CN212740793U - Seawater atomization cyclone desalination equipment system - Google Patents

Abstract

The utility model provides a sea water atomizing gas desalts equipment system soon, this sea water atomizing gas desalts equipment system soon includes the atomizing desalination tower, sets up the brine room that is used for atomizing spun atomizing device and atomizing desalination tower bottom with high temperature sea water in the atomizing desalination tower, atomizing device is connected with the gaseous preheating device that is located the external jar, jar body upper portion is equipped with and utilizes the negative pressure principle to suck atomizing fresh water out jar body and carry out the water device and the fan of congealing of collecting, it is connected with the fan to congeal the water device, the brine room is connected with the salt extraction device. The utility model discloses equipment system investment is few, simple structure, and area is little, and the operation energy consumption is low (fresh water < 4 kW.h every m), and the water yield is high, the sea water desalination cost of going is low, easily promotes.

Description

Seawater atomization cyclone desalination equipment system

Technical Field

The utility model relates to a sea water desalination technical field especially relates to a sea water atomizing air-swirl desalination's equipment system.

Background

At present, the Chinese fresh water resource reserves are about 2.8 trillion t, which accounts for about 6 percent of the total amount of global water resources, the per-capita fresh water accounts for less than 2300t, and the per-capita fresh water accounts for less than 1/4 percent of the total water of the world, and is one of the countries with the most poor per-capita water resources. The large population base exacerbates the contradiction between supply and demand of water resources.

Meanwhile, the spatial distribution of water resources in China is extremely uneven, and an obvious pattern with few east-docetaxel and few south-north is formed. The water shortage of about 2/3 major cities in China is nearly 1/5, and the water shortage phenomenon is more obvious in North China, northeast China, northwest China and coastal areas. The crisis of fresh water resources not only seriously restricts the high-speed development of the economy of China, but also seriously affects the daily work and life of people.

Although the fresh water resources in China are seriously deficient, the sea area in China is wide, the coastline is long and narrow, the seawater resources are rich, the seawater resources are reasonably utilized and processed to be converted into the fresh water resources, the problem of shortage of the fresh water resources in coastal areas can be greatly relieved, and the method is an effective measure for promoting the sustainable development of coastal area economy and island economy.

At present, the seawater desalination projects in China are mainly distributed in 9 provinces and cities (Shandong, Zhejiang, Guangdong, Tianjin, Liaoning, Hebei, Jiangsu, Fujian, Hainan and the like) along the sea, wherein the seawater desalination projects in Jiangsu and Hainan are low in scale and both are not more than 1 million t/d.

As is known, the average salinity of the seawater on the earth is 35 per thousand, the salinity of the seawater in different areas is different and is influenced by the fresh water on the continent, the salinity of the shallow sea is generally 27 to 30 per thousand, the salinity of the estuary area is generally 0 to 30 per thousand, the salinity of the bay area is generally higher than 45 per thousand due to higher evaporation capacity, less runoff of the fresh water and the influence of high-salinity wastewater discharged by a seawater desalination plant, and the salinity of the mediterranean sea and the red sea is also more than 41 per thousand.

The salt content of seawater is complex and mainly composed of Na⁺，K⁺，Ca²⁺，Mg²⁺And Sr²⁺Isocation and Cl^-，SO₄ ^2-，Br^-，HCO₃ ^-Plasma and molecular H₃BO₃And the like. Typical salinity of seawater is generally between 30 per thousand and 43 per thousand, wherein Ca²⁺The content variation range is 360-500 Mg/L, Mg²⁺The content variation range is 1150-1600 mg/L, Na⁺The content variation range is 9700-13500 mg/L, K⁺The content variation range is 400-550 mg/L, and Cl is^-The content variation range is 16300-23700 mg/L, SO₄ ^2-The content variation range is 2400-3380 mg/L, and HCO₃ ^-The content variation range is 130-200 mg/L. In other words, seawater is also an abundant salt mine, while a large amount of industrial salt and civil salt in China currently come from well salt in inland areas, and the large amount of exploitation of well salt causes geological subsidence collapse and waste residue pollution.

In the aspect of seawater desalination, since the last 60 th century in China, a plurality of scientific and technological enterprises and scientific research institutes of universities related to oceans develop series of researches and practices for seawater desalination, the current methods for seawater desalination mainly comprise a distillation method, a membrane separation method, a crystallization method, a renewable energy source combination method, a solvent extraction method, an ion exchange method and the like, and the existing research and application achievements can be roughly summarized into the following five categories:

the first type is a distillation process, which essentially comprises:

(1) low temperature multi-effect distillation technology (LT-MED): the seawater is distilled and condensed for a plurality of times at low temperature to prepare fresh water, but the outer wall of the heat exchange tube is easy to scale, the improvement of the heat efficiency is limited by low temperature (less than or equal to 70 ℃), the equipment volume is large, and the investment is relatively high.

(2) Multistage flash technology (MSF): the seawater is pretreated, sterilized, heated by steam, and subjected to multistage flash evaporation and then condensed to prepare fresh water, the system has the advantages of higher operating temperature, large corrosion tendency of structural materials, high heat consumption, high electric energy consumption, high engineering investment amount, small operation elasticity of equipment, difficulty in adapting to engineering with large water yield change and capability of causing heat pollution to marine environment.

(3) Vapor compression distillation (VC): the system has high requirement on the sealing performance, high requirement on the pretreatment of the seawater, easy scaling, high heat consumption and power consumption, large equipment volume, high operation cost and high heat pollution to the marine environment.

The second type is a membrane separation method, which mainly comprises:

(1) reverse osmosis technology (SWRO): the separation of salt impurities and fresh water is realized by utilizing the pressure difference between two sides of the reverse osmosis membrane, and the current market application accounts for about 85 percent. The method has high requirements on pretreatment of seawater, large membrane component loss, sensitive membrane flux to temperature, large amount of high-quality corrosion-resistant auxiliary materials (stainless steel pipelines, plates and titanium metal pipelines) and high fresh water treatment cost.

