A method for brine atomization evaporation concentration

Abstract

The application discloses a method for brine atomization evaporation concentration, comprising the following steps: S1, determining the initial Baume degree and the material content of the original brine, and introducing the original brine into the original brine pool according to the planned evaporation rate; S2, calculating the corresponding phase diagram, the target saturation track and the target saturation point; S3, setting the initial atomized water droplet particle size, the water evaporation amount and the atomization time, and the real-time wind power data including the wind speed and the wind direction; S4, adjusting the atomized water droplet particle size and the atomization time in the atomization evaporation process, and ensuring that the saturation track of the brine in the phase diagram overlaps with the target saturation track; S5, repeatedly performing steps S2-S4 to precipitate different precipitated materials, and introducing the brine product into the next stage spray pool for continuous atomization evaporation; when the saturation point of the brine in the phase diagram coincides with the target saturation point, the evaporation is stopped and the static setting is performed. The application realizes comprehensive atomization coverage in the brine volume, compared with single-point atomization, can more fully utilize the wind power resources, accelerates the precipitation speed, and prevents the local accumulation phenomenon from occurring.

Description

Technical Field

[0001] This invention relates to the field of salt lake brine utilization technology, and in particular to a brine atomization evaporation concentration method. Background Technology

[0002] Brine is commonly used to extract certain chemical raw materials, such as salt, iodine, boron, and bromine. Based on its location, it can be divided into shallow brine and deep brine, with deep brine often associated with oil, gas, and rock salt deposits. The scientific name for brine is bittern, a mixture of magnesium chloride, magnesium sulfate, and sodium chloride.

[0003] High-concentration brine is highly corrosive and may corrode and damage equipment such as containers or pipes, causing the equipment to be unable to work for a long time in a high-concentration brine environment. At the same time, high-concentration brine may react with other substances to produce toxic gases. If the concentration is too high, it is prone to chemical reactions such as crystallization or decomposition. It is not very stable, and once leaked, it may cause great harm to water bodies and soil environments.

[0004] The application of elemental crystallization separation in high-concentration brine within multi-aqueous systems is a complex and important process, particularly in resource recovery, chemical production, and environmental protection. High-concentration brine typically contains various dissolved salts and minerals, and crystallization separation technology can effectively extract and separate these elements, thereby achieving efficient resource utilization and sustainable environmental development.

[0005] Current techniques for crystallizing and separating elements from a multi-element aqueous system involve pouring brine into a drying tank and then allowing it to dry naturally under sunlight. This method is extremely inefficient and requires a vast area, potentially hundreds of square kilometers. Furthermore, due to factors such as rainfall, the drying speed cannot be controlled, and the precipitation pathways within the aqueous system are uncertain on the phase diagram, resulting in uncontrollable purity and quantity of the separated substances. Summary of the Invention

[0006] This invention overcomes the shortcomings of the prior art and provides a method for brine atomization evaporation concentration.

[0007] To achieve the above objectives, the technical solution adopted by the present invention is: a brine atomization evaporation concentration method, comprising the following steps:

[0008] S1. Initial detection: Determine the initial Baume degree and substance content of the raw brine, and obtain the planned evaporation rate according to the purification process and the corresponding target precipitate, and introduce the raw brine into the raw brine tank.

[0009] S2. Calculation parameters: Calculate the corresponding phase diagram, target saturation trajectory, and target saturation point based on the target precipitate.

[0010] S3. Set parameters: Set the initial atomized water droplet size, water evaporation rate and atomization time according to real-time wind data and planned evaporation rate. Real-time wind data includes wind speed and wind direction.

[0011] S4. Atomization Evaporation: Start the atomization evaporation process, monitor the real-time Baume degree of the brine, the real-time state of the precipitated substances, and the real-time wind force data, and adjust the atomized water droplet size and atomization time to ensure that the saturation trajectory of the brine in the phase diagram overlaps with the target saturation trajectory.

[0012] S5. Repeat steps S2-S4 to precipitate different precipitates, and introduce the brine obtained in S4 into the next stage spray tank for continued atomization and evaporation. When the saturation point of the brine in the phase diagram coincides with the target saturation point, stop evaporation and allow it to settle.

[0013] In a preferred embodiment of the present invention, in step S1, the formula for the planned evaporation rate is: Where C is the evaporation rate, B is the Baume degree of the brine after evaporation, and b is the Baume degree of the brine before evaporation.

