heating tank B2 are respectively connected with the heat absorption end and the heat release end of the heat pump B4, and the heating tank B2 is provided with a brine inlet B21 and a tail halogen discharge port B22, and the tail halogen row
  • the outlet B22 is connected to the heat storage tank B1 through a pipe;
  • the refiner includes a pure tank B3, the pure tank is provided with a water outlet B32 and a water inlet B31, and the lower part of the pure tank B3 is provided with a radial filter for supporting lithium carbonate crystals. Net B33.
  • the upper portion of the purified tank B3 is provided with a detachable radial filter B34 for preventing the outflow of lithium carbonate crystals.
  • the brine concentrating crystallizer is connected to the vacuuming device B5, the vacuuming device B5 is connected to the water vapor condenser, and the water vapor condenser is connected to the distilled water temporary storage tank B6.
  • the vacuuming device extracts water vapor and reduces the pressure on the surface of the liquid, which helps to accelerate the concentration of the liquid.
  • the extracted water vapor is condensed and the by-product distilled water is especially suitable for remote areas lacking pure water.
  • the distilled water temporary storage tank B6 is provided with a water inlet B31 connected to the purified tank.
  • the distilled water can be preheated to the desired temperature before the distilled water is introduced into the pure tank.
  • the refiner is provided with a heat exchanger B41 to ensure that the temperature inside the tank remains stable during rinsing.
  • the heat exchanger B41 can be disposed in the pure tank, or in an external pipeline or a circulation pump, more preferably in a distilled water storage tank, or at multiple locations at the same time to ensure distilled water during flushing. The temperature is maintained at the desired temperature.
  • a filter screen is arranged in front of the tail halogen discharge port, so that the lithium carbonate crystal salt can be taken out when the tail halogen is discharged, thereby affecting the yield.
  • a detachable inner screen layer is provided in the heating tank. This ensures that most of the lithium carbonate crystals are deposited in the screen, and the obtained lithium carbonate can be easily taken out. The extracted lithium carbonate can be transferred to a purified tank for further purification.
  • a circulation pump B7 is provided between the water outlet B32 of the purified tank and the water inlet B31. This allows the hot water to be circulated to wash the lithium carbonate crystal salt to speed up the purification process.
  • the water discharged from the circulation pump preferably flushes the lithium carbonate crystal salt from the bottom upward, so that crystal deposition can be avoided, and the bottom crystal is difficult to be washed, which affects the purification effect.
  • other rinsing methods can also be used, such as rinsing from top to bottom, rotary rinsing, etc., or a combination of various rinsing methods.
  • the pure tank is provided with a hot air drying device.
  • the hot air drying device can be simply placed in the hot air inlet and outlet of the pure tank.
  • the hot air is preferably blown from the bottom of the lithium carbonate crystals and blown out from the upper portion, so that the purified lithium carbonate can be dried more quickly.
  • the water outlet of the purified tank is provided with a three-way valve, and one end of the three-way valve is connected to the heat storage tank through a pipe.
  • the three-way valve makes it easy to control the flow of water as needed.
  • the flushed hot water is introduced into the heat storage tank, and then the heat pump is used to utilize the waste heat, which helps to improve energy utilization, and is particularly suitable for use in remote areas.
  • a filter screen is provided in front of the water outlet and the water inlet of the purified tank. This helps prevent crystallization from entering the pipeline, affecting the normal operation of the equipment and the yield of lithium carbonate.
  • Li ion concentration 1.29g / L brine, 60 ° C or more additional crystals precipitated crude lithium salt and brine mixed wet salt simply remove the supernatant, weighed 897.6g, mixed with 80 ° C distilled water 3000g, mixed thoroughly for 3 minutes, after After suction filtration and drying, 47.4 g of lithium carbonate having a purity of 62% was obtained, and a lithium carbonate yield of 73.5% was obtained from the crude lithium salt.
  • Li ion concentration 1.29g / L brine, 60 ° C or more, crystallized precipitation of crude lithium salt and brine mixed wet salt simply remove the supernatant, weighed 877.9g, with 70 ° C distilled water 2250g, respectively, 1200g, 600g, 300g, 150g
  • the mixture was rinsed in the manner of Example 1 for 4 times, and stirred for 30 minutes each time for 2 minutes. After suction filtration and drying, 37.56 g of lithium carbonate having a purity of 91.3% was obtained, and the yield of lithium carbonate was obtained from the crude lithium salt. It is 85.7%.
  • Li ion concentration of 1.29g / L brine, 60 ° C or more increased crystal precipitation of crude lithium salt and brine mixed wet salt simply remove the supernatant and weigh 986.7g, placed in a pure tank, add 90 ° C distilled water 1800g, every 10 The cycle was repeated for one minute in a single direction, and dried by hot air to obtain 39.74 g of lithium carbonate having a dry purity of 97.6%, and a lithium carbonate yield of 96.97% from the crude lithium salt.
  • the purified tank can continuously carry out the purification process of the lithium carbonate salt in a rapid and water-saving manner. Flushing in the direction of change not only improves the flushing efficiency, but also avoids the accumulation of crystals in the pipeline or in the pure tank. It can be self-cleaning, facilitate the use of equipment, and help to reduce maintenance.
  • the purification operation time of the lithium carbonate coarse salt is reduced to one-third of the traditional method; the self-cleaning design eliminates the drawback that the traditional scrubbing method must be frequently maintained; the amount of flushing distilled water used is reduced to 60% of the conventional method. Moreover, the systemic loss of lithium carbonate in the conventional process is avoided, and a lithium carbonate product having a purity of 97% or more and a yield of 96% or more is obtained.
  • the industrial building suitable for high altitude areas including the side wall C1, the top wall C1 is fixed with a top cover C2, the top cover C2 is arched, the top cover C2 is provided with an insulation layer, and the top cover C2 is
  • the inner wall C3 is isolated as the inner production area C4 and the outer auxiliary area C5, the production area C4 is provided with a thermal insulation board C43, and the auxiliary area C5 is provided with a ditches C6.
  • the inner wall preferably consists of a load bearing column and a thermal insulation panel.
  • part of the top cover of the production area can transmit light, and correspondingly, the thermal insulation board underneath is also light-transmissive, so that natural light can be fully utilized to further reduce energy consumption.
  • the top cover can be provided with several venting windows that can be opened and closed.
  • the arched top covers can also be spliced to each other as needed to achieve a larger production area in parallel. This makes it easy to adjust the overall size of the building to meet the needs of different production scales. It can also be easily expanded with the expansion of production scale to meet the needs of production in different periods.
  • a reservoir C61 is connected, and at least one of the reservoirs C61 is located in the auxiliary zone C5.
  • both ends of the trench C6 have a certain slope.
  • venting cover is arranged above the trench.
  • the venting cover will not affect the emission of moisture, but also avoid excessive dust and debris entering the ditch.
  • a part of the top cover above the auxiliary area in the above industrial building is light transmissive, and the auxiliary area is planted with plants.
  • the planted plants preferably release oxygen at night, which prevents plants from consuming too much oxygen at night and affecting air quality.
  • a heat exchanger is provided in the reservoir in the above industrial building.
  • the heat exchanger stores excess heat to maintain nighttime temperatures in the building.
  • a condensed water collecting pipe is provided under the top cover in the above industrial building.
  • the outlet of the condensate collection pipe is located in the plant area, making full use of water resources to provide sufficient water for plant growth.
  • the side wall in the above industrial building is provided with an inlet. This can facilitate people's access, and can also open the entrance as needed to enhance the air circulation in the auxiliary area.
  • the production area in the above industrial building is provided with a gate C41, and the wall on the opposite side of the gate C41 is provided with a ventilation window.
  • a living area is provided in the auxiliary area in the above industrial building.
  • Various living facilities that help improve the hard conditions of the plateau can be set up in the living area.
