WO2021169324A1 - 一种节能零排放低温常压蒸发结晶***及其工作方法 - Google Patents

一种节能零排放低温常压蒸发结晶***及其工作方法 Download PDF

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WO2021169324A1
WO2021169324A1 PCT/CN2020/121316 CN2020121316W WO2021169324A1 WO 2021169324 A1 WO2021169324 A1 WO 2021169324A1 CN 2020121316 W CN2020121316 W CN 2020121316W WO 2021169324 A1 WO2021169324 A1 WO 2021169324A1
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chamber
heat exchanger
condensing
evaporation
evaporation chamber
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PCT/CN2020/121316
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English (en)
French (fr)
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王晓龙
郜时旺
刘练波
许世森
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中国华能集团清洁能源技术研究院有限公司
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Publication of WO2021169324A1 publication Critical patent/WO2021169324A1/zh

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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
    • 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

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  • the invention belongs to the technical field of zero discharge of high-concentration brine, and specifically relates to an energy-saving zero-discharge low-temperature atmospheric pressure evaporation crystallization system and a working method thereof.
  • Fresh water is the material basis for human survival. With the development of industrial civilization, the problem of high-concentration salt water discharged from seawater desalination and industrial production is becoming more and more serious. Evaporative concentration of solution is an important way to solve this problem.
  • Traditional solution concentration methods include multi-stage flash evaporation, multi-effect evaporation, reverse osmosis and other methods. The process of multi-stage flash evaporation and multi-effect evaporation needs to consume a lot of steam; the reverse osmosis method needs to consume high-quality electric energy, and the operation and maintenance are complicated, and the cost is high.
  • the traditional solution concentration method concentrates the salinity of the solution to over 6% and then discharges it directly into the environment, ignoring the impact of high-salinity solutions on the ecological environment of the surrounding seas in the long run. It can be seen that the traditional solution concentration method has high energy consumption and high pollution, and it is of great significance to develop a solution concentration process with low energy consumption, low cost and zero pollution emission.
  • the purpose of the present invention is to provide an energy-saving zero-emission low-temperature atmospheric pressure evaporative crystallization system and its working method.
  • the system design is reasonable and realizes the concentrated crystallization of concentrated brine and the collection of condensate. And zero discharge treatment of high concentration brine under normal temperature and pressure.
  • the invention discloses an energy-saving zero-discharge low-temperature atmospheric evaporative crystallization system, which includes an evaporation chamber, a crystallization kettle, an evaporative condensation heat exchanger, a condensation chamber and a refrigeration chamber unit;
  • the top and bottom of the evaporation chamber and the condensing chamber are connected to form an annular gas circulation channel.
  • the top of the evaporation chamber and the condensing chamber are connected with an insulating barrier.
  • the lower part of the evaporation chamber and the condensing chamber is provided with a gas circulation fan, and the condensing chamber
  • the side is provided with an air inlet, the air inlet surface of the gas circulation fan faces the air inlet, and the air outlet surface faces the evaporation chamber;
  • the inlet of the evaporation chamber is connected with a feed pump of concentrated brine.
  • the evaporation chamber is equipped with an evaporation chamber sprayer and an evaporation chamber packing.
  • the evaporation chamber sprayer is arranged above the evaporation chamber packing.
  • the bottom outlet of the evaporation chamber is connected with the crystallization kettle.
  • the brine feed pump is connected, the bottom side outlet of the evaporation chamber is connected with the hot side of the evaporative condensation heat exchanger, and the hot side of the evaporative condensation heat exchanger is connected with the evaporation chamber sprayer;
  • the condensing chamber is provided with a condensing chamber sprinkler and a condensing chamber packing.
  • the condensing chamber sprinkler is arranged above the condensing chamber packing.
  • the outlet at the bottom of the condensing chamber is connected with the hot end of the refrigeration chamber unit.
  • the hot end of the refrigeration chamber unit is connected to the evaporative condensation heat exchanger.
  • Cold side connection the cold side of the evaporative condensation heat exchanger is connected with a condensing device, the condensing device is connected with the cold end of the refrigeration room unit, and the cold end of the refrigeration room unit is connected with the condensing chamber sprayer; the bottom side outlet of the condensing room is connected with a condensate discharge Tube.
  • the refrigeration chamber unit includes a refrigeration chamber hot end heat exchanger, a throttle valve, a refrigeration chamber cold end heat exchanger, and a refrigeration chamber compressor, and the low boiling point working fluid is in the refrigeration chamber hot end heat exchanger and throttling valve.