(2) Electrodialysis technique (ED): the salt and the water are directionally moved and separated by utilizing the action of potential difference, and the operation energy consumption is higher (generally 17-20 kW.h/m)³) And it is difficult to remove salts having a small dissociation degree, non-dissociative substances, bacteria, etc., and the water quality of the product is poor.

The third type is a crystallization process comprising:

(1) freezing crystallization method

The freezing crystallization method comprises three types, namely a natural freezing method, an artificial freezing method and an exchange crystallization freezing desalination method. The natural freezing method is to freeze sea water and freeze the sea water to ice by using natural environment conditions, and the ice is melted to prepare fresh water, and the method is greatly influenced by natural environment factors such as seasons and the like. The artificial freezing method is to utilize direct or indirect heat exchange between a refrigerant or a refrigerant (n-butane, isobutane, R410A and the like) and seawater to freeze and freeze the seawater, but the artificial freezing method has the problems of large equipment volume, high energy consumption in the process of recovering and reusing the refrigerant, high energy consumption in the process of melting ice, low desalting rate and the like. The exchange crystallization freezing desalination method is a heat exchange crystallization method which utilizes precooled seawater and straight-chain hydrocarbon coexisting in a solid-liquid state, and the energy consumption is high due to pressure conversion in the separation process.

(2) Hydrate crystallization method: the hydration crystal is formed by hydration agent (monofluoro dichloroethane, methane, carbon dioxide gas, etc.) and water under certain temperature and pressure, the crystal particle is easy to form compression agglomeration and is difficult to clean, and the fresh water is mixed with trace hydration agent, so the quality of the fresh water is relatively low.

The fourth type is a renewable energy source combination method, and the prior art comprises the following steps:

(1) solar seawater desalination: the heat generated by solar energy replaces heat sources such as steam and the like to heat and distill seawater to prepare fresh water, the method has large loss of steam condensation latent heat, and simultaneously does not consider the problems of scaling inside materials, long-term stable operation of photo-thermal materials, efficient condensation and recovery of water vapor and the like.

(2) Desalting seawater by using geothermal energy: the method mainly utilizes geothermal resources (waste oil and gas wells) and the like to convert into mechanical energy to pressurize seawater to overcome natural permeation for desalination, needs to be combined with a reverse osmosis method and a low-temperature multi-effect distillation method for application, and can generate new secondary pollution in the utilization process of the waste oil and gas wells.

(3) Wind energy/ocean energy sea water desalination: the seawater desalination method mainly utilizes mechanical energy generated by wind power or mechanical energy converted by tidal energy, wave energy, temperature difference energy and the like in the ocean to pressurize the seawater so as to overcome natural permeation to dilute the seawater, and needs to be combined with a mainstream seawater desalination method for application.

The fifth type is a grease separation desalination method, for example, coconut oil and seawater are mixed, heated, condensed, separated and desalted, but the efficiency is low, and secondary pollution is easy to cause. Secondly, various medicaments are added into the strong brine generated in the existing seawater desalination engineering, and corresponding comprehensive utilization and disposal measures are not provided subsequently, so that the strong seawater is directly discharged into the ocean, and the ecological environment of the ocean is greatly influenced.

Obviously, the existing seawater desalination technologies have the technical problems of high construction cost, large equipment floor area, high requirement on seawater pretreatment, complex process, high energy consumption, high water production cost, low fresh water separation efficiency, low fresh water effluent quality and the like. In addition, in the prior art, the concentrated seawater is directly discharged into the ocean, which affects the ecological environment of the ocean, and the concentrated seawater after seawater desalination needs to be considered for chemical resource extraction and deep processing, so that an industrial chain for comprehensive utilization of seawater is formed, and the development of circular economy is urgent.

On the other hand, the prior art of directly extracting salt or potassium salt from seawater or salt lake brine is complex in process and large in investment, is almost limited to salt extraction or potassium salt extraction, and does not relate to seawater desalination treatment.

SUMMERY OF THE UTILITY MODEL

The utility model aims to solve the technical problem that overcome the above-mentioned defect that prior art exists, provide a simple structure, small investment, can separate the sea water desalination for the sea water atomizing gas of fresh water and bittern equipment system soon with high efficiency.

The utility model provides a technical scheme that its technical problem adopted is: an equipment system for seawater atomization cyclone desalination salt extraction mainly comprises an atomization desalination tower, wherein the atomization desalination tower atomizes and separates seawater into fresh water and brine with enriched salt, and the atomization desalination tower mainly comprises a tank body, an atomization device, a brine chamber, a fan, a parallel multi-pipe vortex cyclone condensation device and a fiber wire mesh water condensation device; the atomization device is arranged at the middle lower part of the tank body, the brine chamber is arranged at the bottom of the tank body, the air inlet of the fan is communicated with the negative pressure pumping hole at the upper part or the top of the tank body, the air outlet of the fan is communicated with the inlet of the parallel multi-tube vortex cyclone condensation device through a pipeline, the air outlet of the parallel multi-tube vortex cyclone condensation device is communicated with the inlet of the fiber wire mesh condensation device through a pipeline, and the water outlet of the parallel multi-tube vortex cyclone condensation device and the water outlet of the fiber wire mesh condensation device are respectively communicated with the fresh water collection device through;

or the negative pressure air extraction opening at the upper part or the top of the tank body is communicated with the inlet of the parallel multi-tube vortex cyclone condensing device through a pipeline, the air outlet of the parallel multi-tube vortex cyclone condensing device is communicated with the air inlet of the fan through a pipeline, and the air outlet of the fan is communicated with the inlet of the fiber wire mesh water condensing device through a pipeline;

or the negative pressure air suction opening at the upper part or the top of the tank body is communicated with the inlet of the parallel multi-tube vortex cyclone condensing device through a pipeline, the air outlet of the parallel multi-tube vortex cyclone condensing device is communicated with the inlet of the fiber wire mesh water condensing device through a pipeline, and the air outlet of the fiber wire mesh water condensing device is communicated with the air inlet of the fan.