  • the industrial building of the invention has excellent heat preservation and moisture retention, and can basically retain the moisture generated in the production process, improve the air humidity in the building, and make people feel more comfortable.
  • an additional insulation board is arranged above the production area, which can effectively reduce the loss of heat from the top, and greatly reduce the adverse effects of excessive temperature difference between day and night on the equipment.
  • the increase in humidity is also conducive to reducing dust in the building, while effectively avoiding the accumulation of static electricity, which is conducive to safe production.
  • the industrial building of the invention has a small overall wind resistance and excellent wind resistance.
  • the arched top cover ensures that the snow can slide down faster, avoid excessive accumulation, and has better weather resistance to meet the special requirements of high altitude areas.
  • the industrial building of the invention can realize modular design, is easy to be assembled in situ, greatly reduces construction difficulty and improves construction efficiency.
  • Water or salt lake brine can be added to the ditch.
  • the water evaporates under the action of heat, which improves the humidity of the auxiliary area and provides a more comfortable living and working environment for the people in the living area.
  • a higher temperature liquid can be introduced into the ditch to further reduce the temperature difference between the inside and outside of the building.
  • the higher temperature liquid can be a liquid produced during the day and stored in the reservoir.
  • the ditch can be further used for preliminary warming and concentration treatment of the salt lake brine to reduce energy consumption.
  • the salt crystals therein can be further concentrated at the bottom for collection.
  • Plants planted in the auxiliary area can use the condensed water produced during production and life to grow, and at the same time release enough oxygen to better supply oxygen to the living area, improve air quality, and create a more suitable ecological environment for human habitation.
  • the production of a large amount of primary condensate in the production area can partially provide a living fresh water and medical pure water raw material of about 60 ° C in the living area, which can solve the long-term medical and health problems of local people.
  • the surrounding soil Due to the long-term air condensate entering the soil, the surrounding soil is continuously moistened, extracting the necessary water for plant growth around the plant, and further improving the small environment around the building.

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Abstract

高效热能回收利用方法、系统及基于其的高纯度碳酸锂的制备方法及系统。利用聚光式太阳能光热装置对导热油加热至高温，之后应用其对减压蒸发进行快速补热，同时，采用多种方式对热能进行回收，以回收生产过程中的大部分热能，实现在高原地区的连续生产，降低电力消耗，减少光伏电站的装机容量。采用高纯度碳酸锂的制备方法及系统，实现物理法制备，不污染环境。

Description

高效热能回收利用方法、系统及基于其的高纯碳酸锂制备方法及系统 技术领域
本发明涉及一种适用于高原地区，特别是偏远高原地区的高效热能回收利用方法及系统。
背景技术
高原地区，特别是地理位置偏远的高原地区，普遍人烟稀少，昼夜温差大，基础设施薄弱，交通不便，水电供应严重不足。但是同时，高原地区又贮藏着大量的矿产资源有待开发。