  • the valve, the cold end heat exchanger of the refrigeration chamber and the refrigeration chamber compressor circulate, the outlet at the bottom of the condensation chamber is connected with the hot end heat exchanger of the refrigeration chamber, and the hot end heat exchanger of the refrigeration chamber is connected with the cold side of the evaporative condensation heat exchanger;
  • the device is connected with the cold end heat exchanger of the refrigeration chamber, and the cold end heat exchanger of the refrigeration chamber is connected with the condensing chamber sprayer.
  • the condensing device is a condensing fan or a cooler.
  • the connecting pipeline between the bottom outlet of the evaporation chamber and the crystallization kettle is provided with a concentrated brine discharge pump.
  • the connecting pipeline between the bottom side outlet of the evaporation chamber and the hot side of the evaporative condensation heat exchanger is provided with a concentrated brine internal circulation pump.
  • a condensate internal circulation pump is provided on the connecting pipeline between the bottom outlet of the condensing chamber and the hot end of the refrigerating chamber unit.
  • a condensate drain pump is provided on the condensate drain pipe.
  • a waste heat utilization heat exchanger is provided on the connecting pipeline between the hot side of the evaporative condensation heat exchanger and the evaporation chamber sprayer, and the waste heat utilization heat exchanger is connected to the external system.
  • both the evaporation chamber sprinkler and the condensation chamber sprinkler are multilayered.
  • the invention discloses a working method of the energy-saving zero-emission low-temperature atmospheric evaporative crystallization system, which includes:
  • the concentrated brine enters the evaporation chamber through the concentrated brine feed pump, and the concentrated liquid at the bottom of the evaporation chamber enters the hot side of the evaporative condensation heat exchanger, and exchanges heat with the higher temperature condensate on the cold side of the evaporative condensation heat exchanger to become a high-temperature concentrated liquid. Sprayed from the sprayer of the evaporation chamber, in the filling area of the evaporation chamber, it is in reverse contact with the air sent from the gas circulation fan to cool down and returns to the bottom of the evaporation chamber.
  • the moisture in the concentrated liquid is absorbed by the heated air, and the salt is in The concentrated liquid is retained; the concentrated liquid at the bottom of the evaporation chamber will continuously accumulate salinity and gradually approach the crystallization saturation concentration; the bottom concentrated liquid will enter the crystallization kettle from the bottom outlet of the evaporation chamber to achieve solid-liquid separation to obtain solid salt, and the turbid liquid in the crystallization kettle will return to the concentrated solution. Circulate after the brine feed pump;
  • the hot air with moisture enters the condensing chamber through the air inlet, and contacts with the spray liquid of the condensing chamber sprayer in the same direction to cool down in the filling area of the condensing chamber.
  • the moisture in the air condenses into condensate and falls; after the air cools down, it passes through the gas
  • the circulating fan is sent to the evaporation chamber; the condensate accumulates at the bottom of the condensing chamber and enters the hot end of the refrigeration chamber from the outlet of the condensing chamber to exchange heat and increase the temperature.
  • the heated condensate exchanges heat with the concentrated liquid in the evaporative condensation heat exchanger and then cools down.
  • the cooled condensate passes through the condensing device to further reduce the temperature, and then exchanges heat in the cold end of the refrigeration chamber unit to cool again, and then the low-temperature condensate enters the condensing chamber sprayer; the accumulated condensate is used as the system output water and passes through the condensate discharge pipe Send out the system;
  • the air enters the condensing chamber from the air inlet under the action of the suction of the gas circulation fan, maintains the slightly positive pressure of the system, and circulates in the annular gas circulation channel formed by the evaporation chamber and the condensing chamber.
  • the present invention has the following beneficial technical effects:
  • the invention discloses an energy-saving zero-emission low-temperature atmospheric pressure evaporation crystallization system, which includes an evaporation chamber, a crystallization kettle, an evaporation condensation heat exchanger, a condensation chamber, and a refrigeration chamber unit, which utilizes low temperature atmospheric pressure evaporation and crystallization, LAEC) working principle, simulating water evaporation and rainfall cycle in natural rainfall.
  • LAEC low temperature atmospheric pressure evaporation and crystallization
  • This system uses the characteristics of different air temperature to carry different moisture capacity, and realizes the concentrated crystallization of concentrated brine and the collection of condensate through the circulation in the evaporation chamber and the condensing chamber, and realizes the zero discharge treatment of high-concentration brine under normal temperature and pressure.
  • the annular closed loop shape is adopted to reduce the resistance drop of the gas circulation.