[0014] In a preferred embodiment of the present invention, in step S1, the purification process includes a potassium extraction process and a lithium extraction process.

[0015] In a preferred embodiment of the present invention, in the potassium extraction process, the atomized water droplet particle size varies from 500 to 2000 μm, and the evaporation rate is 5% to 15%.

[0016] In a preferred embodiment of the present invention, the Baume degree of the brine varies from 23 to 32°Bé during the potassium extraction process.

[0017] In a preferred embodiment of the present invention, in the lithium extraction process, the Li in the original brine... + The concentration is 0.05–0.2 g / L, the atomized water droplet size varies from 40 to 500 μm, and the evaporation rate is 30–50%.

[0018] In a preferred embodiment of the present invention, the Baume degree of the brine varies from 12 to 34°Bé in the lithium extraction process.

[0019] In a preferred embodiment of the present invention, the specific steps for setting the atomization time in step S3 are as follows:

[0020] S31. Calculate the amount of water evaporation using the formula E=K×(ρ1-ρ s )×u; where E is the water evaporation rate, in kg / m³ 2 ·s, where K is the mass transfer coefficient, ranging from 0.1 to 3 kg / (m³). 2 ·s·Pa), where ρ1 is the water vapor pressure in Pa, ρ s ρ is saturated vapor pressure, in Pa; u is wind speed, in m / s.

[0021] S32. Calculate the evaporation time using the following formula: Where t is the evaporation time in seconds, M is the amount of water to be evaporated in kilograms, and A is the evaporation area in square meters. 2 E is the average evaporation rate calculated in S32.

[0022] In a preferred embodiment of the present invention, in step S5, the area S of the spray tank gradually decreases as the order n of the spray tank increases, with the formula S = S0 - k·S0, where S0 is the initial area of ​​the original brine tank and k is the area reduction rate, ranging from 0.85 to 0.92.

[0023] In a preferred embodiment of the present invention, the specific steps for adjusting the atomized water droplet size and atomization time in step S4 are as follows: if the real-time saturation trajectory is lower than the target trajectory, it indicates that the evaporation rate is too low, so the atomized water droplet size is reduced or the atomization time is extended; if the real-time saturation trajectory is higher than the target trajectory, it indicates that the evaporation rate is too high, so the atomized water droplet size is increased or the atomization time is shortened.

[0024] This invention addresses the shortcomings of the prior art and has the following beneficial effects:

[0025] (1) This invention provides a brine atomization evaporation concentration method. The three-dimensional atomization technology is used to achieve full atomization coverage within the volume of brine. Compared with single-point atomization, it can make fuller use of wind resources and accelerate the precipitation speed. It solves the problem of resource waste caused by the large area occupied by the drying pool in the prior art. At the same time, it disperses the distribution of precipitated crystals and helps to prevent local accumulation. It solves the problem of uncontrollable purity and quantity of separated substances due to the inability to control the drying speed. It improves the precipitation rate of salt fields and improves the purity of precipitates.

[0026] (2) By repeatedly performing the atomization evaporation step, the present invention can effectively separate and precipitate different target precipitates, thereby improving resource utilization. The treated brine is sent to the next stage spray tank for further treatment, which can achieve cascade purification, reduce the amount of treatment per batch, and reduce the difficulty of operation. Furthermore, by using the brine saturation point to coincide with the target point as the stopping condition, the purification end time can be well controlled, reducing product loss.

[0027] (3) This invention clearly distinguishes between the potassium extraction process and the lithium extraction process in the purification process, and sets different target precipitates for each of these two processes. This distinction allows each process to be optimized for specific target substances, improving the efficiency and accuracy of purification. By controlling the parameters in the potassium extraction and lithium extraction processes separately, it is possible to ensure that products with higher purity and more stable quality are obtained, meeting market demands.

[0028] (4) The present invention can finely break brine into nano-sized ultrafine water droplets, which are smaller in size than those produced by traditional methods. This increases the contact area between the brine and the surrounding air. These ultrafine water droplets are evenly sprayed into the air to form a three-dimensional atomization zone, so that each water droplet can be fully exposed to the air. Due to the small size of the water droplets and the high surface tension, they can float in the air for a certain period of time and fully contact the surrounding air, creating conditions for the rapid evaporation of crystals in the brine. Attached Figure Description

[0029] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments recorded in the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0030] Figure 1 This is a flowchart of a preferred embodiment of the present invention. Detailed Implementation

[0031] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0032] Many specific details are set forth in the following description in order to provide a full understanding of the invention. However, the invention may also be practiced in other ways different from those described herein. Therefore, the scope of protection of the invention is not limited to the specific embodiments disclosed below.