Further, this system still includes gaseous preheating device, sea water pumping installation, brine discharge device, edulcoration device, spray drying device, gaseous preheating device, sea water pumping installation be linked together with the hot-blast import of the atomizing device of atomizing desalination tower, sea water import respectively, the heat transfer air inlet of environment cold air and parallel multitube vortex cyclone condensing equipment is linked together with the pipeline, gaseous preheating device's air inlet and parallel multitube vortex cyclone condensing equipment's heat transfer gas export are linked together with the pipeline, brine discharge device's import and the brine room bin outlet of atomizing desalination tower bottom be linked together.

Further, a discharge hole of the brine discharge device is communicated with a brine inlet of the impurity removal device through a pipeline, and the impurity removal device removes main impurity components in brine and/or extracts valuable components enriched in the brine by a conventional method; the purified brine outlet of the impurity removing device is communicated with the feed liquid inlet of the spray drying device through a pipeline, and the spray drying device dries the purified brine of the impurity removing device into powder salt.

Further, the discharging concentration of the brine water enriching the salinity in the brine chamber is 5-35%.

Preferably, the discharging concentration of the brine water enriching the salt in the brine chamber is 9-25%.

Further, the gas preheating device comprises a gas heating device and a fan which utilize solar energy and/or fuel combustion heat energy and/or waste heat and/or electric heat, and preferably a pollution-free solar energy-gathering gas preheating device and/or an electric heat gas preheating device.

Further, the tank body in the atomization desalting tower is in a cylindrical body, a spherical body, an elliptical body, a polygonal body or a special-shaped structural body; the atomization device can be designed into a ring shape, a plate shape, a strip shape, a cone shape or an abnormal shape and is arranged on the wall of the tank body and/or in the tank body, and the system for atomizing and separating seawater in the atomization desalting tower into fresh water vapor and salt brine with enriched salt is arranged in parallel in one stage or multiple stages.

Furthermore, the tank body, the fan, the multi-pipe vortex cyclone condensing device and the fiber mesh water condensing device of the atomization desalting tower can be designed into an integrated device or a separated single device.

Furthermore, a hot air injection device and/or a dosing device can be arranged, and the hot air injection device is arranged in the brine chamber or the side wall of the lower part of the tank body so as to further concentrate brine and clear salt crystal deposition; the dosing device is arranged on the side wall of the tank body.

Further, the impurity removal device comprises a conventional systematic device such as a dosing, reaction, crystallization separation or filtration separation mechanism and the like; the spray drying device comprises a conventional spray drying tower, a cyclone separator, a bag dust collector, a centrifugal fan and other systematic devices.

Further, a magnesium hydroxide extraction device and a strontium salt extraction device are arranged between the impurity removal device and the spray drying device.

The utility model has the advantages that:

(1) the utility model adopts the negative pressure space atomization and gasification technology to directly separate the seawater into fresh water vapor fog and brine water with enriched salt, the desalination is thorough, the water yield is large, and the quality of the produced desalinated water is good, so that the utility model has good application value for desalinating the seawater of residents living, industry and islands in coastal areas, ships, oil platforms and the like, and desalinating the brackish water in inland water-deficient areas;

(2) the utility model has the advantages of less investment, simple structure, small occupied area, low energy consumption for processing (fresh water is less than 4 kW.h per m), high water yield, low operation cost and easy popularization;

(3) the waste heat can be efficiently recovered while the condensed water is dehydrated by the parallel multi-tube vortex cyclone condensing device, the moisture in the gas is secondarily removed by the fiber mesh condensing device, and the fresh water can be completely recovered and directly mineralized according to the requirements (the fiber mesh condensing device can carry particles or mineral powder such as limestone, dolomite, medical stone and the like in a mesh);

(4) the method has good process controllability and low requirement on water quality (being suitable for seawater and salt lake water with different salinity), the salt brine of the seawater after being directly atomized, separated and enriched with salinity is easy to remove impurities, valuable resource substances such as magnesium hydroxide, strontium salt, sylvite, industrial salt and the like are extracted, and the impurity removal and the salt extraction are carried out;

(5) the equipment system is easy to realize small integration convenient for transportation and is suitable for different environments.

Drawings

Fig. 1 is a schematic structural diagram of embodiment 1 of the present invention;

FIG. 2 is a schematic view of the atomizer of the embodiment shown in FIG. 1;

fig. 3 is a schematic structural diagram of embodiment 2 of the present invention;

FIG. 4 is a schematic view of the atomizer in the embodiment of FIG. 3;

fig. 5 is a schematic structural diagram of embodiment 3 of the present invention;

FIG. 6 is a schematic view of the atomizer in the embodiment of FIG. 5;

in the figure, 1-an atomization desalting tower, 101-a first tank, 101 '-a second tank, 102-a first atomization device, 102' -a second atomization device, 103-a first brine chamber, 103 '-a second brine chamber, 104-a first fan, 104' -a second fan, 105-a parallel multi-pipe vortex cyclone condensation device, 106-a fiber wire mesh condensation device, 2-a gas preheating device, 201-a solar heat source gas preheating device, 202-a fuel combustion heat energy gas preheating device, 203-a waste heat source gas preheating device, 204-an electric heat source gas preheating device, 3-a first seawater pumping device, 3 '-a second seawater pumping device, 4-a first brine discharge device, 4' -a second brine discharge device, 5-an impurity removal device, 501-a medicine adding mechanism, 502-an impurity removing reaction mechanism, 503-an impurity removing and filtering mechanism, 6-a spray drying device, 601-a spray drying tower, 602-a cyclone separator, 603-a bag type dust collector, 604-a centrifugal fan, 605-a gas condensation device, 7-a first hot air blowing device, 7' -a second hot air blowing device, 8-a magnesium hydroxide extracting device, 801-modifier adding mechanism, 802-magnesium extracting reaction mechanism, 803-magnesium extracting filtering mechanism, 9-strontium salt extracting device, 901-precipitant adding mechanism, 902-strontium extracting reaction mechanism, 903-strontium extracting filtering mechanism, 10-first hot air spraying device, 10 '-second hot air spraying device, 11-first dosing device and 11' -second dosing device.