  • the system is reasonable in design and has the characteristics of low energy consumption, low cost, zero pollutant discharge, high salinity and COD removal efficiency, and significant energy-saving effects.
  • the concentrated brine is processed into solid salt and clean water, which has obvious environmental advantages.
  • the refrigeration chamber unit adopts a low-boiling point working fluid cycle to realize the transfer of heat from low temperature to high temperature, and can achieve a good treatment effect without external heat sources and cold sources, and realizes energy saving and consumption reduction.
  • waste heat is introduced into the external system by the heat exchanger to heat the concentrated liquid, making full use of the remaining energy and maximizing energy efficiency.
  • the evaporation chamber sprayer and the condensation chamber sprayer are both multi-layered, which increases the effective contact area of gas and liquid and enhances the mass transfer effect.
  • the working method of the energy-saving zero-emission low-temperature atmospheric evaporative crystallization system disclosed in the present invention has high automation, low energy consumption, low cost, zero pollutant emission, high salinity and COD removal efficiency, and significant energy-saving effect.
  • the concentrated brine is processed It is solid salt and clean water, with good economic benefits, obvious environmental protection advantages, and good application prospects.
  • Figure 1 is a schematic diagram of the overall structure of the energy-saving zero-emission low-temperature atmospheric pressure evaporative crystallization system of the present invention.
  • 1-concentrated brine feed pump 2-evaporation chamber, 3-concentrated brine discharge pump, 4-crystallization kettle, 5-concentrated brine internal circulation pump, 6-evaporation condensation heat exchanger, 7-waste heat utilization and exchange Heater, 8-gas circulation fan, 9-evaporation chamber sprayer, 10-evaporation chamber packing, 11-condensate internal circulation pump, 12-hot end heat exchanger of refrigeration chamber, 13-throttle valve, 14-refrigeration Room cold end heat exchanger, 15-refrigeration chamber compressor, 16-condensing fan, 17-condensation chamber sprayer, 18-condensation chamber packing, 19-condensation chamber, 20-condensate discharge pump.
  • the energy-saving zero-discharge low-temperature atmospheric evaporative crystallization system of the present invention includes an evaporating chamber 2, a crystallization kettle 4, an evaporative condensation heat exchanger 6, a condensation chamber 19, and a refrigeration chamber unit.
  • the top and bottom of the evaporation chamber 2 and the condensation chamber 19 are connected to form a ring-shaped gas circulation channel.
  • the top of the evaporation chamber 2 and the condensation chamber 19 are connected with an insulating barrier.
  • the insulating barrier can be silicate with a filter membrane.
  • the partition reduces the heat exchange between the system and the outside. At the same time, gas and water vapor can pass through the filter membrane, but the liquid cannot pass through the filter membrane.
  • the lower part of the evaporating chamber 2 and the condensing chamber 19 is provided with a gas circulating fan 8.
  • the cross-sectional area of the lower part of the evaporating chamber 2 and the condensing chamber 19 is gradually reduced from the condensing chamber 19 to the evaporating chamber 2, and the side of the condensing chamber 19 is provided with air
  • the air inlet surface of the gas circulation fan 8 faces the air inlet
  • the air outlet surface faces the evaporation chamber 2.
  • the inlet of the evaporation chamber 2 is connected with a concentrated brine feed pump 1.
  • the evaporation chamber 2 is equipped with an evaporation chamber sprayer 9 and an evaporation chamber filler 10.
  • the evaporation chamber sprayer 9 is set above the evaporation chamber filler 10, and the evaporation chamber sprayer 9 can be set up in multiple layers, the bottom outlet of the evaporation chamber 2 is connected with the crystallization kettle 4, and the connection pipe between the bottom outlet of the evaporation chamber 2 and the crystallization kettle 4 is equipped with a concentrated brine discharge pump 3; the crystallization kettle 4 and a concentrated brine feed pump 1 Connection, the bottom side outlet of the evaporation chamber 2 is connected with the hot side of the evaporative condensation heat exchanger 6, and the connecting pipeline between the bottom side outlet of the evaporation chamber 2 and the hot side of the evaporative condensation heat exchanger 6 is equipped with a concentrated brine internal circulation pump 5.
  • the hot side of the evaporative-condensation heat exchanger 6 is connected to the evaporation chamber sprayer 9, and a waste heat utilization heat exchanger can be installed on the connecting pipeline between the hot side of the evaporative-condensation heat exchanger 6 and the evaporation chamber sprayer 9 7.