如高原地区的盐湖中含有多种高价值的矿物盐，如锂、钾等具有战略意义的盐。但是盐湖中的矿物盐含量普遍较低，大规模开采利用难度较大。受限于恶劣的自然条件，近年来的开采工艺主要是盐湖水晒盐法、矿床开采等方法，其中晒盐法是最环保的开采方法。在晒盐法开采矿物盐的过程中，结晶操作直接影响着开采效率。一般而言，盐湖卤水要经历制卤、浓缩、结晶等多个过程，生产周期达10个月之久，生产效率慢。加速矿物盐结晶有利于缩短开采时间，提高产率。
目前的加速结晶方法主要是太阳池自然蒸发，该方法集中利用日照提高卤水温度，加速矿物盐析出，但此法严重依赖自然天气，受日照强度、风雨等因素的影响，对于产量的提高具有一定的局限性，还是没有从根本上改变“靠天吃饭”的状况。
太阳能是一种清洁能源，在日照充足的地区太阳能更为丰富。合理的利用太阳能有助于解决能源短缺的问题。
太阳能光热装置因为结构简单，一般仅需要集热板即可将太阳能转化为热能。且具有转化效率较高，可达60％以上。目前已经开发了多种民用太阳能光热装置，如各种太阳能热水器，取得了较好的效果。
现有的太阳能光热装置，普遍仅能将介质加热到不超过100℃，可以满足低海拔、平均气温较高地区的使用。但是，在高寒高海拔地区并不适用，更无法应用于工业生产。
目前，缺乏一种适用于高原地区使用的太阳能光热装置，无形中增加了利用高原地区丰富太阳能的难度。
在高原地区的各种资源中，锂是极为重要的一种。锂的电化学活动性强，又是轻金属，具有广泛的用途。目前锂的应用领域包括：陶瓷和玻璃、合成橡胶、铝生产、塑料、药品、润滑剂、空调机、电视(荧光屏)、锂电池、锂合金和核工业等；消费量达几万吨/年，且还在不断增长。
在世界锂总资源量中，卤水锂矿约占75％，硬岩锂矿占25％；在我国锂总资源量中，卤水锂矿约占72％，硬岩锂矿占28％。在60年代以前，锂资源主要来自硬盐锂矿石。盐湖的提锂成本较硬岩低1-1.5倍以上，目前从盐湖中生产的锂盐已超过硬岩锂矿，从盐湖卤水中提取锂盐已成为发展大趋势。
由于含锂盐湖水化学类型和经济技术条件不同，所以采用的工艺路线也各不相同。现有技术中从卤水中提锂的方法有：有机离子(TBP，即磷酸三丁酯等)交换树脂法、无机离子交换剂法、铝酸盐法、氯化氢盐析法、铝酸盐法以及沉淀法(即磷酸盐法)和碳法等。但这些方法均存在能耗较高、耗料较多，有的系统选型难，产能低或工艺流程复杂、污染环境等问题。
除此之外，智利阿塔卡玛湖、美国银峰湖等硫酸盐湖采用盐田法进行预浓缩，然后再运至工厂加工；然而由于我国主要的盐湖为碳酸盐湖，上述适于硫酸盐湖的盐田法不适应于我国碳酸型盐湖。上世纪末，我国有专家提出了适于碳酸盐湖中提取锂的盐田法，并实际应用于锂盐的提取。然而实践后发现，该技术存在如下缺点，导致亏损：
1、需要大面积建造盐田，建造成本以及后期维护成本相当大；同时人为大幅增加了盐湖增发量，破坏了盐湖的液位平衡，可能影响盐湖地区的生态；
2、受自然条件影响大；
3、制得的锂盐纯度低，杂质多，需要运至工厂再加工；这样，运输成本非常高；而且其中大部分为运输杂质的“无用运输”；
4、制盐时间长；工艺过程不能实现自动化，效率低。
此外，现有的盐湖基本都处于偏远地带，交通不便，能源、淡水等缺乏，进一步加大了纯化的难度。
为此，需要提供一种改进的从碳酸型盐湖中提取锂盐的方法及系统。
高海拔地区，特别是海拔在4000米以上的高海拔地区，普遍气压低，氧含量低，空气干燥。同时，高原地区的昼夜温差可达30℃以上。恶劣的自然环境环境，水电缺乏对高原地区工业生产与人员生存提出了巨大的挑战，限制了高原资源的开发。
现阶段，未有特别设计的适用于高海拔地区的工业建筑，高海拔地区的工业生产依然以初级的资源采集为主，之后再转移到低海拔等自然条件较好的地区进行后续的精加工。
为了更为有效地开发高海拔地区的资源，有必要开发出一种适用于高海拔地区并兼有资源采集和初步精加工的工业建筑。
发明内容
本发明的一个目的在于提供一种适用于高原地区的高效热能回收利用方法及系统。
本发明的另一个目的在于提供一种碳酸锂的制备方法及系统。
本发明的再一个目的在于提供一种与上述方法和系统配套的适用于高海拔地区的工业建筑。
本发明所采取的技术方案是：
高效热能回收利用方法，包括如下步骤：
1)利用聚光式太阳能光热装置，将导热油加热至120℃以上，备用；
2)通过太阳能光热装置对水箱热端内的液态导热介质和预热池中的卤水进行加热，预热后的卤水导入升温釜；
3)高温热泵从水箱冷端吸热，通过水箱热端向升温釜放热，将升温釜中的卤水加热至所需温度；
4)将升温釜中的卤水导入反应釜内，抽真空进行减压浓缩，将加热后的导热油导入反应釜内的热交换器对反应釜进行快速补热，将反应釜内减压浓缩中产生的蒸汽通过管路导入预热池内的热交换器进行冷却，得到的蒸馏水收集在蒸馏水箱；
5)将反应釜内结晶后的高温上清液通过管路导入冷端结晶釜，水箱冷端通过热交换器与冷端结晶釜进行热交换，将高温上清液冷却，冷却结晶后的常温或低温上清液导入上清液沉淀池；
6)使用导热油对蒸馏水进行加热，并对反应釜内的粗结晶盐进行擦洗，将高温擦洗液导入擦洗液保温釜；
7)必要时使用加热后的蒸馏水或沉淀后的热擦洗液对系统与卤水接触的装置及管路进行冲洗。作为本发明的进一步改进，回收冲洗液中的热能之后将常温冲洗液回湖。
作为本发明的进一步改进，水箱热端和水箱热端内容纳的液态导热介质独立为水、导热油。
适用于高原地区的高效热能回收利用系统，包括：预热池、升温釜、反应釜、冷端结晶釜、擦洗液保温釜和上清液沉淀池；预热池、升温釜、反应釜、冷端结晶釜和蒸馏水箱均设有热交换器，擦洗液保温釜内设有恒温器；预热池设有连接至升 温釜的管路，升温釜设有连接至反应釜的管路，反应釜设有连接至冷端结晶釜和擦洗液保温釜的管路，冷端结晶釜设有连接至上清液沉淀池的管路；
所述系统还设有导热油箱，导热油箱连接有加热导热油的聚光式太阳能光热装置，以及连接至反应釜内的热交换器和蒸馏水箱热交换器的闭合导热油管路；
水箱热端和预热池连接有用于向其供热的太阳能光热装置；
水箱热端和水箱冷端之间设有高温热泵，水箱热端和升温釜之间设有热交换器；水箱冷端与冷端结晶釜之间设有热交换器；
反应釜连接有抽真空装置，抽真空装置设有将蒸汽导入预热池内的热交换器并延伸至蒸馏水箱的管路；蒸馏水箱设有将蒸馏水导入反应釜和擦洗液保温釜的管路。
作为本发明的进一步改进，预热池由至少两个预热池串联而成。
作为本发明的进一步改进，水箱热端连接有用于向其辅助供热的电热加装置。
作为本发明的进一步改进，上述系统中使用的高温热泵具有：
实现热交换产生热水的多点热平衡换热器，其具有冷水输入端，其出口端输出的热水经过水泵和单向阀后接入水箱热端；
热泵压缩机，其压缩输出的冷媒依次经过蒸发器、节流器后提供给多点热平衡换热器，冷媒从多点热平衡换热器输出后又被热泵压缩机吸入循环；
所述的多点热平衡换热器由多组换热器串联而成，各组换热器间设有交叉流道。
作为本发明的进一步改进，多点热平衡换热器的热水出口端设有温度调节阀，温度调节阀的输出连接水泵。
作为本发明的进一步改进，热泵压缩机与蒸发器之间设有气液分离器。
作为本发明的进一步改进，多点热平衡换热器的冷水输入端设有除污仪。
作为本发明的进一步改进，高温热泵使用的冷媒为质量比为R124:R245a:R22＝3：3：1的三元复合冷媒。
可与上述系统配套使用或单独使用的高温聚光式太阳能集热器，包括弧形的聚光式反光板和固定该反光板的支架，反光板的正面固定有透光板，反光板的两端设有端板，反光板、透光板和端板共同形成一个腔，腔内平行方向设有集热管，集热管内设有进液口和出液口。
