Method for improving utilization of the completion fluid

Abstract

The application provides a method for improving utilization of a halogen replacement completion liquid. The method for improving utilization of the halogen replacement completion liquid comprises: performing first halogen replacement on E halogen and first F halogen to obtain first halogen replacement completion liquid and first carnallite; and performing second halogen replacement on the first halogen replacement completion liquid and second F halogen to obtain second halogen replacement completion liquid and second carnallite. Compared with a traditional method of directly discharging and treating the halogen replacement completion liquid as waste liquid, the first halogen replacement completion liquid obtained in a halogen replacement-cold crystallization method is subjected to second halogen replacement with fresh second F halogen, so that potassium chloride in the first halogen replacement completion liquid is separated out, the utilization of the first halogen replacement completion liquid is improved through recycling, and the potassium chloride in the first halogen replacement completion liquid is recovered, thereby reducing the loss of potassium chloride. The method can be applied to the field of potassium chloride production, and the second carnallite can be used to prepare potassium chloride, thereby reducing the loss of potassium chloride.

Description

Technical Field

[0001] This invention relates to the field of potassium chloride production technology, and more specifically, to a method for improving the utilization rate of brine concentrate. Background Technology

[0002] The "halogenation-cold crystallization method" involves mixing the E-halogen mother liquor (containing potassium chloride, sodium chloride, and carnallite, all saturated) with the F-halogen mother liquor (containing magnesium chloride, sodium chloride, and carnallite, all saturated). This process results in the co-precipitation of carnallite and a small amount of sodium chloride. The mechanism is as follows: after the two salt solutions are mixed, the mixed liquid falls into the carnallite phase region and is located below the dissolution curves of sodium chloride and carnallite on the phase diagram and the saturation surface of carnallite. Therefore, the mixed liquid is in a supersaturated state, and it will precipitate a certain amount of salt. Because it is in the carnallite phase region, carnallite precipitates first. After sodium chloride becomes saturated, carnallite and sodium chloride precipitate together until the brine is saturated. The amount of precipitated solid phase (carnallite and sodium chloride) is very small compared to the brine, which means that the brineation process is essentially a process of processing a large amount of liquid.

[0003] In the "brine-cold crystallization" production process, the brine-drinking liquid is discharged into the salt field as wastewater. The brine-drinking liquid contains potassium-containing carnallite that has not been reused. These potassium-containing carnallite deposits in the salt pond to form a high-sodium carnallite pool. This pool cannot be reused in the brine-drinking process, resulting in a low recycling rate.

[0004] Therefore, researching and developing a method to improve the utilization rate of the brine-mixing solution is of great significance for increasing the yield of potassium chloride. Summary of the Invention

[0005] The main objective of this invention is to provide a method for improving the utilization rate of brine dilution solution, in order to solve the problem that brine dilution solution is usually discharged as wastewater in the prior art, resulting in a large loss of potassium chloride.

[0006] To achieve the above objectives, the present invention provides a method for improving the utilization rate of brine-mixing solution. The method includes: performing a first brine-mixing with a first brine (E-halogen) and a first brine (F-halogen) to obtain a first brine-mixing solution and a first carnallite; and performing a second brine-mixing with a second brine (F-halogen) to obtain a second brine-mixing solution and a second carnallite.

[0007] Furthermore, the ratio of E halide to the first F halide is 1:(1.12 to 1.25); preferably, the Baumé degree of E halide is 28 to 33°Be′, and the Baumé degree of the first F halide is 34 to 37°Be′.

[0008] Furthermore, the ratio of the first brine-mixed liquid to the second brine is 1:(0.5 to 0.9); preferably, the Baume degree of the first brine-mixed liquid is 32 to 33°Be′, and the Baume degree of the second brine is 35 to 37°Be′.

[0009] Furthermore, the temperature of the second brine mixing process is 0 to 25°C; preferably, when the temperature of the second brine mixing is 20°C, the brine mixing ratio of the first brine mixing solution to the second brine F is 1:(0.5 to 0.6).

[0010] Furthermore, based on the weight percentage of the E halide, the E halide comprises 23–27 wt% magnesium chloride, 2–3 wt% potassium chloride, 1.8–3.2 wt% sodium chloride, and the balance being moisture.

[0011] Furthermore, by weight percentage, the first or second F halide comprises 32–37 wt% magnesium chloride, 0.15–0.45 wt% potassium chloride, 0.2–0.6 wt% sodium chloride, and the balance being moisture.

[0012] Furthermore, the process between the first and second brine additions includes a stirring process and a settling process, resulting in the second brine addition solution and the first carnallite.