  • the waste heat utilization heat exchanger 7 is connected with the external system, and the waste heat of the external system is introduced into the system.
  • the condensing chamber 19 is provided with a condensing chamber sprinkler 17 and a condensing chamber filler 18.
  • the condensing chamber sprinkler 17 is arranged above the condensing chamber filler 18.
  • the condensing chamber sprinkler 17 can be arranged in multiple layers, and the refrigeration chamber units include sequentially connected
  • the cold end heat exchanger 14 and the refrigerating chamber compressor 15 circulate, the bottom outlet of the condensing chamber 19 is connected to the hot end heat exchanger 12 of the refrigerating chamber, and the connecting pipe between the bottom outlet of the condensing chamber 19 and the hot end heat exchanger 12 of the refrigerating chamber
  • the condensing device 16 can be a condensing fan or a cooler, and the condensing device 16 is connected to the cold end of the refrigerating chamber unit, and the refrigerating chamber The cold end of the unit is connected with the condensing chamber sprayer 17; the bottom side outlet of the condensing chamber 19 is connected with a condensate discharge pipe, and the condensate drain pump 20 is provided on the condensate discharge pipe.
  • the working method of the above-mentioned energy-saving zero-emission low-temperature atmospheric pressure evaporative crystallization system includes:
  • the concentrated brine enters the evaporation chamber 2 through the concentrated brine feed pump 1, and the concentrated liquid at the bottom of the evaporation chamber 2 enters the hot side of the evaporative condensation heat exchanger 6 through the concentrated brine internal circulation pump 5, and the temperature of the cold side of the evaporative condensation heat exchanger 6
  • the incoming air will return to the bottom of the evaporation chamber 2 after reverse contact with the temperature.