[0033] like Figure 1 As shown, a method for concentrating brine by atomization evaporation includes the following steps:

[0034] S1. Initial detection: Determine the initial Baume degree and substance content of the raw brine, and obtain the planned evaporation rate according to the purification process and the corresponding target precipitate, and introduce the raw brine into the raw brine tank.

[0035] S2. Calculation parameters: Calculate the corresponding phase diagram, target saturation trajectory, and target saturation point based on the target precipitate.

[0036] S3. Set parameters: Set the initial atomized water droplet size, water evaporation rate and atomization time according to real-time wind data and planned evaporation rate. Real-time wind data includes wind speed and wind direction.

[0037] S4. Atomization Evaporation: Start the atomization evaporation process, monitor the real-time Baume degree of the brine, the real-time state of the precipitated substances, and the real-time wind force data, and adjust the atomized water droplet size and atomization time to ensure that the saturation trajectory of the brine in the phase diagram overlaps with the target saturation trajectory.

[0038] S5. Repeat steps S2-S4 to precipitate different precipitates, and introduce the brine obtained in S4 into the next stage spray tank for continued atomization and evaporation. When the saturation point of the brine in the phase diagram coincides with the target saturation point, stop evaporation and allow it to settle.

[0039] This invention uses three-dimensional atomization technology to achieve comprehensive atomization coverage within the brine volume. Compared with single-point atomization, it can make fuller use of wind resources, accelerate the precipitation speed, solve the resource waste problem of the large area occupied by the drying pool in the prior art, and disperse the distribution of precipitated crystals, which is also conducive to preventing local accumulation. It solves the problem of uncontrollable purity and quantity of separated substances due to the inability to control the drying speed, improves the precipitation rate of salt fields, and improves the purity of precipitates.

[0040] In S1, the purification process includes a potassium extraction process and a lithium extraction process. The target precipitates in the potassium extraction process include sodium chloride, potassium-sodium compounds, and sodium compounds. The target precipitates in the lithium extraction process include sodium compounds, potassium-sodium compounds, and potassium-sodium-magnesium compounds.

[0041] This step clearly distinguishes between potassium extraction and lithium extraction in the purification process, and sets different target precipitates for each process. This distinction allows each process to be optimized for specific target substances, improving purification efficiency and accuracy. By controlling the parameters in the potassium and lithium extraction processes separately, it is possible to obtain products with higher purity and more stable quality, meeting market demands.

[0042] In the potassium extraction process, the atomized water droplet size varies from 500 to 2000 μm, and the evaporation rate is 5 to 15%; the Baumé degree of the brine varies from 23 to 32°Bé.

[0043] By precisely controlling the atomized water droplet size within the range of 500–2000 μm and the evaporation rate within the range of 5–15%, precise separation of different substances in the brine can be achieved. This precise control helps reduce unnecessary energy consumption and material loss, improving resource utilization efficiency. Simultaneously, controlling the brine's Baume degree variation within the range of 23–32°Bé ensures the stability and controllability of the brine during the evaporation process, which is beneficial for obtaining ideal precipitates.

[0044] In the lithium extraction process, the Li in the original brine... +The concentration is 0.05–0.2 g / L, the atomized water droplet size ranges from 40 to 500 μm, and the evaporation rate is 30–50%; the Baumé degree of the brine ranges from 12 to 34°Bé.

[0045] For the Li+ content range in the original brine (0.05–0.2 g / L), by adjusting the atomized water droplet size to 40–500 μm and controlling the evaporation rate to 30–50%, this targeted parameter setting helps reduce interference from other impurity elements and improves the recovery rate and purity of lithium products. Furthermore, controlling the Baume degree of the brine within the range of 12–34°Bé ensures a suitable chemical environment during lithium extraction, which is beneficial for the precipitation and separation of lithium.

[0046] In S1, the formula for the planned evaporation rate is: Where C is the evaporation rate, B is the Baume degree of the brine after evaporation, and b is the Baume degree of the brine before evaporation.