作为本发明的进一步改进，上述集热器中的集热管外套设有透明的保温管。
作为本发明的进一步改进，上述集热器中的集热管表面为黑色。
作为本发明的进一步改进，上述集热器中的保温管为双层真空玻璃管。
作为本发明的进一步改进，上述集热器中的集热管表面为哑光面。
作为本发明的进一步改进，上述集热器中的支架设有调节反光板转动的转轴。
作为本发明的进一步改进，上述集热器中的转轴设有角度计。
作为本发明的进一步改进，上述集热器中的高温聚光式太阳能集热器设有驱动转轴转动的驱动器。
作为本发明的进一步改进，上述集热器中的反光板底部设有排液口。
作为本发明的进一步改进，上述集热器中的透光板表面设有防静电涂层或导电层。
高纯度碳酸锂的制备方法，包括如下步骤：
1)将碳酸型盐湖卤水浓缩，之后升温使碳酸锂饱和结晶析出，收集结晶得到碳酸锂精盐；
2)用60℃以上卤水蒸发和浓缩时回收的蒸馏水冲洗收集得到的碳酸锂精盐，溶解其中的钠钾盐；
3)干燥得到高纯度碳酸锂。
优选的，通过减压蒸发将盐湖卤水浓缩，之后升温至60℃以上，优选65℃、70℃以上保温使碳酸锂结晶析出。
使用卤水蒸发和浓缩时回收的蒸馏水冲洗碳酸锂精盐至其质量基本保持不变。
作为本发明的进一步改进，在冲洗时，定时切换冲洗方向。
作为本发明的进一步改进，用卤水蒸发和浓缩时回收的蒸馏水进行高纯度碳酸锂的制备，蒸馏水来自卤水蒸发和浓缩时得到的冷凝水。
高纯度碳酸锂的制备系统，系统包括卤水浓缩结晶器和精制器，卤水浓缩结晶器设有储热罐和加热罐，储热罐和加热罐均独立设有热交换装置，储热罐和加热罐的热交换装置分别热泵的吸热端和放热端相连，加热罐设有卤水入口和尾卤排出口，尾卤排出口通过管道连接至储热罐；精制器包括精纯罐，精纯罐设有出水口和入水口，精纯罐内下部设有用于承托碳酸锂结晶的径向滤网。
作为本发明的进一步改进，精纯罐内上部设有防止碳酸锂结晶流出的可拆卸径向滤网。
作为本发明的进一步改进，卤水浓缩结晶器连接有抽真空装置，抽真空装置与水蒸汽冷凝器相连，水蒸汽冷凝器连接有蒸馏水暂存罐。抽真空装置可以将水蒸汽抽出，降低液体表面的压力，有助于加速液体的浓缩。抽出的水蒸汽经过冷凝，副产蒸馏水，特别适用于缺乏纯净水的偏远地区。
作为本发明的进一步改进，卤水蒸发和浓缩时回收的蒸馏水暂存罐设有连接至精纯罐的进水口。
作为本发明的进一步改进，尾卤排出口前设有滤网。
作为本发明的进一步改进，精纯罐的出水口和入水口之间设有循环泵。
作为本发明的进一步改进，精制器设有热交换装置。
作为本发明的进一步改进，加热罐内设有可拆卸的内滤网层。
作为本发明的进一步改进，精纯罐设有热风烘干装置。热风烘干装置可以简单为设置在精纯罐的热风入口和出口。
作为本发明的进一步改进，精纯罐的出水口设有三通阀，三通阀的一端通过管道连接至储热罐。
作为本发明的进一步改进，精纯罐的出水口、入水口前设有滤网。
适用于高海拔地区的工业建筑，包括侧墙，侧墙上固定有顶盖，顶盖为拱形，顶盖设有保温层，顶盖下方被内墙隔离为靠内的生产区及靠外的辅助区，生产区上方设有保温板，辅助区设有沟渠。
作为本发明的进一步改进，上述工业建筑中的沟渠两端连通有蓄水池，蓄水池中的至少一个位于辅助区内。特别的，沟渠两端具有一定的坡度。进一步的沟渠上方设有透气盖板。
作为本发明的进一步改进，上述工业建筑中的辅助区上方的部分顶盖是透光的，辅助区内种植有植物。
作为本发明的进一步改进，上述工业建筑中的蓄水池内设有热交换器。
作为本发明的进一步改进，上述工业建筑中的顶盖下方设有冷凝水收集管。
作为本发明的进一步改进，上述工业建筑中的侧墙设有入口。
作为本发明的进一步改进，上述工业建筑中的生产区设有大门，大门对侧的墙上设有透气窗。
作为本发明的进一步改进，上述工业建筑中的辅助区内设有生活区。
本发明的有益效果是：
本发明的热能利用方法，可以高效回收热能，同时具备快速换热能力和慢速换热能力，满足工业生产对热的不同需求，可广泛应用于各种需要升温、冷却的工业生产过程，特别适用于盐湖矿物盐的提取。
本发明的热能利用系统，可以充分利用高原地区丰富的太阳，高效地回收热能，并为生产提供稳定的供热，满足生产的需要。同时，本发明系统可以副产淡水，进一步满足生产和生活需要。
本发明的热能利用系统，设计合理，使用液体和热泵进行热能交换，使的卤水仅在各种釜内进行结晶，不会使卤水输送管路结垢。利用高温导热油对卤水进行快速补热，可以满足水在减压状态下大量蒸发时所需要的热量，可以实现标准化操作，在有阳光的情况下，约1～2小时即可完成一批卤水的浓缩结晶，在午间热量充足的情况下，10～30min即可完成一批卤水的浓缩结晶，大大加快了卤水的浓缩，便于从卤水中提取各种矿物盐，使得生产更为可控，避免了“靠天吃饭”。
使用多级预热池串联，每个预热池中的卤水量相对减少，结合逆流换热，可以更快地得到温度更高的卤水，同时提高换热效率，满足连续生产的需要。
与使用电阻式加热器对液体进行加热相比，本发明的系统可在相同耗电的前提下提升2～3倍的制热量，同时回收了生产流程中绝大部分热能，实现了高原地区的高效热能回收利用，与大幅减少了高原地区工业化提取装置所需要的能源，大大减少了固定投资量，绿色环保。
本热能利用系统所使用的高温热泵，换热效率高，通过一级热泵即可在高原地区将水箱热端的温度提升85℃，换热效率高。同时，热泵不与腐蚀性强的卤水直接接触，使用寿命长，可以稳定运行。
本发明的高温太阳能集热器，整体全封闭，与外界无空气对流，无对流热损失，光热转化效率高，可以将导热介质加热至200℃以上，满足特殊工业化生产的需要。可以很好地应用于其他介质的加热，如水、防冻液、导热油等的加热。
本发明的高温太阳能集热器，结构简单，易于制造，易于整体安装，不需考虑季节性冻土的施工影响，互换性强，维护方便，可以有效抵挡沙尘、大风、雨雪、紫外线引起的设备老化等不利自然条件，特别适用于高原地区。
本发明的碳酸锂提纯工艺，无需要使用化学试剂，通过物理操作即可以完成碳酸锂的精纯，精纯后的碳酸锂纯度高达95％以上，有助于减少后期的运输成本成进一步提纯的成本。本发明工艺，对运输的要求极低，同时也不会污染环境。
本发明的碳酸锂提纯工艺，可以充分回收利用盐湖卤水蒸发、浓缩时所产生的水蒸汽，并将其冷凝为纯净的蒸馏水。蒸馏水在使用之后，可以重新进入盐湖，有效地向盐湖补水，避免盐湖水位下降而引起的生态问题。
利用抽真空装置，在加速卤水浓缩的同时可以通过冷凝水蒸汽副产蒸馏水。得到的蒸馏水可以进一步用于碳酸锂精盐的提纯。有效地解决了偏远的盐湖地区缺少淡水(蒸馏水)的问题，进一步降低了纯化的成本。蒸馏水在使用之后，可以重新进入盐湖，有效地向盐湖补水，避免或减少因盐湖水位下降而引起的生态问题。
本发明的碳酸锂提纯系统，使用方便，可以制备得到高纯度的碳酸锂。同时，可在储热罐中副产钠钾盐。
本发明的碳酸锂提纯系统，无需额外补充化学制剂，能源利用率高。
本发明的工业建筑，拱形顶盖自上而下延伸到侧墙，覆盖整个生产区和辅助区，具有较好的密闭性，大大减少了内部保温材料的使用，同时减少内部保温设计的难度。本发明的工业建筑，可以很好地保留水气和热量，具有极好地保温、保湿性，有助于提高建筑内的空气湿度和温度，使人感觉更为舒适。同时，生产区上方额外设有保温板，可有效减少热量从顶部散失，大幅降低了昼夜温差过大对设备带来的不利影响。湿度的提高，也有利于减少建筑内的扬尘，同时有效避免了静电累积，有利于安全生产。
本发明的工业建筑，整体的风阻较小，具有极好的抗风性。可以保证积雪可以顺着顶盖更快滑下，避免过多累积，具有更好的耐暴风雪性，可以满足高海拔地区的特殊要求。