  • the moisture in the concentrated liquid is absorbed by the heated air, while the salt is retained in the concentrated liquid; the concentrated liquid at the bottom of the evaporation chamber 2 will continue to accumulate salinity and gradually Close to the crystallization saturation concentration; the bottom concentrated liquid enters the crystallization tank 4 from the bottom outlet of the evaporation chamber 2 through the concentrated brine discharge pump 3 to achieve solid-liquid separation to obtain solid salt, and the turbid liquid of the crystallization tank 4 returns to the concentrated brine feed pump 1 and then circulates;
  • the hot air with moisture enters the condensing chamber 19 through the air inlet, and the spray liquid of the condensing chamber sprayer 17 is in contact with the condensing chamber filler 18 in the same direction to cool down.
  • the moisture in the air condenses into condensate and falls; after the air cools down Then it is sent to the evaporation chamber 2 by the gas circulation fan 8; the condensate accumulates at the bottom of the condensing chamber 19, from the bottom outlet of the condensing chamber 19 through the condensate internal circulation pump 11, the refrigerating chamber hot end heat exchanger 12, and the refrigerated chamber compressor 15
  • the low-boiling-point working fluid commonly used refrigerants can be selected for compression work
  • the air enters the condensing chamber 19 from the air inlet under the suction force of the gas circulation fan 8 to maintain the slightly positive pressure of the system, and circulates in the annular gas circulation channel formed by the evaporation chamber 2 and the condensing chamber 19.

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Abstract

一种节能零排放低温常压蒸发结晶***及其工作方法，属于高浓度盐水零排放技术领域。包括蒸发室(2)、结晶釜(4)、蒸发冷凝换热器(6)、冷凝室(19)和制冷室单元，利用空气温度不同携带水分能力不同的特点，通过在蒸发室(2)和冷凝室(19)的循环，实现浓盐水的浓缩结晶和冷凝液的收集，实现了常温常压下的高浓度盐水零排放处理。该***设计合理，自动化程度高，低能耗、低成本、污染物零排放、盐度及COD脱除效率高，节能效果显著，浓盐水经处理为固体盐和清水，具有良好的经济收益，环保优势明显，具有良好的应用前景。

Description

一种节能零排放低温常压蒸发结晶***及其工作方法 技术领域
本发明属于高浓度盐水零排放技术领域，具体涉及一种节能零排放低温常压蒸发结晶***及其工作方法。
背景技术
淡水是人类赖以生存的物质基础，随着工业文明的发展，海水淡化及工业生产排放的高浓度盐水问题日益严重，溶液蒸发浓缩是解决这一问题的重要途径。传统溶液浓缩方法包括多级闪蒸、多效蒸发、反渗透等方法。多级闪蒸、多效蒸发过程需要消耗大量的蒸汽；反渗透法需要消耗高品质的电能，且运行维护复杂，成本较高。传统溶液浓缩方法将溶液盐度浓缩至6％以上即直接排入环境，忽略了长此以往高盐度溶液对周围海域生态环境产生的影响。由此可见，传统溶液浓缩方法能耗高、污染大，研发低能耗、低成本、污染零排放的溶液浓缩工艺具有重要意义。
发明内容