[0047] In S2, the specific steps for calculating the parameters are as follows:

[0048] S21. Based on the chemical composition and concentration of the target precipitate, look up the saturation curve of the substance at different temperatures to obtain the corresponding relationship between the saturation value and concentration of the substance at different evaporation rates, which is the phase diagram of the substance at different evaporation rates.

[0049] S22. Based on the planned evaporation rate and the expected trend of brine evaporation, draw the ideal saturation trajectory from the initial saturation point to the target saturation point on the phase diagram; the target saturation point refers to the saturation point corresponding to when the brine saturation reaches the target concentration.

[0050] In S3, the specific steps for setting the atomization time are as follows:

[0051] S31. Calculate the amount of water evaporation using the formula E=K×(ρ1-ρ s )×u; where E is the water evaporation rate, in kg / m³ 2 ·s, where K is the mass transfer coefficient, ranging from 0.1 to 3 kg / (m³). 2 ·s·Pa), where ρ1 is the water vapor pressure in Pa, ρ s ρ is saturated vapor pressure, in Pa; u is wind speed, in m / s.

[0052] S32. Calculate the evaporation time using the following formula: Where t is the evaporation time in seconds, M is the amount of water to be evaporated in kilograms, and A is the evaporation area in square meters. 2 E is the average evaporation rate calculated in S32.

[0053] In S4, the specific steps for adjusting the atomized water droplet size and atomization time are as follows: if the real-time saturation trajectory is lower than the target trajectory, it indicates that the evaporation rate is too low, so reduce the atomized water droplet size or extend the atomization time; if the real-time saturation trajectory is higher than the target trajectory, it indicates that the evaporation rate is too high, so increase the atomized water droplet size or shorten the atomization time.

[0054] In S5, the area S of the spray tank also includes the fact that the area S of the spray tank gradually decreases as the order n of the spray tank increases. The formula is S = S0 - k·S0, where S0 is the initial area of ​​the original brine tank and k is the area reduction rate, which ranges from 0.85 to 0.92.

[0055] By repeatedly performing the atomization evaporation step, different target precipitates can be effectively separated and precipitated, improving resource utilization. The treated brine is sent to the next stage of the spray tank for further treatment, which can achieve cascade purification, reduce the amount of brine processed at one time, and reduce the difficulty of operation. Furthermore, by using the brine saturation point to coincide with the target point as the stopping condition, the purification end time can be well controlled, reducing product loss.

[0056] The principle of this application is to atomize the brine into water droplets and spray them into the air to make full contact with the surrounding air. By increasing the contact area between the brine and the air, the evaporation rate is increased. The brine is concentrated by controlling the saturation trajectory of the phase diagram, and the corresponding precipitate is formed.

[0057] In this application, the applicant’s previously filed patent number 201721333929.1, an anti-salt-caking and anti-scaling brine mist disperser, and patent number 201721333170.7, an anti-salt-caking, anti-scaling and corrosion-resistant water pump are combined as the atomizing evaporation device in this application.

[0058] The process for potassium extraction from brine using the method provided in this application is as follows:

[0059] 1. The raw brine is introduced into the raw brine tank. The Baumé degree of the raw brine is measured to be 23-25 ​​using a Baumé meter. The droplet size is set to vary from 800 to 1000 μm. Evaporation is carried out. After 7-15% of the water is lost through evaporation, the brine is introduced into the first-stage spray tank. At this time, there is no sediment in the raw brine tank.

[0060] 2. The Baumé degree of the brine was measured again using a Baumé meter to be 25-27. The droplet size was set to vary from 800 to 1000 μm. Evaporation was carried out. After 7-15% of the water was lost through evaporation, the brine was introduced into the second-stage spray tank. At this time, there was no sediment in the first-stage spray tank.

[0061] 3. The Baumé degree of the brine was measured again using a Baumé meter to be 27-29. The droplet size was set to vary from 1000 to 1200 μm. Evaporation was carried out. After evaporation and loss of 5-10% of the water, the brine was introduced into the third-stage spray tank. At this time, the precipitate in the second-stage spray tank was sodium chloride.

[0062] 4. The Baumé degree of the brine was measured again using a Baumé meter to be 29-31. The droplet size was set to vary from 1000 to 1200 μm. Evaporation was carried out. After evaporation and loss of 5-10% of the water, the brine was introduced into the fourth-stage spray tank. At this time, the precipitate in the third-stage spray tank was potassium and sodium compounds.