Detailed Description

The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.

The impurity removal chemical reagent used in the embodiment of the utility model is obtained through a conventional commercial way if no special description is provided.

Example 1

Referring to fig. 1 and 2, the present embodiment includes an atomization desalination tower 1, a first tank 101, a first atomization device 102, a first brine chamber 103, a first fan 104, a parallel multi-tube vortex cyclone condensation device 105, a fiber mesh condensation device 106, a gas preheating device 2, a solar heat source gas preheating device 201, a waste heat source gas preheating device 203, a first seawater pumping device 3, a first brine discharge device 4, a first hot air blowing device 7, and a first hot air injection device 10. The first seawater pumping device 3 is communicated with the first atomizing device 102 through a pipeline, a heat source outlet of the gas preheating device 2 taking solar energy as a heat source is respectively communicated with the first hot air blowing device 7 and the first hot air spraying device 10 through pipelines, the first hot air blowing device 7 is communicated with the first atomizing device 102 through a pipeline, the first hot air spraying device 10 is arranged on the lower side wall outside the first tank body 101, an exhaust port of the first tank body 101 is communicated with an air inlet of the parallel multi-pipe vortex cyclone condensing device 105 through a pipeline, and an air outlet of the parallel multi-pipe vortex cyclone condensing device 105 is communicated with an air inlet of the fiber mesh water condensing device 106 through a pipeline; an air outlet of the fiber mesh water condensing device 106 is communicated with an air inlet of the first fan 104 through a pipeline; the discharge port of the first brine chamber 103 is communicated with the inlet of the first brine discharge device 4; a heat exchange air inlet of the parallel multi-tube vortex cyclone condensing device 105 is communicated with ambient cold air through a pipeline, and a heat exchange air outlet of the parallel multi-tube vortex cyclone condensing device 105 is communicated with the waste heat source gas preheating device 203 through a pipeline; the waste heat source gas preheating device 203 is communicated with the gas preheating device 2 through a pipeline.

The raw seawater used in this example is taken from the peripheral sea area of island petrochemical base in some province of east China, and has salinity of about 32.3 ‰, pH of 7.92, and main ion content of Na⁺10.12g/L，K⁺ 0.3921g/L，Ca²⁺0.4056g/L，Mg²⁺ 1.162g/L，Cl^- 17.27g/L，SO₄ ^2- 2.813g/L，HCO₃ ^- 0.1322g/L, performing a seawater atomization cyclone desalination salt extraction test by using the equipment system, wherein the seawater treatment capacity of the device is designed to be 30m for cultivation/h.

The method for desalinating seawater by using the seawater atomization cyclone desalination equipment system in the embodiment 1 comprises the following steps: the raw seawater with the salinity of 32.3 per thousand is conveyed to the first atomization device 102 through the first seawater pumping device 3, meanwhile, the solar heat source gas preheating device 201 absorbs solar energy to heat air, the raw seawater and the residual heat gas provided by the residual heat source gas preheating device 203 are mixed and heated into hot air with the temperature of about 165 ℃ through the gas preheating device 2, the hot air is blown into the seawater first atomization device 102 through the first hot air blowing device 7, the seawater is heated and atomized through the first atomization device 102 and then is upwards sprayed out of the tank body 101, the seawater is gasified and atomized and separated into water vapor and brine through the first atomization device 102 by utilizing the centrifugal force of high-speed rotation, the water vapor and the brine are dripped to the first brine chamber 103 at the bottom of the tank body 101, the other hot air with the temperature of about 165 ℃ from the gas preheating device 2 is sprayed and blown into the first brine chamber 103 at the lower part of the tank body 101 through the first hot air spraying device 10, the brine is further concentrated and salt crystal bonding is cleaned through the disturbance of the, the airflow containing water vapor directly enters the parallel multi-tube vortex cyclone condensing device 105 at the top of the first tank 101 through a pipeline, heat exchange condensation and cyclone separation are carried out through a plurality of cyclone mechanisms in the parallel multi-tube vortex cyclone condensing device 105 to collect fresh water, cold air introduced into the parallel multi-tube vortex cyclone condensing device 105 forms waste heat air after condensation heat exchange, the waste heat air is collected through the pipeline and conveyed to the waste heat source air preheating device 203, the waste heat source air preheating device 203 takes the absorbed waste heat as one of auxiliary heat sources of the air preheating device 2, dehydrated air in the parallel multi-tube vortex cyclone condensing device 105 is sucked into the fiber mesh water condensing device 106 through negative pressure, fine water particles in the dehydrated air are adsorbed on the surface or in gaps of a mesh by fiber mesh screens in the fiber mesh water condensing device 106, and the adsorbed water particles fall and are separated from the fiber meshes after being gathered and gradually enlarged, fresh water is obtained after collection; the gas of second degree dehydration discharges through reaching standard through first fan 104, and the negative pressure suction power of system realizes through first fan 104 behind the fibre silk screen condensate device 106. Brine in the first brine chamber 103 at the bottom of the tank 101 is discharged through the first brine discharge device 4.

Collecting the brine falling from the atomization separation at the bottom of the atomization desalting tower for extracting salt, wherein the salinity is 13.3%, the pH value is 9.39, and the content of main ionic components is Na⁺ 44.878g/L，K⁺ 2.0512g/L，Ca²⁺ 2.6516g/L，Mg²⁺ 6.5560g/L，Cl^- 66.958g/L，SO₄ ^2- 6.8248g/L，HCO₃ ^- 3.3934g/L。

The fresh water yield of the equipment system is about 22.7 m for each h, the pH value of the product fresh water is 7.45 through relevant detection, the average value of Total Dissolved Solids (TDS) is 46mg/L, the requirement that the Total Dissolved Solids (TDS) is less than 1000mg/L in sanitary Standard for Drinking Water (GB 5749-2006) is met, the energy consumption for preparing fresh water by each m is about 3.2 kW.h, and the method is superior to the traditional technologies such as multi-effect distillation, multi-stage flash evaporation and membrane method dilution.