为了解决上述现有技术中存在的缺陷，本发明的目的在于提供一种节能零排放低温常压蒸发结晶***及其工作方法，***设计合理，实现了浓盐水的浓缩结晶和冷凝液的收集，以及常温常压下的高浓度盐水零排放处理。
本发明通过以下技术方案来实现：
本发明公开了一种节能零排放低温常压蒸发结晶***，包括蒸发室、结晶釜、蒸发冷凝换热器、冷凝室和制冷室单元；
蒸发室和冷凝室顶部和下部连通，形成环状的气体循环通道，蒸发室和冷凝室的顶部连通处设有绝热隔层，蒸发室和冷凝室的下部连通处设有气体循环风机，冷凝室侧部开设有空气入口，气体循环风机的进风面朝向空气入口，出 风面朝向蒸发室；
蒸发室入口连接有浓盐水进料泵，蒸发室内设有蒸发室喷淋器和蒸发室填料，蒸发室喷淋器设在蒸发室填料上方，蒸发室底部出口与结晶釜连接，结晶釜与浓盐水进料泵连接，蒸发室底部侧出口与蒸发冷凝换热器的热侧连接，蒸发冷凝换热器的热侧与蒸发室喷淋器连接；
冷凝室内设有冷凝室喷淋器和冷凝室填料，冷凝室喷淋器设在冷凝室填料上方，冷凝室底部出口与制冷室单元热端连接，制冷室单元热端与蒸发冷凝换热器的冷侧连接，蒸发冷凝换热器的冷侧连接有冷凝装置，冷凝装置与制冷室单元冷端连接，制冷室单元冷端与冷凝室喷淋器连接；冷凝室底部侧出口连接有冷凝液排放管。
优选地，制冷室单元包括依次连接的制冷室热端换热器、节流阀、制冷室冷端换热器和制冷室压缩机，低沸点工质在制冷室热端换热器、节流阀、制冷室冷端换热器和制冷室压缩机中循环，冷凝室底部出口与制冷室热端换热器连接，制冷室热端换热器与蒸发冷凝换热器的冷侧连接；冷凝装置与制冷室冷端换热器连接，制冷室冷端换热器与冷凝室喷淋器连接。
优选地，冷凝装置为冷凝风扇或冷却器。
优选地，蒸发室底部出口与结晶釜之间的连接管路上设有浓盐水外排泵。
优选地，蒸发室底部侧出口与蒸发冷凝换热器的热侧之间的连接管路上设有浓盐水内循环泵。
优选地，冷凝室底部出口与制冷室单元热端之间的连接管路上设有冷凝液内循环泵。
优选地，冷凝液排放管上设有冷凝液外排泵。
优选地，蒸发冷凝换热器的热侧与蒸发室喷淋器之间的连接管路上设有余热利用换热器，余热利用换热器与外部***连接。
优选地，蒸发室喷淋器和冷凝室喷淋器均为多层。
本发明公开了上述节能零排放低温常压蒸发结晶***的工作方法，包括：
浓盐水经浓盐水进料泵进入蒸发室，蒸发室底部的浓液进入蒸发冷凝换热器的热侧，与蒸发冷凝换热器的冷侧温度较高的冷凝液换热成为高温浓液，从蒸发室喷淋器喷下，在蒸发室填料区域与从气体循环风机送入的空气逆向接触降温后回到蒸发室底部，接触过程中浓液中的水分被加热的空气吸收，而盐分在浓液中保留；蒸发室底部的浓液会不断积累盐度并逐步接近结晶饱和浓度；底部浓液从蒸发室底部出口进入结晶釜内实现固液分离得到固体盐，结晶釜的浊液返回浓盐水进料泵后循环；
带有水分的热空气经空气入口进入冷凝室，与冷凝室喷淋器喷淋液在冷凝室填料区域同向接触降温，降温过程中空气的水分凝结成冷凝液落下；空气降温后再经气体循环风机送入蒸发室；冷凝液在冷凝室底部积累，从冷凝室底部出口进入制冷室单元热端换热升温，升温后的冷凝液在蒸发冷凝换热器中与浓液换热后降温，降温后的冷凝液经过冷凝装置进一步降低温度，再在制冷室单元冷端中换热再次降温，随后低温冷凝液进入冷凝室喷淋器；积累的冷凝液作为***产出清水经冷凝液排放管送出***；
空气在气体循环风机吸力的作用下，从空气入口进入冷凝室，维持***的微正压状态，在蒸发室和冷凝室形成的环状气体循环通道中循环。
与现有技术相比，本发明具有以下有益的技术效果：
本发明公开的一种节能零排放低温常压蒸发结晶***，包括蒸发室、结晶釜、蒸发冷凝换热器、冷凝室和制冷室单元，利用低温常压蒸发(Low temperature Ambient pressure Evaporation and Crystallization,LAEC)工作原理，模拟自然降雨中水蒸发及降雨循环。在自然中，相对湿度低于100％的气流经过海洋上方时能吸收水分但不吸收盐分，当过饱和的气流遇冷时会冷凝下来，生成降雨。LAEC技术则是在密闭环境内模拟这种自然现象，当气体在蒸发室内加热并吸收水分，然后在冷凝室内凝结成纯水。本***利用空气温度不同携带水分能力不同的特 点，通过在蒸发室和冷凝室的循环，实现浓盐水的浓缩结晶和冷凝液的收集，实现了常温常压下的高浓度盐水零排放处理。利用外在冷源(冷凝装置)冷却冷凝液，实现能效的最大化；在蒸发室和冷凝室采用喷淋加填料层来提高气液有效接触面积，加强了传质效果；蒸发室和冷凝室采用环形闭式循环外形，减小了气体循环的阻力降。该***设计合理，具有低能耗、低成本、污染物零排放、盐度及COD脱除效率高的特点，节能效果显著，浓盐水经处理为固体盐和清水，环保优势明显。
进一步地，制冷室单元采用低沸点工质循环实现热量从低温向高温转移，在无外部热源和冷源的情况下也能达到好的处理效果，实现了节能降耗。
进一步地，余热利用换热器引入外部***的余热加热浓液，充分利用了剩余能量，实现了能效的最大化。
进一步地，蒸发室喷淋器和冷凝室喷淋器均为多层，提高了气液有效接触面积，加强了传质效果。