本发明的工业建筑可以实现模块化设计，易于原地组装，大大减少了施工难度，提高了施工效率。
沟渠内可添加水或盐湖卤水，白天，水在热的作用下蒸发，提高辅助区的湿度，为生活区的人员提供更为舒适的生活、工作环境。夜间，可以在沟渠内通入温度较高的液体，进一步减少建筑内外的温差。温度较高的液体可以是白天生产并储存在蓄水池内的液体。在盐湖地区，沟渠可以进一步用于对盐湖卤水进行初步的升温、浓缩处理，减少能耗。特别的，当沟渠两端具有一定的坡度时，可以使其中的盐结晶进一步集中在底部，便于收集。
辅助区种植的植物可以利用生产、生活过程中所产生的冷凝水进行生长，同时释放出足够的氧气，更好地为生活区供氧，改善空气质量，营造较为适宜人居的生态环境。
生产区产生巨量的初级冷凝水可部分为生活区提供纯净的约60℃的生活淡水及医用纯净水原料，可解决当地人员长期以来的医疗卫生难题。
因厂房长期的空气冷凝水进入土壤，持续湿润周围的土壤，为厂房周围的植物生长提取必需的水分，进一步改善建筑周围的小环境。
蓄水池内设有热交换器，可以将白天富余的热能储存起来，待夜晚温度下降时为建筑内供热。
附图说明
图1是本发明热回收利用系统的结构示意图；
图2是本发明热回收利用系统高温热泵的结构示意图；
图3是本发明热回收利用系统多点热平衡换热器的结构示意图；
图4和图5是本发明集热器的结构示意图；
图6是本发明高纯度碳酸锂制备系统浓缩结晶器的结构示意图；
图7是本发明高纯度碳酸锂制备系统精制器的结构示意图；
图8是本发明工业建筑的截面结构示意图；
图9是本发明工业建筑的平面结构示意图。
具体实施方式
高效热能回收利用方法，包括如下步骤：
1)利用聚光式太阳能光热装置，将导热油加热至120℃以上，备用；
2)通过太阳能光热装置对水箱热端内的液态导热介质和预热池中的卤水进行加热，预热后的卤水导入升温釜；
3)高温热泵从水箱冷端吸热，通过水箱热端向升温釜放热，将升温釜中的卤水加热至所需温度；
4)将升温釜中的卤水导入反应釜内，抽真空进行减压浓缩，将加热后的导热油导入反应釜内的热交换器对反应釜进行快速补热，将反应釜内减压浓缩中产生的蒸汽通过管路导入预热池内的热交换器进行冷却，得到的蒸馏水收集在蒸馏水箱；
5)将反应釜内结晶后的高温上清液通过管路导入冷端结晶釜，水箱冷端通过热交换器与冷端结晶釜进行热交换，将高温上清液冷却，冷却结晶后的常温或低温上清液导入上清液沉淀池；
6)使用导热油对蒸馏水进行加热，并对反应釜内的粗结晶盐进行擦洗，将高温擦洗液导入擦洗液保温釜；
7)必要时使用加热后的蒸馏水或沉淀后的热擦洗液对系统与卤水接触的装置及管路进行冲洗，回收冲洗液中的热能之后将常温冲洗液回湖。
为了更为快速地供热，使用聚光式太阳能光热装置将导热油加热至120℃以上，优选加热至150℃以下，更佳的，加热至200℃以上。
水箱热端需要与升温釜换热，加热升温釜内的卤水，液态导热介质的温度一般在70～80℃。为获得更好的加热效果，要求水箱热端内的液态导热介质具有更高的温度。水的价格低廉，安全性较高，无污染，但是其沸点较低；导热油的价格较高，沸点高，安全性好，但是其比热容较低。根据具体的应用需要，液态导热介质可以选择水或导热油，或其他的液态导热介质。
水箱冷端需要与冷端结晶釜换热，介质温度一般不超过40℃。使用比热容高、低成本和高安全性的水作为导热介质更为经济实用。当然，如有特殊要求，也可以采用导热油或其他液态导热介质。
下面结合附图，进一步说明本发明的热能回收利用系统。
参照图1～3，适用于高原地区的高效热能回收利用系统，包括预热池1、升温釜8、反应釜2、冷端结晶釜4、擦洗液保温釜3和上清液沉淀池5；预热池1、升温釜8、反应釜2、和冷端结晶釜4内均设有热交换器，擦洗液保温釜3内设有恒温器；预热池1设有连接至升温釜8的管路，升温釜8设有连接至反应釜2的管路，反应釜2设有连接至冷端结晶釜4和擦洗液保温釜3的管路，冷端结晶釜4设有连接至上清液沉淀池5的管路，
所述系统还设有导热油箱60，导热油箱60连接有加热导热油的聚光式太阳能光热装置，以及连接至反应釜内的热交换器和蒸馏水箱热交换器的闭合导热油管路；
水箱热端61和预热池1连接有用于向其供热的太阳能光热装置；
水箱热端61和水箱冷端62之间设有高温热泵，水箱热端61和升温釜1之间设有热交换器；水箱冷端62与冷端结晶釜4之间设有热交换器；
反应釜2连接有抽真空装置21，抽真空装置21设有将蒸汽导入预热池1内的热交换器并延伸至蒸馏水箱22的管路；蒸馏水箱22设有将水导入蒸馏水加热器并延伸至反应釜2和擦洗液保温釜3的管路。
作为本发明的进一步改进，预热池由至少两个预热池串联而成。不同的预热池之间相对独立，可以对其中容纳的卤水进行逐级加热，保证预热末端的卤水可以较快达到所需要的温度。
作为本发明的进一步改进，水箱热端连接有用于向其辅助供热的电热加装置。通过使用辅助供热装置，可以将富余的电力转化为热能，加速生产。同时也避免了直接加热卤水导致加热装置结垢，影响加热效率。
作为本发明的进一步改进，上述系统中使用的高温热泵7具有：
实现热交换产生热水的多点热平衡换热器71，其具有冷水输入端，其出口端输出的热水经过水泵713和单向阀714后接入水箱热端61；
热泵压缩机72，其压缩输出的冷媒依次经过蒸发器721、节流器722后提供给多点热平衡换热器71，冷媒从多点热平衡换热器71输出后又被热泵压缩机72吸入循环；
所述的多点热平衡换热器71由多组换热器715串联而成，各组换热器715间设有交叉流道716。
作为本发明的进一步改进，多点热平衡换热器71的热水出口端设有温度调节阀717，温度调节阀717的输出连接水泵713。
作为本发明的进一步改进，热泵压缩机72与蒸发器721之间设有气液分离器723。
作为本发明的进一步改进，多点热平衡换热器71的冷水输入端设有除污仪718。
作为本发明的进一步改进，高温热泵使用的冷媒为质量比为R124:R245a:R22＝3：3：1的三元复合冷媒。该复合冷媒的排气压力在23～24公斤，回气压力在2～3公斤，冷凝温度在115～120℃，在海拔3500～4500米保证热水温度最高达到85℃，满足高原工业化生产应用。
下面结合从盐湖中提取碳酸锂，进一步说明本发明方法和系统。
高效热能回收利用提取碳酸锂的方法，包括如下步骤：
1)利用聚光式太阳能光热装置，将导热油加热至200℃以上，备用；
2)通过太阳能光热装置以及辅可选的辅助电加热装置将水箱热端内的水加热至80℃以上，同时将预热池中的卤水进行预热，将预热后的卤水导入升温釜；
3)将水箱热端内的热水循环导入升温釜内的换热盘管，将升温釜中的卤水加热至70℃以上；
4)将升温釜中的温度达70℃以上卤水导入反应釜内，抽真空进行减压浓缩，同时将加热后的导热油导入反应釜内的热交换器对反应釜进行快速补热，保证卤水可以持续快速沸腾，快速蒸发浓缩；将减压浓缩中产生的蒸汽通过管路导入预热池内的热交换器进行冷却，释放出的热先对二级预热池(高温)进行加热，冷凝后的热水导入一级预热池(低温)的换热器，这样通过逆流换热，使得卤水与蒸汽(热水)之间保持较大的温差，既可以将二级预热温中的卤水有效地预热，又可以充分回收蒸汽中的潜热；得到的蒸馏水收集在蒸馏水箱，备用；
5)将反应釜内结晶后的高温上清通过管路导入冷端结晶釜，将水箱冷端内的液态导热介质循环导入冷端结晶釜内的换热盘管，将冷端结晶釜内的高温上清液冷却，温度降低后，上清液中的盐饱和结晶，得到K、Na盐；冷却结晶后的常温或低温上清液导入上清液沉淀池，进行进一步的回收处理或补充至盐湖中，减少其对盐湖生态的破坏；