[0013] Furthermore, the stirring process takes 30–50 minutes and the rotation speed is 30–50 r / min.

[0014] Furthermore, the settling time is 15–20 min, and the temperature is 0–25℃.

[0015] To achieve the above objectives, another aspect of the present invention provides an application of the method for improving the utilization rate of the brine preparation solution provided in this application in the field of potassium chloride production.

[0016] Compared to traditional methods that directly discharge the brine-mixing solution as waste liquid, this application utilizes the technical solution of the present invention to perform a second brine-mixing process by mixing the first brine-mixing solution obtained during the brine-mixing-cold crystallization process with fresh second brine (F). This process precipitates potassium chloride from the first brine-mixing solution, improving its utilization rate by reusing the first brine-mixing solution, thereby recovering potassium chloride and reducing potassium chloride loss. Applying this method to the production of potassium chloride enables the preparation of potassium chloride using second carnallite, further reducing potassium chloride loss. Attached Figure Description

[0017] The accompanying drawings, which form part of this application, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:

[0018] Figure 1The phase diagram of the quaternary water-salt system in the second brine mixing process of Example 1 is shown;

[0019] Figure 2 A process flow diagram for the preparation of potassium chloride in Example 1 is shown. Detailed Implementation

[0020] It should be noted that, unless otherwise specified, the embodiments and features described in this application can be combined with each other. The present invention will now be described in detail with reference to the embodiments.

[0021] As described in the background section, existing brine-cold crystallization processes suffer from the problem that the brine-mixing solution is typically discharged as wastewater, resulting in significant potassium chloride loss. To address this technical problem, this application provides a method for improving the utilization rate of the brine-mixing solution. This method includes: performing a first brine-mixing process with a first brine (E) and a first brine (F) to obtain a first brine-mixing solution and a first carnallite; and performing a second brine-mixing process with a second brine (F) to obtain a second carnallite.

[0022] Compared to traditional methods that directly discharge the brine-mixing solution as waste, this application involves a second brine-mixing process using the first brine-mixing solution obtained during the brine-mixing-cold crystallization method. This process involves mixing the first brine-mixing solution with fresh second brine (F) to extract potassium chloride from the first solution. By reusing the first brine-mixing solution, its utilization rate is improved, thereby recovering potassium chloride and reducing its loss. Applying this method to potassium chloride production allows for the use of second carnallite to prepare potassium chloride, further reducing potassium chloride loss.

[0023] It should be noted that the halogen ratio in this application refers to the volume ratio. Baumé degree (°Be′) is a method for expressing solution concentration.

[0024] In a preferred embodiment, the ratio of E halogen to the first F halogen is 1:(1.12 to 1.25). The ratio of E halogen to the first F halogen includes, but is not limited to, the above range. Limiting it to the above range is beneficial to improving the generation rate of the first halogenated liquid, thereby improving its recycling rate.

[0025] To further improve the generation rate and recycling rate of the first brine solution, the preferred Baumé degree of the E brine is 28–33°Be′, and the preferred Baumé degree of the first F brine is 34–37°Be′.

[0026] In a preferred embodiment, the ratio of the first brine-mixing solution to the second brine F is 1:(0.5-0.9). The ratio of the first brine-mixing solution to the second brine F is not limited to the above range. Limiting it to the above range is beneficial to improving the brine mixing effect of the second brine, thereby improving the recovery rate of the first brine-mixing solution, and further improving the yield of potassium chloride obtained from the subsequent potassium chloride preparation process.

[0027] To further improve the brine mixing effect of the second brine mixing and further improve the recovery rate of the first brine mixing solution, preferably, the Baume degree of the first brine mixing solution is 32-33°Be′ and the Baume degree of the second brine is 35-37°Be′.

[0028] In a preferred embodiment, the temperature of the second brine addition process is 0–25°C. The temperature of the second brine addition process includes, but is not limited to, the above range. Limiting it to this range is beneficial for improving the brine addition effect of the second process, thereby improving the recovery rate of the first brine addition solution, and further improving the yield of potassium chloride obtained from the subsequent potassium chloride preparation process.

[0029] In order to further improve the recovery rate of the first brine preparation solution and thus further improve the yield of potassium chloride obtained by the subsequent potassium chloride preparation process, preferably, when the temperature of the second brine preparation is 20°C, the brine ratio of the first brine preparation solution to the second brine is 1:(0.5~0.6).