[0063] 5. The Baumé degree of the brine was measured to be 31-32. The droplet size was set to vary from 1200 to 1400 μm. Evaporation was carried out. After the brine reached the saturation point of the phase diagram, the evaporator was stopped and the brine was allowed to settle. At this time, the precipitate in the fourth-stage spray tank was potassium compound.

[0064] In the potassium extraction process, the dam width of the spray tank is ≥8m to ensure the placement of the evaporation equipment and the adjacent vehicle transport passage. The atomizing evaporation equipment is placed upwind of the spray tank to fully utilize wind power and create a wind-cutting angle, saving energy. Simultaneously, the equipment is located near a power source to ensure power supply without affecting the spraying effect or electrical safety.

[0065] Air ducts are maintained between equipment based on the head distance to avoid mutual interference and maximize the effect of each unit; the air duct distance is set to be one time the length of the spray tank to prevent the evaporated brine from drifting out of the spray tank by the wind and to ensure the yield.

[0066] The process for lithium extraction from brine using the method provided in this application is as follows:

[0067] 1. The raw brine is introduced into the raw brine tank. The Baumé degree of the raw brine is measured to be 12-20 using a Baumé meter. The droplet size is set to vary from 800 to 1000 μm. Evaporation is carried out. After 40-50% of the water is lost through evaporation, the brine is introduced into the first-stage spray tank. At this time, there is no sediment in the raw brine tank.

[0068] 2. The Baumé degree of the brine was measured again using a Baumé meter to be 20-26. The droplet size was set to vary from 40 to 150 μm. Evaporation was carried out. After 40-50% of the water was lost through evaporation, the brine was introduced into the second-stage spray tank. At this time, the precipitate in the first-stage spray tank was sodium compound.

[0069] 3. The Baumé degree of the brine was measured again using a Baumé meter to be 26-31. The droplet size was set to vary from 100 to 300 μm. Evaporation was carried out. After evaporation and loss of 30-40% of the water, the brine was introduced into the third-stage spray tank. At this time, the precipitate in the second-stage spray tank was potassium and sodium compounds.

[0070] 4. The Baume degree of the brine was measured to be 31-34. The droplet size was set to vary from 100 to 300 μm. Evaporation was carried out. After the brine reached the saturation point of the phase diagram, the evaporator was stopped and the brine was allowed to settle. At this time, the precipitate in the three-stage spray tank was potassium, sodium and magnesium compounds.

[0071] In the lithium extraction process, the dam of the spray tank is designed to stably support the evaporation equipment. The atomizers of the equipment are positioned slightly upwind of the center of the spray tank to fully utilize wind power. Appropriate distances are maintained between atomizers to preserve airflow and prevent self-interference, maximizing the effectiveness of each atomizer. The airflow distance is set at least twice the length of the spray tank to prevent evaporated brine from drifting out of the tank by the wind, ensuring a high yield. Simultaneously, the equipment is located near a power source to ensure power supply without affecting the spraying effect or electrical safety.

[0072] Example 1

[0073] 1. The raw material composition is shown in Table 1:

[0074] Table 1. Composition of raw halogen elements

[0075] Li (mg / L) Mg (mg / L) Cl (mg / L) Na (mg / L) K (mg / L) 362 105 42 2675 29

[0076] 2. Concentration steps:

[0077] (1) The original brine was introduced into the original brine tank and the initial Baumé degree was measured to be 23. The substance content is shown in Table 1. In order to extract potassium from the brine, the atomized water droplet particle size was set to 800μm and evaporation was carried out. After evaporation and loss of 7% of the water, the brine was introduced into the first-stage spray tank. At this time, there was no sediment in the original brine tank. The size of the original brine tank was 28m×20m×8m.

[0078] (2) The Baumé degree of the brine was measured to be 25 again using a Baumé meter. The atomized water droplet size was set to 800 μm and evaporation was carried out. After evaporation and loss of 7% of the water, the brine was introduced into the second-stage spray tank. At this time, there was no sediment in the first-stage spray tank. The size of the first-stage spray tank was 25m × 18m × 8m.

[0079] (3) The Baumé degree of the brine was measured to be 27. The atomized water droplet particle size was set to 1000μm and evaporated. After evaporation and loss of 5% of the water, the brine was introduced into the third-stage spray tank. At this time, the precipitate in the second-stage spray tank was sodium chloride. The size of the second-stage spray tank was 22m×16m×8m.