6)使用导热油对蒸馏水进行加热，使用加热后的蒸馏水对沉积在反应釜内的碳酸锂粗结晶盐进行擦洗，溶解其中的K、Na盐，收集擦洗液导入擦洗液保温釜，保温沉降，进一步回收其中的碳酸锂；收集、干燥反应釜内的碳酸锂结晶；
7)当设备运行一段时间后，使用加热后的蒸馏水或擦洗液保温釜内的上清液对系统与卤水接触的装置和管路进行冲洗，冼去管路中、反应釜、擦洗液保温釜内因为长期运行而生成的盐垢，回收冲洗液中的热能之后将冲洗液回湖。
按上述生产工艺，约1～2小时即可完成一批卤水的浓缩结晶，在午间热量充足的情况下，10～30min即可完成一批卤水的浓缩结晶。按一天8～10小时的工作时间计算，当天即可完成多批卤水的浓缩结晶，收集得到的碳酸锂可以统一集中在擦洗液保温釜内保温过夜，待晶体长大后继续后处理得到纯度高达90％以上的碳酸锂结晶，完全摆脱了“靠天吃饭”的传统生产工艺。
本发明热能回收利用方法及系统，可以回收利用系统中近60～70％的热能，可以使配套的太阳能光伏发电电站的装机容量降低至原装机容量的25～33％，大幅减少了固定投资。
试验数据表明，在海拔3700以上的高原地区，采用聚光式太阳能光热装置，一般在上午10：00左右即可达到100℃以上的温度，直至18：30左右，其温度依然可以保护在120℃以上，完全可以实现工业化生产，彻底改变了现有盐湖的生产 工艺。
下面结合附图，进一步说明本发明的高温聚光式太阳能集热器。
参照图4和图5，高温聚光式太阳能集热器，包括弧形的聚光式反光板A1和固定该反光板A1的支架A2，反光板A1的正面固定有透光板A3，反光板A1的两端设有端板A4，反光板A1、透光板A3和端板A4共同形成一个腔，腔内平行方向设有集热管A5，集热管A5内设有进液口和出液口。
弧形聚光式反光板整体呈槽形，所谓平行方向为与反光板的轴线方向。这样不同角度照射进来的阳光基本可以聚焦在一条直线上，无需频繁调节反光板的角度，有利于减少设备维护。
作为本发明的进一步改进，上述集热器中的集热管A5外套设有透明的保温管A6。保温管既可以透光，又可以阻隔空气对流。这样可以进一步减少集热管与外部环境间的热交换，提高光热转换效率。
作为本发明的进一步改进，上述集热器中的集热管表面为黑色。黑色表面可以更为充分吸收各种光，提高光热转换效率。
作为本发明的进一步改进，上述集热器中的保温管为双层真空玻璃管。双层真空玻璃管的透光性、保温性能良好，更有助于提高光热转换效率。
作为本发明的进一步改进，上述集热器中的集热管表面为哑光面。哑光面可以进一步减少光反射，进而提高光热转换效率。
作为本发明的进一步改进，上述集热器中的支架A2设有调节反光板A1转动的转轴A21，方便在太阳照射角度改变过大的情况下进行调整。
作为本发明的进一步改进，上述集热器中的转轴设有角度计，便于快速准确的调整。
作为本发明的进一步改进，上述集热器中的高温聚光式太阳能集热器设有驱动转轴转动的驱动器，以利于自动化调控。
作为本发明的进一步改进，上述集热器中的反光板底部设有排液口A11，既可以持腔内外的压力平衡，也避免腔内积水。
作为本发明的进一步改进，上述集热器中的透光板表面设有防静电涂层或导电层A31，将表面的静电消除，防止表面吸附灰尘影响透光。
使用时，将导热液通过进液口导入，出液口导出即可。必要时，可以将多个集热器串联，以获得更高的温度，也可以通过调整进液的速度来调整导热液的温度。方便获得所需要的温度。
高纯度碳酸锂的制备方法，包括如下步骤：
1)将碳酸型盐湖卤水浓缩，之后升温使碳酸锂饱和结晶析出，收集结晶得到碳酸锂精盐；
2)用60℃以上卤水蒸发和浓缩时回收的蒸馏水冲洗收集得到的碳酸锂精盐，溶解其中的钠钾盐；
3)干燥得到高纯度碳酸锂。
优选的，通过减压蒸发将盐湖卤水浓缩，之后升温至60℃以上，优选65℃、70℃以上保温使碳酸锂结晶析出。结晶时的温度越高，越有利于析出更高纯度的碳酸锂精盐，有利于减少后续纯化操作的难度。
使用蒸馏水冲洗碳酸锂精盐至其质量减少至无明显减少时。一般而言，碳酸锂精盐在冲洗到质量减少至其原质量(干重)的20～30％时，其质量基本稳定，并不会因为继续冲冼1～2小时而显著降低。在这种情况下，继续冲洗的意义并不能显著提高终产品高纯度碳酸锂的纯度，可以停止冲洗，以节约水和其他能源，同时提高生产效率。
作为本发明的进一步改进，在冲洗时，定时切换冲洗方向。如每隔10秒、20秒变更一下冲洗方向，更有利于提高冲洗效率，同时防止结晶堵塞滤网。
蒸馏水来自卤水浓缩或蒸发时得到的冷凝水。
参照图6和图7，高纯度碳酸锂的制备系统，包括卤水浓缩结晶器和精制器，卤水浓缩结晶器设有储热罐B1和加热罐B2，储热罐B1和加热罐B2均独立设有热交换装置B41，储热罐B1和加热罐B2的热交换装置分别与热泵B4的吸热端和放热端相连，加热罐B2设有卤水入口B21和尾卤排出口B22，尾卤排出口B22通过管道连接至储热罐B1；精制器包括精纯罐B3，精纯罐设有出水口B32和入水口B31，精纯罐B3内下部设有用于承托碳酸锂结晶的径向滤网B33。
作为本发明的进一步改进，精纯罐B3内上部设有防止碳酸锂结晶流出的可拆卸径向滤网B34。
作为本发明的进一步改进，卤水浓缩结晶器连接有抽真空装置B5，抽真空装置B5与水蒸汽冷凝器相连，水蒸汽冷凝器连接有蒸馏水暂存罐B6。抽真空装置可以将水蒸汽抽出，降低液体表面的压力，有助于加速液体的浓缩。抽出的水蒸汽经过冷凝，副产蒸馏水，特别适用于缺乏纯净水的偏远地区。
作为本发明的进一步改进，蒸馏水暂存罐B6设有连接至精纯罐的进水口B31。当然的，为了提高精纯的效率，在将蒸馏水导入精纯罐前可以将蒸馏水预热至所需温度。进一步的，精制器设有热交换器B41，以保证罐内的温度在冲洗时保持稳定。热交换器B41既可以设置在精纯罐内，也可以设置在外部的管路中或循环泵，更佳地可设置在蒸馏水储罐内，或同时在多个位置设置，保证冲洗时蒸馏水的温度保持在所需的温度。
作为本发明的进一步改进，尾卤排出口前设有滤网，这样可以避免在排出尾卤时，将碳酸锂结晶精盐带出，影响得率。
作为本发明的进一步改进，加热罐内设有可拆卸的内滤网层。这样可以保证绝大部分碳酸锂结晶都沉积于滤网中，可以方便地将得到的碳酸锂取出。取出的碳酸锂可以转移至精纯罐进一步纯化。
作为本发明的进一步改进，精纯罐的出水口B32和入水口B31之间设有循环泵B7。这样可以将热水循环冲洗碳酸锂结晶精盐，加快纯化进程。循环泵排出的水优选从底部向上冲洗碳酸锂结晶精盐，这样可以避免结晶沉积，底部结晶难以冲洗到，影响纯化效果。当然，也可以采用其他冲洗方式，如从上往下冲洗，旋转冲洗等，或多种冲洗方式相结合。
作为本发明的进一步改进，精纯罐设有热风烘干装置。热风烘干装置可以简单为设置在精纯罐的热风入口和出口。热风优选从碳酸锂结晶的底部吹入，从上部吹出，这样可以更快地将纯化后的碳酸锂干燥。
作为本发明的进一步改进，精纯罐的出水口设有三通阀，三通阀的一端通过管道连接至储热罐。三通阀可以方便地根据需要控制水的流向。冲洗完毕的热水导入储热罐中，之后使用热泵利用其中的余热，有助于提高能源的利用率，特别适用于偏远地区。
作为本发明的进一步改进，精纯罐的出水口、入水口前设有滤网。这样有助于防止结晶进入管路，影响设备正常运行和碳酸锂的得率。
实施例1：
Li离子浓度1.29g/L卤水，60℃以上增发结晶析出粗锂盐与卤水混合湿盐，简单去除上清液后称重897.6g，用80℃蒸馏水3000g一次性混合后充分搅拌3分钟，经抽滤及烘干，得到纯度为62％的碳酸锂47.4g，从粗锂盐中得到碳酸锂收率为73.5％。
实施例2：