本发明公开的上述节能零排放低温常压蒸发结晶***的工作方法，自动化程度高，低能耗、低成本、污染物零排放、盐度及COD脱除效率高，节能效果显著，浓盐水经处理为固体盐和清水，具有良好的经济收益，环保优势明显，具有良好的应用前景。
附图说明
图1为本发明的节能零排放低温常压蒸发结晶***的整体结构示意图。
图中：1-浓盐水进料泵、2-蒸发室、3-浓盐水外排泵、4-结晶釜、5-浓盐水内循环泵、6-蒸发冷凝换热器、7-余热利用换热器、8-气体循环风机、9-蒸发室喷淋器、10-蒸发室填料、11-冷凝液内循环泵、12-制冷室热端换热器、13-节流阀、14-制冷室冷端换热器、15-制冷室压缩机、16-冷凝风扇、17-冷凝室喷淋器、18-冷凝室填料、19-冷凝室、20-冷凝液外排泵。
具体实施方式
下面结合附图和具体实施例对本发明做进一步详细描述，其内容是对本发明的解释而不是限定：
如图1，本发明的节能零排放低温常压蒸发结晶***，包括蒸发室2、结晶釜4、蒸发冷凝换热器6、冷凝室19和制冷室单元。
蒸发室2和冷凝室19顶部和下部连通，形成环状的气体循环通道，蒸发室2和冷凝室19的顶部连通处设有绝热隔层，绝热隔层可以采用带有滤膜的硅酸盐隔板，降低***和外部的换热，同时气体和水蒸气能够通过滤膜，液体不能通过滤膜。蒸发室2和冷凝室19的下部连通处设有气体循环风机8，蒸发室2和冷凝室19的下部连通处截面积由冷凝室19向蒸发室2渐缩，冷凝室19侧部开设有空气入口，气体循环风机8的进风面朝向空气入口，出风面朝向蒸发室2。
蒸发室2入口连接有浓盐水进料泵1，蒸发室2内设有蒸发室喷淋器9和蒸发室填料10，蒸发室喷淋器9设在蒸发室填料10上方，蒸发室喷淋器9可以多层设置，蒸发室2底部出口与结晶釜4连接，蒸发室2底部出口与结晶釜4之间的连接管路上设有浓盐水外排泵3；结晶釜4与浓盐水进料泵1连接，蒸发室2底部侧出口与蒸发冷凝换热器6的热侧连接，蒸发室2底部侧出口与蒸发冷凝换热器6的热侧之间的连接管路上设有浓盐水内循环泵5，蒸发冷凝换热器6的热侧与蒸发室喷淋器9连接，可以在蒸发冷凝换热器6的热侧与蒸发室喷淋器9之间的连接管路上设置余热利用换热器7，余热利用换热器7与外部***连接，将外部***的余热引入***。
冷凝室19内设有冷凝室喷淋器17和冷凝室填料18，冷凝室喷淋器17设在冷凝室填料18上方，冷凝室喷淋器17可以多层设置，制冷室单元包括依次连接的制冷室热端换热器12、节流阀13、制冷室冷端换热器14和制冷室压缩机15，低沸点工质在制冷室热端换热器12、节流阀13、制冷室冷端换热器14和制冷室压缩机15中循环，冷凝室19底部出口与制冷室热端换热器12连接，冷凝室19底部出口与制冷室热端换热器12之间的连接管路上设有冷凝液内循环 泵11，制冷室热端换热器12与蒸发冷凝换热器6的冷侧连接；冷凝装置16与制冷室冷端换热器14连接，制冷室冷端换热器14与冷凝室喷淋器17连接；蒸发冷凝换热器6的冷侧连接有冷凝装置16，冷凝装置16可以采用冷凝风扇或冷却器，冷凝装置16与制冷室单元冷端连接，制冷室单元冷端与冷凝室喷淋器17连接；冷凝室19底部侧出口连接有冷凝液排放管，冷凝液排放管上设有冷凝液外排泵20。
上述节能零排放低温常压蒸发结晶***的工作方法，包括：
浓盐水经浓盐水进料泵1进入蒸发室2，蒸发室2底部的浓液经浓盐水内循环泵5进入蒸发冷凝换热器6的热侧，与蒸发冷凝换热器6的冷侧温度较高的冷凝液换热成为高温浓液，再经过余热利用换热器7吸收热量继续升高温度，从蒸发室喷淋器9喷下，在蒸发室填料10区域与从气体循环风机8送入的空气逆向接触降温后回到蒸发室2底部，接触过程中浓液中的水分被加热的空气吸收，而盐分在浓液中保留；蒸发室2底部的浓液会不断积累盐度并逐步接近结晶饱和浓度；底部浓液从蒸发室2底部出口经浓盐水外排泵3进入结晶釜4内实现固液分离得到固体盐，结晶釜4的浊液返回浓盐水进料泵1后循环；
带有水分的热空气经空气入口进入冷凝室19，与冷凝室喷淋器17喷淋液在冷凝室填料18区域同向接触降温，降温过程中空气的水分凝结成冷凝液落下；空气降温后再经气体循环风机8送入蒸发室2；冷凝液在冷凝室19底部积累，从冷凝室19底部出口经冷凝液内循环泵11制冷室热端换热器12，与被制冷室压缩机15压缩做功升温的低沸点工质(可选用常用制冷剂)换热升高温度，升温后的冷凝液在蒸发冷凝换热器6中与浓液换热后降温，降温后的冷凝液经过冷凝装置16进一步降低温度，再在制冷室单元冷端中换热再次降温，随后低温冷凝液进入冷凝室喷淋器17；积累的冷凝液作为***产出清水经冷凝液外排泵20由冷凝液排放管送出***；
空气在气体循环风机8吸力的作用下，从空气入口进入冷凝室19，维持系 统的微正压状态，在蒸发室2和冷凝室19形成的环状气体循环通道中循环。
需要说明的是，以上所述仅为本发明实施方式的一部分，根据本发明所描述的***所做的等效变化，均包括在本发明的保护范围内。本发明所属技术领域的技术人员可以对所描述的具体实例做类似的方式替代，只要不偏离本发明的结构或者超越本权利要求书所定义的范围，均属于本发明的保护范围。

Claims (10)

  1. 一种节能零排放低温常压蒸发结晶***，其特征在于，包括蒸发室(2)、结晶釜(4)、蒸发冷凝换热器(6)、冷凝室(19)和制冷室单元；