[0080] (4) The Baumé degree of the brine was measured to be 29. The atomized water droplet size was set to 1000μm and evaporated. After evaporation and loss of 5% of the water, the brine was introduced into the fourth-stage spray tank. At this time, the precipitate in the third-stage spray tank was potassium and sodium compounds. The size of the third-stage spray tank was 20m×14m×8m.

[0081] (5) The Baume degree of the brine was measured to be 31. The atomized water droplet size was set to 1200 μm and evaporation was carried out. After the brine reached the saturation point of the phase diagram, the evaporator was stopped and allowed to settle. At this time, the precipitate in the fourth-stage spray tank was potassium compound. The size of the fourth-stage spray tank was 18m×12m×8m.

[0082] 3. The composition of the potassium compound precipitate obtained during the process is shown in Table 2:

[0083] Table 2. Precipitated components of potassium compounds

[0084] Li (mg / L) Mg (mg / L) Cl (mg / L) Na (mg / L) K (mg / L) 463 46 59781 1428 19723

[0085] Example 2

[0086] The similarities between this embodiment and Embodiment 1 will not be repeated here. The differences between this embodiment and Embodiment 1 are as follows:

[0087] 2. Concentration steps:

[0088] (1) The original brine was introduced into the original brine tank. The Baumé degree of the original brine was measured to be 25 using a Baumé meter. The atomized water droplet particle size was set to 1000μm and evaporated. After evaporation and loss of 15% of the water, the brine was introduced into the first-stage spray tank. At this time, there was no sediment in the original brine tank.

[0089] (2) The Baumé degree of the brine was measured to be 27 again using a Baumé meter. The atomized water droplet size was set to 1000 μm and evaporation was carried out. After evaporation and loss of 15% of the water, the brine was introduced into the second-stage spray tank. At this time, there was no sediment in the first-stage spray tank.

[0090] (3) The Baumé degree of the brine was measured to be 29 again using a Baumé meter. The atomized water droplet size was set to 1200 μm and evaporation was carried out. After evaporation and loss of 10% of the water, the brine was introduced into the third-stage spray tank. At this time, the precipitate in the second-stage spray tank was sodium chloride.

[0091] (4) The Baumé degree of the brine was measured to be 31 again using a Baumé meter. The atomized water droplet size was set to 1200 μm and evaporation was carried out. After evaporation and loss of 10% of the water, the brine was introduced into the fourth-stage spray tank. At this time, the precipitate in the third-stage spray tank was potassium and sodium compounds.

[0092] (5) The Baume degree of the brine was measured to be 32. The atomized water droplet size was set to 1400 μm and evaporation was carried out. After the brine reached the saturation point of the phase diagram, the evaporator was stopped and allowed to settle. At this time, the precipitate in the fourth-stage spray tank was potassium compound.

[0093] 3. The composition of the potassium compound precipitate obtained during the process is shown in Table 3:

[0094] Table 3. Precipitated components of potassium compounds

[0095] Li (mg / L) Mg (mg / L) Cl (mg / L) Na (mg / L) K (mg / L) 492 63 65327 1677 23139

[0096] Example 3

[0097] 1. The raw material composition is shown in Table 4:

[0098] Table 4. Composition of Halogen Elements

[0099]

[0100]

[0101] 2. Concentration steps:

[0102] (1) The original brine was introduced into the original brine tank. The Baumé degree of the original brine was measured to be 12 using a Baumé meter. The atomized water droplet particle size was set to 40μm. Evaporation was carried out. After 40% of the water was lost through evaporation, the brine was introduced into the first-stage spray tank. At this time, there was no sediment in the original brine tank. The size of the original brine tank was 28m×20m×8m.

[0103] (2) The Baumé degree of the brine was measured to be 20 again using a Baumé meter. The atomized water droplet size was set to 40μm and evaporation was carried out. After evaporation and loss of 40% of the water, the brine was introduced into the second-stage spray tank. At this time, the precipitate in the first-stage spray tank was sodium compound. The size of the first-stage spray tank was 25m×18m×8m.

[0104] (3) The Baumé degree of the brine was measured to be 26 again using a Baumé meter. The atomized water droplet size was set to 100μm and evaporation was carried out. After evaporation and loss of 30% of the water, the brine was introduced into the third-stage spray tank. At this time, the precipitate in the second-stage spray tank was potassium and sodium compounds. The size of the second-stage spray tank was 22m×16m×8m.