Li离子浓度1.29g/L卤水，60℃以上增发结晶析出粗锂盐与卤水混合湿盐，简单去除上清液后称重877.9g，用70℃蒸馏水2250g，分别以1200g、600g、300g、150g共计4次以实施例1方式冲洗，每次充分搅拌30秒共计2分钟，经抽滤及烘干后得到干燥的纯度为91.3％的碳酸锂37.56g，从粗锂盐中得到碳酸锂收率为85.7％。
实施例3：
Li离子浓度1.29g/L卤水，60℃以上增发结晶析出粗锂盐与卤水混合湿盐，简单去除上清液后称重986.7g，置于精纯罐内，加入90℃蒸馏水1800g，每10秒改变一次方向反复循环1分钟，通入热空气吹干后得到干燥的纯度为97.6％的碳酸锂39.74g，从粗锂盐中得到碳酸锂收率为96.97％。
由上述实施例的数据可知，精纯罐可以快速、省水持续进行碳酸锂精盐的提纯环节。变化方向进行冲洗，既可以提高冲洗效率，也避免了管路或精纯罐内累积结晶，可以实现自清洁，方便设备的使用，也有助于减少维护。
该环节对碳酸锂粗盐的提纯操作时间，缩减到了传统方法的三分之一；自清洁的设计免除了传统擦洗方式必须频繁维护的弊病；所用冲洗蒸馏水的量缩减到了传统方法的60％，并且避免了碳酸锂在传统工艺中的系统性损失，获得了品位97％以上，收率96％以上的纯度特别好的碳酸锂产品。
下面结合附图，进一步说明本发明的适用于高海拔地区的工业建筑。
参照图8和9，适用于高海拔地区的工业建筑，包括侧墙C1，侧墙C1上固定有顶盖C2，顶盖C2为拱形，顶盖C2设有保温层，顶盖C2下方被内墙C3隔离为靠内的生产区C4及靠外的辅助区C5，生产区C4上方设有保温板C43，辅助区C5设有沟渠C6。内墙优选由承重柱和保温隔音板组成。
优选的，生产区的部分顶盖可以透光，对应地，其下方的保温板也为透光的，这样可以充分地利用自然光，进一步减少能耗。为了方便散热，顶盖上可设有数个可启闭的排气窗。
拱形顶盖也可以根据需要相互拼接，并联得到更大的生产区。这样可以方便根据需要调整建筑的总体大小，满足不同生产规模的需要。也可以方便地随生产规模的扩大而扩建，满足不同时期生产的需要。
作为本发明的进一步改进，上述工业建筑中的沟渠C6两端连通有蓄水池C61，蓄水池C61中的至少一个位于辅助区C5内。特别的，沟渠C6两端具有一定的坡度。
进一步的，沟渠上方设有透气盖板。透气盖板既不会影响水气的散发，又可以避免过多尘土、杂物进入沟渠。
作为本发明的进一步改进，上述工业建筑中的辅助区上方的部分顶盖是透光的，辅助区内种植有植物。种植的植物优选在夜间可以释放氧气，这样可以避免植物在夜间过多消耗氧气，影响空气质量。
作为本发明的进一步改进，上述工业建筑中的蓄水池内设有热交换器。热交换器可以将多余的热量储存起来，方便维持建筑内夜间的温度。
作为本发明的进一步改进，上述工业建筑中的顶盖下方设有冷凝水收集管。冷凝水收集管的出水口设置在植物区，充分利用水资源，为植物生长提供充足的水分。
作为本发明的进一步改进，上述工业建筑中的侧墙设有入口。这样可以方便人们进出，也可以根据需要打开入口，加强辅助区的空气流通。
作为本发明的进一步改进，上述工业建筑中的生产区设有大门C41，大门C41对侧的墙上设有透气窗。这样，当生产区的温度过高时，可以很快地通过空气对流进行散热，快速调节生产区的温度。
作为本发明的进一步改进，上述工业建筑中的辅助区内设有生活区。生活区内可以设置各种有助于改善改善高原艰苦环境的各种生活设施。
本发明的工业建筑，具有极好地保温、保湿性，基本上可以将生产过程中产生的水分保留，提高建筑内的空气湿度，使人感觉更为舒适。同时，生产区上方额外设有保温板，可有效减少热量从顶部散失，大幅降低了昼夜温差过大对设备带来的不利影响。湿度的提高，也有利于减少建筑内的扬尘，同时有效避免了静电累积，有利于安全生产。本发明的工业建筑，整体的风阻较小，具有极好的抗风性。拱形顶盖可以保证积雪可以更快滑下，避免过多累积，具有更好的耐暴风雪性，可以满足高海拔地区的特殊要求。
本发明的工业建筑可以实现模块化设计，易于原地组装，大大减少了施工难度，提高了施工效率。
沟渠内可添加水或盐湖卤水，白天，水在热的作用下蒸发，提高辅助区的湿度，为生活区的人员提供更为舒适的生活、工作环境。夜间，可以在沟渠内通入温度较高的液体，进一步减少建筑内外的温差。温度较高的液体可以是白天生产并储存在蓄水池内的液体。在盐湖地区，沟渠可以进一步用于对盐湖卤水进行初步的升温、浓缩处理，减少能耗。特别的，当沟渠两端具有一定的坡度时，可以使其中的盐结晶进一步集中在底部，便于收集。
辅助区种植的植物可以利用生产、生活过程中所产生的冷凝水进行生长，同时释放出足够的氧气，更好地为生活区供氧，改善空气质量，营造较为适宜人居的生态环境。
生产区产生巨量的初级冷凝水可部分为生活区提供纯净的约60℃的生活淡水及医用纯净水原料，可解决当地人员长期以来的医疗卫生难题。
因厂房长期的空气冷凝水进入土壤，持续湿润周围的土壤，为厂房周围的植物生长提取必需的水分，进一步改善建筑周围的小环境。
蓄水池内设有热交换器，可以将白天富余的热能储存起来，待夜晚温度下降时为建筑内供热。在生产检修时，更能充分地储存热能，减少不必要的浪费。

Claims (41)

  1. 高效热能回收利用方法，包括如下步骤：
    1)利用聚光式太阳能光热装置，将导热油加热至120℃以上，备用；
    2)通过太阳能光热装置对水箱热端内的液态导热介质和预热池中的卤水进行加热，预热后的卤水导入升温釜；
    3)高温热泵从水箱冷端吸热，通过水箱热端向升温釜放热，将升温釜中的卤水加热至所需温度；
    4)将升温釜中的卤水导入反应釜内，抽真空进行减压浓缩，将加热后的导热油导入反应釜内的热交换器对反应釜进行快速补热，将反应釜内减压浓缩中产生的蒸汽通过管路导入预热池内的热交换器进行冷却，得到的蒸馏水收集在蒸馏水箱；
    5)将反应釜内结晶后的高温上清液通过管路导入冷端结晶釜，水箱冷端通过热交换器与冷端结晶釜进行热交换，将高温上清液冷却，冷却结晶后的常温或低温上清液导入上清液沉淀池；
    6)使用导热油对蒸馏水进行加热，并对反应釜内的粗结晶盐进行擦洗，将高温擦洗液导入擦洗液保温釜；
    7)必要时使用加热后的蒸馏水或沉淀后的热擦洗液对系统与卤水接触的装置及管路进行冲洗。
  2. 根据权利要求1所述的高效热能回收利用方法，其特征在于：水箱冷端和水箱热端的液态导热介质独立为水或导热油。
  3. 适用于高原地区的高效热能回收利用系统，包括：预热池、升温釜、反应釜、冷端结晶釜、擦洗液保温釜和上清液沉淀池；预热池、升温釜、反应釜、冷端结晶釜和蒸馏水箱均设有热交换器，擦洗液保温釜内设有恒温器；预热池设有连接至升温釜的管路，升温釜设有连接至反应釜的管路，反应釜设有连接至冷端结晶釜和擦洗液保温釜的管路，冷端结晶釜设有连接至上清液沉淀池的管路，其特征在于：
    所述系统还设有导热油箱，导热油箱连接有加热导热油的聚光式太阳能光热装置，以及连接至反应釜内的热交换器和蒸馏水箱热交换器的闭合导热油管路；
    水箱热端和预热池连接有用于向其供热的太阳能光热装置；
    水箱热端和水箱冷端之间设有高温热泵，水箱热端和升温釜之间设有热交换器；水箱冷端与冷端结晶釜之间设有热交换器；
    反应釜连接有抽真空装置，抽真空装置设有将蒸汽导入预热池内的热交换器并延伸至蒸馏水箱的管路；蒸馏水箱设有将蒸馏水导入反应釜和擦洗液保温釜的管路。
  4. 根据权利要求3所述的高效热能回收利用系统，其特征在于：预热池由至少两个预热池串联而成。