    蒸发室(2)和冷凝室(19)顶部和下部连通，形成环状的气体循环通道，蒸发室(2)和冷凝室(19)的顶部连通处设有绝热隔层，蒸发室(2)和冷凝室(19)的下部连通处设有气体循环风机(8)，冷凝室(19)侧部开设有空气入口，气体循环风机(8)的进风面朝向空气入口，出风面朝向蒸发室(2)；
    蒸发室(2)入口连接有浓盐水进料泵(1)，蒸发室(2)内设有蒸发室喷淋器(9)和蒸发室填料(10)，蒸发室喷淋器(9)设在蒸发室填料(10)上方，蒸发室(2)底部出口与结晶釜(4)连接，结晶釜(4)与浓盐水进料泵(1)连接，蒸发室(2)底部侧出口与蒸发冷凝换热器(6)的热侧连接，蒸发冷凝换热器(6)的热侧与蒸发室喷淋器(9)连接；
    冷凝室(19)内设有冷凝室喷淋器(17)和冷凝室填料(18)，冷凝室喷淋器(17)设在冷凝室填料(18)上方，冷凝室(19)底部出口与制冷室单元热端连接，制冷室单元热端与蒸发冷凝换热器(6)的冷侧连接，蒸发冷凝换热器(6)的冷侧连接有冷凝装置(16)，冷凝装置(16)与制冷室单元冷端连接，制冷室单元冷端与冷凝室喷淋器(17)连接；冷凝室(19)底部侧出口连接有冷凝液排放管。
  2. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于，制冷室单元包括依次连接的制冷室热端换热器(12)、节流阀(13)、制冷室冷端换热器(14)和制冷室压缩机(15)，低沸点工质在制冷室热端换热器(12)、节流阀(13)、制冷室冷端换热器(14)和制冷室压缩机(15)中循环，冷凝室(19)底部出口与制冷室热端换热器(12)连接，制冷室热端换热器(12)与蒸发冷凝换热器(6)的冷侧连接；冷凝装置(16)与制冷室冷端换热器(14)连接，制冷室冷端换热器(14)与冷凝室喷淋器(17)连接。
  3. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于， 冷凝装置(16)为冷凝风扇或冷却器。
  4. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于，蒸发室(2)底部出口与结晶釜(4)之间的连接管路上设有浓盐水外排泵(3)。
  5. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于，蒸发室(2)底部侧出口与蒸发冷凝换热器(6)的热侧之间的连接管路上设有浓盐水内循环泵(5)。
  6. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于，冷凝室(19)底部出口与制冷室单元热端之间的连接管路上设有冷凝液内循环泵(11)。
  7. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于，冷凝液排放管上设有冷凝液外排泵(20)。
  8. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于，蒸发冷凝换热器(6)的热侧与蒸发室喷淋器(9)之间的连接管路上设有余热利用换热器(7)，余热利用换热器(7)与外部***连接。
  9. 根据权利要求1所述的节能零排放低温常压蒸发结晶***，其特征在于，蒸发室喷淋器(9)和冷凝室喷淋器(17)均为多层。
  10. 根据权利要求1～9任意一项所述节能零排放低温常压蒸发结晶***的工作方法，其特征在于，包括：
    浓盐水经浓盐水进料泵(1)进入蒸发室(2)，蒸发室(2)底部的浓液进入蒸发冷凝换热器(6)的热侧，与蒸发冷凝换热器(6)的冷侧温度较高的冷凝液换热成为高温浓液，从蒸发室喷淋器(9)喷下，在蒸发室填料(10)区域与从气体循环风机(8)送入的空气逆向接触降温后回到蒸发室(2)底部，接触过程中浓液中的水分被加热的空气吸收，而盐分在浓液中保留；蒸发室(2)底部的浓液会不断积累盐度并逐步接近结晶饱和浓度；底部浓液从蒸发室(2)底部出口进入结晶釜(4)内实现固液分离得到固体盐，结晶釜(4)的浊液返 回浓盐水进料泵(1)后循环；
    带有水分的热空气经空气入口进入冷凝室(19)，与冷凝室喷淋器(17)喷淋液在冷凝室填料(18)区域同向接触降温，降温过程中空气的水分凝结成冷凝液落下；空气降温后再经气体循环风机(8)送入蒸发室(2)；冷凝液在冷凝室(19)底部积累，从冷凝室(19)底部出口进入制冷室单元热端换热升温，升温后的冷凝液在蒸发冷凝换热器(6)中与浓液换热后降温，降温后的冷凝液经过冷凝装置(16)进一步降低温度，再在制冷室单元冷端中换热再次降温，随后低温冷凝液进入冷凝室喷淋器(17)；积累的冷凝液作为***产出清水经冷凝液排放管送出***；
    空气在气体循环风机(8)吸力的作用下，从空气入口进入冷凝室(19)，维持***的微正压状态，在蒸发室(2)和冷凝室(19)形成的环状气体循环通道中循环。
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