[0105] (4) The Baume degree of the brine was measured to be 31. The atomized water droplet particle size was set to 100 μm and evaporation was carried out. After the brine reached the saturation point of the phase diagram, the evaporator was stopped and allowed to settle. At this time, the precipitate in the three-stage spray tank was potassium, sodium and magnesium compounds. The size of the three-stage spray tank was 20m×14m×8m.

[0106] 3. The composition of potassium, sodium, and magnesium compound precipitates obtained during the process is shown in Table 5:

[0107] Table 5. Precipitated Compositions of Potassium, Sodium, and Magnesium Compounds

[0108] Li (mg / L) Mg (mg / L) Cl (mg / L) Na (mg / L) K (mg / L) 35237 73 61028 1613 18

[0109] Example 4

[0110] The similarities between this embodiment and Embodiment 3 will not be repeated here. The differences between this embodiment and Embodiment 3 are as follows:

[0111] 2. Concentration steps:

[0112] (1) The original brine is introduced into the original brine tank. The Baumé degree of the original brine is measured to be 20 using a Baumé meter. The atomized water droplet particle size is set to 150μm. Evaporation is carried out. After 50% of the water is lost through evaporation, the brine is introduced into the first-stage spray tank. At this time, there is no sediment in the original brine tank.

[0113] (2) The Baumé degree of the brine was measured to be 26 again using a Baumé meter. The atomized water droplet size was set to 150 μm and evaporation was carried out. After 50% of the water was lost through evaporation, the brine was introduced into the second-stage spray tank. At this time, the precipitate in the first-stage spray tank was sodium compound.

[0114] (3) The Baumé degree of the brine was measured to be 31 again using a Baumé meter. The atomized water droplet size was set to 300 μm and evaporation was carried out. After evaporation and loss of 40% of the water, the brine was introduced into the third-stage spray tank. At this time, the precipitate in the second-stage spray tank was potassium and sodium compounds.

[0115] (4) The Baume degree of the brine was measured to be 34. The atomized water droplet size was set to 300 μm and evaporation was carried out. After the brine reached the saturation point of the phase diagram, the evaporator was stopped and allowed to settle. At this time, the precipitate in the three-stage spray tank was potassium, sodium and magnesium compounds.

[0116] 3. The composition of potassium, sodium, and magnesium compound precipitates obtained during the process is shown in Table 6:

[0117] Table 6. Precipitated Compositions of Potassium, Sodium, and Magnesium Compounds

[0118] Li (mg / L) Mg (mg / L) Cl (mg / L) Na (mg / L) K (mg / L) 47236 92 83201 1873 12

[0119] Comparative Example 1

[0120] (1) The original brine from Example 1 was placed in a drying tank and naturally dried under sunlight to extract potassium. The drying tank had dimensions of 28m × 20m × 8m. The composition of the precipitate is shown in Table 7.

[0121] Table 7. Components of Sediment Deposits from Natural Sun-Drying

[0122] Li (mg / L) Mg (mg / L) Cl (mg / L) Na (mg / L) K (mg / L) 358 72 30975 1261 10342

[0123] Comparing Table 7 with Table 3, the potassium extraction method of this application increased the contents of Li, Cl, Na, and K in the compound, with the largest increases in Cl and K. The extracted K content was 19723 mg / L, while the traditional method only yielded 10342 mg / L, representing an increase of 47.6%. The extracted Li, Cl, and Na contents were also higher than those obtained using the traditional method. Li increased by 105 mg / L, Cl by 28806 mg / L, and Na by 167 mg / L.

[0124] This indicates that this method can effectively improve the extraction rate of the target substance K, while also increasing the extraction rates of Li, Cl, and Na. By real-time monitoring and control of parameters such as atomized water droplet size and atomization time, it ensures that the saturation trajectory of the brine in the phase diagram coincides with the target saturation trajectory, thus more effectively achieving the precipitation of different substances and improving concentration efficiency. Overall, this method is superior to traditional methods in extracting target substances.

[0125] (2) The original brine from Example 3 was placed in a drying tank and naturally dried under sunlight to extract lithium. The drying tank had dimensions of 28m × 20m × 8m. The composition of the precipitate is shown in Table 8.