  5. 根据权利要求3或4所述的高效热能回收利用系统，其特征在于：水箱热端连接有用于向其辅助加热装置。
  6. 根据权利要求3～5任意一项所述的高效热能回收利用系统，其特征在于：所述的高温热泵具有：
    实现热交换产生热水的多点热平衡换热器，其具有冷水输入端，其出口端输出的热水经过水泵和单向阀后接入水箱热端；
    热泵压缩机，其压缩输出的冷媒依次经过蒸发器、节流器后提供给多点热平衡换热器，冷媒从多点热平衡换热器输出后又被热泵压缩机吸入循环；
    所述的多点热平衡换热器由多组换热器串联而成，各组换热器间设有交叉流道。
  7. 根据权利要求6所述的高效热能回收利用系统，其特征在于：所述的多点热平衡换热器的热水出口端设有温度调节阀，温度调节阀的输出连接水泵。
  8. 根据权利要求6或7所述的高效热能回收利用系统，其特征在于：所述的热泵压缩机与蒸发器之间设有气液分离器。
  9. 根据权利要求6～8任意一项所述的高效热能回收利用系统，其特征在于：所述的多点热平衡换热器的冷水输入端设有除污仪。
  10. 根据权利要求6～9任意一项所述的高效热能回收利用系统，其特征在于：所述的高温热泵使用的冷媒为质量比为R124:R245a:R22＝3：3：1的三元复合冷媒。
  11. 根据权利要求3～10任意一项所述的高效热能回收利用系统，其特征在于：聚光式太阳能光热装置为高温聚光式太阳能集热器，包括弧形的聚光式反光板和固定该反光板的支架，所述反光板的正面固定有透光板，反光板的两端设有端板，反光板、透光板和端板共同形成一个腔，腔内平行方向设有集热管，集热管内设有进液口和出液口。
  12. 根据权利要求11所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的集热管外套设有透明的保温管。
  13. 根据权利要求11或12所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的集热管表面为黑色。
  14. 根据权利要求11～13任意一项所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的集热管表面为哑光面。
  15. 根据权利要求11～14任意一项所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的保温管为双层真空玻璃管。
  16. 根据权利要求11～15任意一项所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的支架设有调节反光板转动的转轴。
  17. 根据权利要求11～16任意一项所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的转轴设有角度计。
  18. 根据权利要求16或17所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器设有驱动转轴转动的驱动器。
  19. 根据权利要求11～18任意一项所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的反光板底部设有排液口。
  20. 根据权利要求11～19任意一项所述的高效热能回收利用系统，其特征在于：所述高温聚光式太阳能集热器的透光板表面设有防静电涂层或导电层。
  21. 高纯度碳酸锂的制备方法，包括如下步骤：
    1)将碳酸型盐湖卤水浓缩，之后升温使碳酸锂饱和结晶析出，收集结晶得到碳酸锂精盐；
    2)用60℃以上的蒸馏水冲洗收集得到的碳酸锂精盐，溶解其中的钠钾盐；
    3)干燥得到高纯度碳酸锂；
    其中，所使用的热能和蒸馏水按权利要求1～3任意一项所述的方法制备得到，或由权利要求3～20任意一项所述的高效热能回收利用系统。
  22. 根据权利要求21所述的制备方法，其特征在于：蒸馏水来自卤水蒸发和浓缩时回收的冷凝水。
  23. 根据权利要求21或22所述的制备方法，其特征在于：使用蒸馏水冲洗碳酸锂精盐至其质量无明显减少时，停止冲洗。
  24. 根据权利要求21～23任意一项所述的制备方法，其特征在于：冲洗收集得到的碳酸锂精盐时，定时切换冲洗方向。
  25. 高纯度碳酸锂的制备系统，其特征在于：所述系统包括卤水浓缩结晶器和精制器，卤水浓缩结晶器设有储热罐和加热罐，储热罐和加热罐均独立设有热交换装置，储热罐和加热罐的热交换装置分别热泵的吸热端和放热端相连，加热罐设有卤水入口和尾卤排出口，尾卤排出口通过管道连接至储热罐；精制器包括精纯罐，精纯罐设有出水口和入水口，精纯罐内下部设有用于承托碳酸锂结晶的径向滤网。
  26. 根据权利要求25所述的制备系统，其特征在于：精纯罐内上部设有防止碳酸锂结晶流出的可拆卸径向滤网。
  27. 根据权利要求25或26所述的制备系统，其特征在于：卤水浓缩结晶器连接有抽真空装置，抽真空装置与水蒸汽冷凝器相连，水蒸汽冷凝器连接有蒸馏水暂存罐。
  28. 根据权利要求25～27所述的制备系统，其特征在于：精纯罐的出水口和入水口之间设有循环泵。
  29. 根据权利要求25～28任意一项所述的制备系统，其特征在于：精制器设有热交换装置。
  30. 根据权利要求25～29任意一项所述的制备系统，其特征在于：精纯罐设有热风烘干装置。
  31. 根据权利要求25～30任意一项所述的制备系统，其特征在于：精纯罐的出水口设有三通阀，三通阀的一端通过管道连接至储热罐。
  32. 适用于高海拔地区的工业建筑，包括侧墙，侧墙上固定有顶盖，其特征在于：所述顶盖为拱形，顶盖设有保温层，顶盖下方被内墙隔离为靠内的生产区及靠外的辅助区，生产区上方设有保温板，辅助区设有沟渠，生产区内容纳有权利要求25～31任意一项所述的制备系统。
  33. 根据权利要求32所述的适用于高海拔地区的工业建筑，其特征在于：所述沟渠两端连通有蓄水池，蓄水池中的至少一个位于辅助区内。
  34. 根据权利要求32或33所述的适用于高海拔地区的工业建筑，其特征在于：所述：辅助区上方的部分顶盖是透光的，辅助区内种植有植物。
  35. 根据权利要求32～34任意一项所述的适用于高海拔地区的工业建筑，其特征在于：所述沟渠上方设有透气盖板。
  36. 根据权利要求32～35任意一项所述的适用于高海拔地区的工业建筑，其特征在于：所述蓄水池内设有热交换器。
  37. 根据权利要求32～36任意一项所述的适用于高海拔地区的工业建筑，其特征在于：所述沟渠两端具有一定的坡度。
  38. 根据权利要求32～37任意一项所述的适用于高海拔地区的工业建筑，其特征在于：所述顶盖下方设有冷凝水收集管。
  39. 根据权利要求32～38任意一项所述的适用于高海拔地区的工业建筑，其特征在于：所述生产区设有大门，大门对侧的墙上设有透气窗。
  40. 根据权利要求32～39任意一项所述的适用于高海拔地区的工业建筑，其特征在于：所述侧墙设有入口。
  41. 根据权利要求32～40任意一项所述的适用于高海拔地区的工业建筑，其特征在于：所述辅助区内设有生活区。
PCT/CN2014/086344 2013-09-13 2014-09-12 高效热能回收利用方法、系统及基于其的高纯碳酸锂制备方法及系统 Ceased WO2015035929A1 (zh)

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