The experiment shows that the seawater atomization cyclone desalination is feasible, the equipment is simple and efficient, the operation is simple and convenient, the energy consumption is low, the fresh water separation efficiency is high, the fresh water effluent quality is high, the yield is high, and the application range is wide.

Example 2

Referring to fig. 3 and 4, the present embodiment includes an atomization desalination tower 1, a first tank 101, a first atomization device 102, a first brine chamber 103, a first fan 104, a parallel multi-tube vortex cyclone condensation device 105, a fiber mesh condensation device 106, an electric heat source gas preheating device 204, a first seawater pumping device 3, a first brine discharge device 4, an impurity removal device 5, a dosing mechanism 501, an impurity removal reaction mechanism 502, an impurity removal filtering and separating mechanism 503, a spray drying device 6, a spray drying tower 601, a bag type dust collector 603, a centrifugal fan 604, a first hot air blowing device 7, a magnesium hydroxide extraction device 8, a modifier addition mechanism 801, a magnesium extraction reaction mechanism 802, a magnesium extraction filtering and separating mechanism 803, a strontium salt extraction device 9, a precipitant addition mechanism 901, a strontium extraction reaction mechanism 902, a strontium extraction filtering and separating mechanism 903, and a first chemical dosing device 11. The first seawater pumping device 3 is communicated with the first seawater atomizing device 102 through a pipeline, the first chemical dosing device 11 is communicated with the lower side wall of the first tank 101 through a pipeline, the heat source outlet of the electric heating heat source gas preheating device 204 is respectively communicated with the hot air inlet of the spray drying tower 601 and the first hot air blowing-in device 7 through pipelines, the first hot air blowing-in device 7 is communicated with the first seawater atomizing device 102 through a pipeline, the exhaust port of the first tank 101 is communicated with the air inlet of the parallel multi-pipe vortex cyclone condensing device 105 through a pipeline, the air outlet of the parallel multi-pipe vortex condensing device 105 is communicated with the air inlet of the first fan 104 through a pipeline, and the air outlet of the first fan 104 is communicated with the air inlet of the fiber mesh water condensing device 106 through a pipeline; the discharge port of the first brine chamber 103 is communicated with the inlet of the first brine discharge device 4; the discharge port of the first brine discharge device 4 is communicated with an impurity removal reaction mechanism 502 of the impurity removal device 5, a dosing mechanism 501 of the impurity removal device 5 is communicated with the impurity removal reaction mechanism 502, an impurity removal filtering mechanism 503 is arranged in the impurity removal reaction mechanism 502, a liquid outlet of the impurity removal reaction mechanism 502 is communicated with a magnesium extraction reaction mechanism 802 of a magnesium hydroxide extraction device 8, a modifier adding mechanism 801 of the magnesium hydroxide extraction device 8 is communicated with the magnesium extraction reaction mechanism 802, a magnesium extraction filtering mechanism 803 is arranged in the magnesium extraction reaction mechanism 802, a liquid outlet of the magnesium extraction reaction mechanism 802 is communicated with a strontium extraction reaction mechanism 902 of a strontium salt extraction device 9, a precipitant adding mechanism 901 of the strontium salt extraction device 9 is communicated with the strontium extraction reaction mechanism 902, a strontium extraction filtering mechanism 903 is arranged in the strontium extraction reaction mechanism 902, and a liquid outlet of the strontium extraction reaction mechanism 902 is communicated with a liquid inlet of a spray drying tower 601 through a pipeline; an air outlet of the spray drying tower 601 is communicated with an air inlet of a bag type dust collector 603 through a pipeline, and an air outlet of the bag type dust collector 603 is communicated with an air inlet of a centrifugal fan 604 through a pipeline; an air outlet of the centrifugal fan 604 is communicated with an air inlet of the gas water condensing device 605 through a pipeline; the heat exchange air inlet of the parallel multi-tube vortex cyclone condensing device 105 is communicated with ambient cold air through a pipeline, and the heat exchange air outlet of the parallel multi-tube vortex cyclone condensing device 105 is communicated with the electric heating heat source gas preheating device 204 through a pipeline.

The raw seawater used in this example is obtained from coastal sea area of certain province in south China, and has a salinity of 33.3 ‰, a pH of 8.16, and Na as main ion component⁺10.678g/L，K⁺ 0.4415g/L，Ca²⁺ 0.4256g/L，Mg²⁺ 1.358g/L，Cl^- 17.852g/L，SO₄ ^2- 2.691g/L，HCO₃ ^- 0.1486g/L, performing a seawater atomization cyclone desalination salt extraction test by using the equipment system, wherein the seawater treatment capacity of the device is 100m for carrying out cultivation/h.