[0126] Table 8. Components of Sediment Deposits from Natural Sun-Drying

[0127] Li (mg / L) Mg (mg / L) Cl (mg / L) Na (mg / L) K (mg / L) 13219 43 23059 1264 15

[0128] Comparing Table 8 with Table 6, the Li content extracted using the method of this application is 47236 mg / L, while the content extracted using the traditional method is only 358 mg / L, which is 130 times higher. The contents of Mg, Cl and Na extracted using the new method are also significantly higher than those extracted using the traditional method, increasing by 20 mg / L, 52326 mg / L and 612 mg / L respectively.

[0129] This indicates that the new method can significantly improve the extraction rate of the target substance Li, while also effectively increasing the extraction rates of Mg, Cl, and Na. Through real-time monitoring and parameter optimization, the brine saturation state is better matched to the target, thus achieving highly efficient substance separation and concentration. Therefore, the new method is superior to traditional methods in extracting Li.

[0130] Based on the preferred embodiments of the present invention described above, those skilled in the art can make various changes and modifications without departing from the inventive concept. The technical scope of this invention is not limited to the contents of the specification, but must be determined according to the scope of the claims.

Claims

1. A method for brine atomization evaporation concentration, comprising the following steps: S1, initial detection: the initial Baume degree and the substance content of the original brine are measured, and the original brine is introduced into the original brine pool according to the planned evaporation rate obtained according to the purification process and the corresponding target precipitated substance; wherein the formula of the planned evaporation rate is , C is the evaporation rate, B is the Baume degree of the brine after evaporation, and b is the Baume degree of the brine before evaporation; the purification process includes a potassium extraction process and a lithium extraction process; the atomized water droplet particle size in the potassium extraction process ranges from 500 to 2000 μm, and the evaporation rate is 5 to 15%; the Li + content in the original brine in the lithium extraction process is 0.05 to 0.2 g / L, the atomized water droplet particle size ranges from 40 to 500 μm, and the evaporation rate is 30 to 50%. S2, calculating parameters: calculating corresponding phase diagram, target saturation trajectory and target saturation point according to target precipitated substance; S3, setting parameters: setting initial atomized water droplet particle size, water evaporation amount and atomization time according to real-time wind data and planned evaporation rate, the real-time wind data including wind speed and wind direction; wherein the specific steps for setting the atomization time are: S31, calculating water evaporation amount, formula is ; wherein, E is water evaporation amount, unit is kg / m 2 ·s, K is mass transfer coefficient, is 0.1-3 kg / (m 2 ·s·Pa), ρ1 is water vapor pressure, unit is Pa, ρ s is saturated water vapor pressure, unit is Pa, u is wind speed, unit is m / s; S32, calculate the evaporation time, the formula is wherein t is the evaporation time, the unit is s, M is the amount of water to be evaporated, the unit is kg, A is the evaporation area, the unit is m 2 , and E is the average evaporation rate calculated in S32. S4, atomization evaporation: starting the atomization evaporation process, monitoring the real-time Baume degree of the brine, the real-time state of the precipitated substance and the real-time wind data, adjusting the atomized water droplet particle size and the atomization time, and ensuring that the saturation trajectory of the brine in the phase diagram overlaps with the target saturation trajectory; S5, repeating steps S2-S4 to precipitate different substances, and introducing the brine obtained in S4 into the next stage of the spray pond for continuous atomization evaporation, when the saturation point of the brine in the phase diagram coincides with the target saturation point, stopping the evaporation and performing static setting.

2. A method of brine atomization evaporation concentration according to claim 1, characterized in that: In the potassium extraction process, the Baume degree of the brine changes in the range of 23-32 °Bé.

3. The method of claim 1, wherein: In the lithium extraction process, the Baume degree of the brine changes in the range of 12-34 °Bé.

4. The method of claim 1, wherein: In the S5, the area S of the spray pool gradually decreases with the increase of the number n of the spray pool, and the formula is wherein S0 is the initial area of the original halogen pool, and k is the area reduction rate, ranging from 0.85 to 0.

92.

5. The method of claim 1, wherein: In the S4, the specific steps for adjusting the atomized water droplet particle size and the atomization time are: the real-time saturation trajectory is lower than the target trajectory, indicating that the evaporation rate is too low, the atomized water droplet particle size is reduced or the atomization time is prolonged, the real-time saturation trajectory is higher than the target trajectory, indicating that the evaporation rate is too high, the atomized water droplet particle size is increased or the atomization time is shortened.

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