The method for desalting and extracting salt from seawater by using the seawater atomization cyclone desalting equipment system in the embodiment 2 comprises the following steps: the raw seawater with the salinity of 33.3 per mill is conveyed to a seawater first atomizing device 102 through a first seawater pumping device 3, a sterilization scale inhibitor is added into a first tank body 101 through a first chemical dosing device 11, meanwhile, the air is heated into hot air at about 195 ℃ through an electric heating source gas preheating device 204, the hot air is blown into the seawater first atomizing device 102 with a plate-shaped structure with gradient (the gradient in four directions is 2 percent), the seawater is heated and atomized and then is upwards atomized and sprayed out in the first tank body 101 of an atomization desalting tower 1, the seawater is gasified and atomized and separated into water vapor and brine through the first atomizing device 102, the dropwise brine descends to a first brine chamber 103 at the bottom of the tank body 101, the airflow containing the water vapor flows through a plurality of cyclone mechanisms of parallel multi-tube vortex condensing devices 105 at the top of the atomization desalting tower 1 through negative pressure suction effect to exchange heat and condense and collect fresh water through cyclone separation, parallel multitube vortex cyclone condensing unit 105 lets in and forms after the cold air condensation heat transfer waste heat air and collects through the pipeline and carry to electric heat source gas preheating device 204, as one of system auxiliary heat source, first fan 104 continuously maintains the negative pressure suction behind parallel multitube vortex cyclone condensing unit 105, and with preliminary dehydration gas discharge in fibre silk screen condensate device 106, tiny water particles in preliminary dehydration gas are adsorbed the entrapment by the silk screen in silk screen surface or clearance, the separation that drops from the silk screen after the gathering of the water particle gathering of adsorption entrapment grow gradually, be fresh water after collecting, the gaseous evacuation of two degrees dehydration. The brine in the first brine chamber 103 at the bottom of the tank 101 is conveyed to a reaction mechanism 502 of an impurity removing device 5 through a first brine discharging device 4, an impurity removing agent is added into the reaction mechanism 502 through a dosing mechanism 501, a filtering mechanism 503 is arranged at the middle lower part of the reaction mechanism 502, the brine is fully reacted and impurity removed, then conveyed to a magnesium extraction reaction mechanism 802 of a magnesium hydroxide extracting device 8 through a pipeline, a modifier is added into the magnesium extraction reaction mechanism 802 through a modifier adding mechanism 801, a magnesium extraction filtering mechanism 803 is arranged at the middle lower part of the magnesium extraction reaction mechanism 802, the solid separated after full modification reaction is vacuum dried to obtain magnesium hydroxide brine, the magnesium hydroxide is conveyed to a strontium extraction reaction mechanism 902 of a strontium salt extracting device 9 through a pipeline, a precipitator is added into the strontium extraction reaction mechanism 902 through a precipitator adding mechanism 901, and a strontium extraction filtering mechanism 903 is arranged at the middle lower part of the strontium extraction reaction mechanism 902, the solid separated by precipitation after full reaction is dried to obtain strontium salt, the rest brine is conveyed to a spray drying tower 601 through a pipeline, hot air of the spray drying tower 601 comes from a gas preheating device 2, crude industrial salt formed by spray drying brine after salt extraction at about 195 ℃ is discharged from the bottom of the spray drying tower 601, dust-containing gas in the spray drying tower 601 is conveyed to a bag type dust collector 603 through a pipeline, the gas is conveyed to an inlet of a fiber mesh water condensation device 106 through a centrifugal fan 604 discharge pipeline after dust removal, and dehydrated gas is discharged up to the standard after being condensed again to collect fresh water.

Collecting the brine falling from the atomization separation at the bottom of the atomization desalting tower for extracting salt, wherein the salinity is 11.2%, the pH value is 9.04, and the content of main ion component is Na⁺ 37.557g/L，K⁺ 1.8129g/L，Ca²⁺ 2.0866g/L，Mg²⁺ 5.7197g/L，Cl^- 56.934g/L，SO₄ ^2- 5.4080g/L，HCO₃ ^- 2.8861g/L。

The fresh water yield of the equipment system is about 70 m/h, the pH value of the product fresh water is 7.79 through relevant detection, the average value of Total Dissolved Solids (TDS) is 43mg/L, the requirement that the Total Dissolved Solids (TDS) is less than 1000mg/L in sanitary Standard for Drinking Water (GB 5749-2006) is met, the energy consumption for preparing fresh water by each m is about 3.5 kW.h, and the method is superior to the traditional technologies such as multi-effect distillation, multi-stage flash evaporation and membrane method fresh water preparation.

The experiment shows that the seawater atomization cyclone desalination and salt extraction are feasible, the equipment is simple and efficient, the operation is simple and convenient, the energy consumption is low, the fresh water separation efficiency is high, the fresh water effluent quality is high, the yield is high, and the application range is wide.

Example 3

Referring to fig. 5 and 6, the present embodiment includes a desalination system comprising 2 sets of parallel atomization, which mainly includes an atomization desalination tower 1, a first tank 101 and a second tank 101 ', a first atomization device 102 and a second atomization device 102', a first brine chamber 103 and a second brine chamber 103 ', a first fan 104 and a second fan 104', a parallel multi-tube vortex cyclone condensation device 105, a fiber mesh condensation device 106, a fuel combustion heat energy gas preheating device 202, a waste heat source gas preheating device 203, a first seawater pumping device 3 and a second seawater pumping device 3 ', a first brine discharge device 4 and a second brine discharge device 4', an impurity removal device 5, a dosing mechanism 501, an impurity removal reaction mechanism 502, an impurity removal filtering mechanism 503, a spray drying device 6, a spray drying tower 601, a cyclone separator 602, a bag type dust collector 603, a centrifugal fan 604, a first hot air blowing device 7 and a second hot air blowing device 7 ″, a third atomization device and a second atomization device 7 ″ A first hot air injection device 10 and a second hot air injection device 10 ', a first medication dosing device 11 and a second medication dosing device 11'. The first seawater pumping device 3 and the second seawater pumping device 3 'are respectively communicated with the first seawater atomization device 102 and the second seawater atomization device 102' through pipelines; the first dosing device 11 and the second dosing device 11 'are respectively communicated with the middle lower side walls of the first tank body 101 and the second tank body 101' through pipelines; a heat source outlet of the gas preheating device 202 which takes fuel combustion as heat energy is respectively communicated with a hot air inlet of the spray drying tower 601, the first hot air blowing device 7, the second hot air blowing device 7 ', the first hot air injection device 10 and the second hot air injection device 10' through pipelines; the first hot air blowing device 7 and the second hot air blowing device 7 'are respectively communicated with the first seawater atomization device 102 and the second seawater inlet atomization device 102' through pipelines; the first hot air injection device 10 and the second hot air injection device 10 'are respectively arranged on the side walls of the lower parts of the first brine chamber 103 and the second brine chamber 103' of the atomization desalting tower; the air outlets of the first tank 101 and the second tank 101 ' are respectively communicated with the air inlets of the first fan 104 and the second fan 104 ' through pipelines, the air outlets of the first fan 104 and the second fan 104 ' are respectively communicated with the air inlets of the parallel multi-pipe vortex cyclone condensing device 105 through pipelines, and the air outlet of the parallel multi-pipe vortex cyclone condensing device 105 is communicated with the fiber wire mesh water condensing device 106 through pipelines; the discharge ports of the first brine chamber 103 and the second brine chamber 103 'are respectively communicated with the inlets of the first brine discharging device 4 and the second brine discharging device 4' through pipelines; the discharge ports of the first brine discharging device 4 and the second brine discharging device 4' are communicated with an impurity removal reaction mechanism 502 of an impurity removal device 5 through pipelines, a medicine adding mechanism 501 of the impurity removal device 5 is communicated with the impurity removal reaction mechanism 502, an impurity removing and filtering mechanism 503 is arranged in the impurity removal reaction mechanism 502, and a liquid outlet of the impurity removal reaction mechanism 502 is communicated with a liquid inlet of a spray drying tower 601 through a pipeline; an air outlet of the spray drying tower 601 is communicated with an air inlet of the cyclone separator 602 through a pipeline, an air outlet of the cyclone separator 602 is communicated with an air inlet of the bag type dust collector 603 through a pipeline, and an air outlet of the bag type dust collector 603 is communicated with an air inlet of the centrifugal fan 604 through a pipeline; the air outlet of the centrifugal fan 604 is communicated with the air inlet of the multi-tube vortex cyclone condensing device 105 through a pipeline; a heat exchange air inlet of the parallel multi-tube vortex cyclone condensing device 105 is communicated with ambient cold air through a pipeline, and a heat exchange air outlet of the parallel multi-tube vortex cyclone condensing device 105 is communicated with the waste heat source gas preheating device 203 through a pipeline; the waste heat source gas preheating device 203 is communicated with the gas preheating device 2 through a pipeline.

The raw seawater used in this example is taken from coastal sea area of certain province in northeast China, and has a salinity of about 29.9 ‰, a pH value of 8.31, and a main ion content of Na⁺9.47g/L，K⁺ 0.413g/L，Ca²⁺ 0.4216g/L，Mg²⁺1.159g/L，Cl^-15.873g/L，SO₄ ^2-2.429g/L，HCO₃ ^-0.1493g/L, performing seawater atomization cyclone desalination salt extraction test by using the equipment system, wherein the seawater treatment capacity of the device is 200m for carrying out cultivation/h.

The method for desalting and extracting salt from seawater by using the seawater atomization cyclone desalting equipment system in the embodiment 3 comprises the following steps: the raw seawater with the salinity of 29.9 per mill is respectively conveyed to a first seawater atomizing device 102 and a second seawater atomizing device 102 ' of a multi-ring structure in the tank through a first seawater pumping device 3 and a second seawater pumping device 3 ', sterilization and scale inhibition medicaments are respectively added into a first tank body 101 and a second tank body 101 ' through a first chemical dosing device 11 and a second chemical dosing device 11 ', meanwhile, a fuel combustion heat energy gas preheating device 202 heats air into hot air with the temperature of about 450 ℃, the hot air entering the tank is doped with a proper amount of cold air to reduce the temperature to about 230 ℃, then the hot air is respectively blown into the first seawater atomizing device 102 and a second seawater inlet second atomizing device 102 ' through a first hot air blowing device 7 and a second hot air blowing device 7 ', the seawater is heated and atomized and then sprayed into the tank body 101, the first seawater atomizing device 102 and the second seawater atomizing device 102 ' gasify and atomize and separate the seawater into steam and brine, the dropwise brine respectively descends to a first brine chamber 103 and a second brine chamber 103 'at the bottom of the tank body 101, the other path of hot air with the temperature of about 230 ℃ from a fuel combustion heat energy gas preheating device 202 is respectively sprayed and blown into the first brine chamber 103 and the second brine chamber 103' at the lower part of the atomization desalination tower through a first hot air spraying device 10 and a second hot air spraying device 10 ', the brine is further concentrated and salt crystal bonding dirt is cleaned through disturbance of the hot air, airflow containing water vapor is respectively sucked under negative pressure by a first fan 104 and a second fan 104' at the top of the tank body 101 and continuously ascends to enter a parallel multi-pipe cyclone condensation device 105, fresh water is collected through heat exchange and cyclone separation of a plurality of cyclone mechanisms of the parallel multi-pipe cyclone condensation device 105, the parallel multi-pipe cyclone condensation device 105 is introduced with ambient cold air for heat exchange, waste heat air is formed and is collected and conveyed to a heat source gas device 203 through a pipeline, the waste heat absorbed by the waste heat source gas preheating device 203 is used as one of the auxiliary heat sources of the gas preheating device 2, the dehydrated gas of the parallel multi-pipe vortex cyclone condensation device 105 is discharged into the fiber mesh water condensation device 106, fine water particles in the primary dehydrated gas are adsorbed on the surface of a material or in gaps by fiber bundle materials, the adsorbed water particles are gathered and gradually enlarged and then fall off and separated from the fiber bundle, and the collected water particles are fresh water and are exhausted by gas subjected to secondary dehydration. Brine in a first brine chamber 103 and a second brine chamber 103 'at the bottom of a tank body 101 is respectively conveyed into an impurity removal reaction mechanism 502 of an impurity removal device 5 through a first brine discharge device 4 and a second brine discharge device 4', an impurity removal medicament is added into the impurity removal reaction mechanism 502 through a medicament adding mechanism 501, an impurity removal filtering and separating mechanism 503 is arranged at the middle lower part of the impurity removal reaction mechanism 502, the brine is fully reacted and impurity removed and then conveyed to a spray drying tower 601 through a pipeline, hot air of the spray drying tower 601 is sourced from a fuel combustion heat energy gas preheating device 202, crude industrial salt formed after purified brine is subjected to spray drying at about 260 ℃ is discharged through the bottom of the spray drying tower 601, gas containing salt dust in the spray drying tower 601 is conveyed to a cyclone separator 602 through a pipeline to further separate and separate part of the industrial salt, the discharged gas is conveyed to a bag type device 603 through a pipeline, the dust is collected and conveyed to an inlet of a parallel multi-pipe cyclone condensation device 105 through a discharge pipeline of a centrifugal fan 604, the dehydrated gas is discharged after fresh water is collected by cyclone condensation and fiber mesh condensation.

Collecting the brine falling from the atomization separation at the bottom of the atomization desalting tower for extracting salt, wherein the salinity is 17.6%, the pH value is 9.97, and the content of main ion component is Na⁺ 65.578g/L，K⁺ 2.8116g/L，Ca²⁺ 3.7572g/L，Mg²⁺ 10.067g/L，Cl^- 7.7540g/L，SO₄ ^2- 12.041g/L，HCO₃ ^- 4.6313g/L。

The fresh water yield of the equipment system is about 166 m/h, the pH value of the product fresh water is 7.97 through relevant detection, the average value of Total Dissolved Solids (TDS) is 47mg/L, the requirement that the Total Dissolved Solids (TDS) is less than 1000mg/L in sanitary Standard for Drinking Water (GB 5749-2006) is met, the energy consumption for preparing fresh water by each m is about 3.9 kW.h, and the method is superior to the traditional technologies such as multi-effect distillation, multi-stage flash evaporation and membrane method fresh water preparation.

The experiment shows that the seawater atomization cyclone desalination and salt extraction are feasible, the equipment is simple and efficient, the operation is simple and convenient, the energy consumption is low, the fresh water separation efficiency is high, the fresh water effluent quality is high, the yield is high, and the application range is wide.

Various modifications and variations of the present invention may be made by those skilled in the art, and they are within the scope of the present invention provided they are within the scope of the claims and their equivalents.

What is not described in detail in the specification is prior art that is well known to those skilled in the art.

Claims (9)

1. A seawater atomization cyclone desalination equipment system comprises an atomization desalination tower for atomizing and separating seawater into fresh water and brine with enriched salt, wherein the atomization desalination tower mainly comprises a tank body, an atomization device arranged at the middle lower part in the tank body and a brine chamber arranged at the bottom of the tank body;

or the negative pressure air extraction opening at the upper part or the top of the tank body is communicated with the inlet of the parallel multi-tube vortex cyclone condensing device through a pipeline, the air outlet of the parallel multi-tube vortex cyclone condensing device is communicated with the air inlet of the fan through a pipeline, and the air outlet of the fan is communicated with the inlet of the fiber wire mesh water condensing device through a pipeline;

or the negative pressure air extraction opening at the upper part or the top of the tank body is communicated with the inlet of the parallel multi-tube vortex cyclone condensing device through a pipeline, the air outlet of the parallel multi-tube vortex cyclone condensing device is communicated with the inlet of the fiber wire mesh water condensing device through a pipeline, and the air outlet of the fiber wire mesh water condensing device is communicated with the air inlet of the fan;

the water outlet of the parallel multi-tube vortex cyclone condensing device and the water outlet of the fiber wire mesh water condensing device are respectively communicated with the fresh water collecting device through pipelines.

2. The seawater atomization cyclone desalination equipment system as claimed in claim 1, characterized in that: the brine discharge device is characterized by further comprising a gas preheating device communicated with a hot air inlet of the atomizing device through a pipeline, and a seawater pumping device communicated with a seawater inlet of the atomizing device through a pipeline, wherein a heat exchange air inlet of the parallel multi-tube vortex cyclone condensing device is communicated with ambient cold air through a pipeline, an air inlet of the gas preheating device is communicated with a heat exchange air outlet of the parallel multi-tube vortex cyclone condensing device through a pipeline, and a discharge port of the brine chamber is communicated with the brine discharge device.

3. The seawater atomization cyclone desalination equipment system as claimed in claim 2, characterized in that: the discharge hole of the brine discharge device is communicated with the brine inlet of the impurity removal device through a pipeline, and the clean brine outlet of the impurity removal device is communicated with the feed liquid inlet of the spray drying device through a pipeline.

4. The seawater atomization cyclone desalination equipment system as claimed in any one of claims 1-3, wherein: the discharging concentration of the brine water enriching the salt in the brine chamber is 5-35%.

5. The seawater atomization cyclone desalination equipment system as claimed in claim 4, characterized in that: the discharging concentration of the brine water with salt enriched in the brine chamber is 9-25%.

6. The seawater atomization cyclone desalination equipment system as claimed in claim 2, characterized in that: the gas preheating device comprises a gas heating device and a fan which utilize solar energy and/or fuel combustion heat energy and/or waste heat and/or electric heat.

7. The seawater atomization cyclone desalination equipment system as claimed in claim 1, characterized in that: the tank body is a cylinder, a sphere, an oval body, a polygonal body or a special-shaped structure body; the atomization device is annular or plate-shaped or strip-shaped or cone-shaped or special-shaped and is arranged on the wall of the tank body and/or in the tank body, and a system for carrying out atomization separation on seawater in the atomization desalination tower into fresh water vapor and brine water rich in salt is arranged in parallel in one stage or multiple stages.

8. The seawater atomization cyclone desalination equipment system as claimed in claim 1, characterized in that: the tank body, the fan, the multi-pipe vortex cyclone condensing device and the fiber mesh water condensing device of the atomization desalting tower are designed into an integrated device or a separated single device.

9. The seawater atomization cyclone desalination equipment system as claimed in any one of claims 1-3, wherein: the hot air injection device and/or the dosing device are/is also arranged, and the hot air injection device is arranged on the side wall of the lower part of the brine chamber or the tank body; the dosing device is arranged on the side wall of the tank body.

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