[0030] In a preferred embodiment, based on the weight percentage of brine E, brine E comprises 23-27 wt% magnesium chloride, 2-3 wt% potassium chloride, 1.8-3.2 wt% sodium chloride, and the balance being water. The content of each component in brine E includes, but is not limited to, the above range. Limiting it to the above range is beneficial to increasing the formation rate of the first brine-addition solution, thereby facilitating the subsequent second brine-addition process and increasing the yield of potassium chloride obtained from the subsequent potassium chloride preparation process.

[0031] In a preferred embodiment, the first F-halogen or the second F-halogen, by weight percentage, comprises 32–37 wt% magnesium chloride, 0.15–0.45 wt% potassium chloride, 0.2–0.6 wt% sodium chloride, and the balance being water. The content of each component in the first F-halogen or the second F-halogen includes, but is not limited to, the above range. Limiting it to the above range is beneficial to improving the recovery rate of the first brine preparation solution, thereby improving the yield of potassium chloride obtained from the subsequent potassium chloride preparation process.

[0032] In a preferred embodiment, the process between the first and second brine additions includes a stirring process and a settling process, resulting in a second brine-added liquid and a first carnallite. Stirring ensures thorough mixing of the E brine and the first F brine, while settling separates the precipitated solids (such as the first carnallite) from the first brine-added liquid, facilitating its collection.

[0033] In a preferred embodiment, the stirring process takes 30–50 minutes and rotates at a speed of 30–50 r / min. The stirring time and speed include, but are not limited to, the above ranges. Limiting them to these ranges helps to ensure a more uniform mixing of the E brine and the first F brine, thereby increasing the formation rate of the first brine-mixed liquid and consequently improving its recycling rate.

[0034] In a preferred embodiment, the settling time is 15–20 min, and the temperature is 0–25°C. The settling time and temperature include, but are not limited to, the above ranges. Limiting them to the above ranges is beneficial to improving the separation efficiency of the first brine-mixing solution and the first carnallite, thereby improving the generation rate of the first brine-mixing solution and thus improving the recovery rate of the first brine-mixing solution.

[0035] In a preferred embodiment, the carnallite comprises 29-35 wt% magnesium chloride, 19-25 wt% potassium chloride, 3-11 wt% sodium chloride, and the balance being water, based on the weight percentage of the first carnallite.

[0036] The second aspect of this application also provides an application of the method for improving the utilization rate of the brine finishing solution provided in this application in the field of potassium chloride production.

[0037] Compared to traditional methods that directly discharge the brine-mixing solution as waste, this application involves a second brine-mixing process using the first brine-mixing solution obtained during the brine-mixing-cold crystallization method. This process involves mixing the first brine-mixing solution with fresh second brine (F) to extract potassium chloride from the first solution. By reusing the first brine-mixing solution, its utilization rate is improved, thereby recovering potassium chloride and reducing its loss. Applying this method to potassium chloride production allows for the use of second carnallite to prepare potassium chloride, further reducing potassium chloride loss.

[0038] The present application will be further described in detail below with reference to specific embodiments, which should not be construed as limiting the scope of protection claimed in the present application.

[0039] Example 1

[0040] A method for improving the utilization rate of brine concentrate includes:

[0041] (1) At 15℃, E brine and the first F brine were mixed at a ratio of 1:1.15. The mixture was stirred and allowed to settle. The stirring time was 20 min and the rotation speed was 40 r / min. After stirring, the mixture was allowed to settle at 15℃ for 36 h to obtain the first brine mixture and the first carnallite.

[0042] The first carnallite obtained in step (1) comprises 33.5 wt% MgCl2, 23.4 wt% KCl, 4.9 wt% NaCl and the balance water, by weight percentage.

[0043] (2) At 15°C, the first brine-mixing solution and the second F brine are mixed for a second brine-mixing process, wherein the brine-mixing ratio of the first brine-mixing solution to the second F brine is 1:0.6, to obtain the second brine-mixing solution and the second carnallite.

[0044] The weight percentage and Baume degree of each component in the E-halogen, F-halogen, and first brine-mixed liquid of this Example 1 are shown in Table 1.

[0045] The phase diagram of the quaternary hydrosalt system during the second brine addition process is as follows: Figure 1 As shown, system point A (KCl = 0.68%, NaCl = 1.3%, MgCl2 = 30.21%) is located in the NaCl crystallization region of the dry basis diagram. Evaporation at 15℃ can be divided into the following four stages: First stage: System point A is located in the NaCl crystallization region of the dry basis diagram. On the dry basis diagram, this system point is the liquid phase point, and point A remains stationary. Second stage: During evaporation and concentration, NaCl precipitates. The solid phase point remains stationary at the NaCl point. The intersection of the solid phase point NaCl and point A is at 15℃, where carnallite and NaCl... At point D on the crystallization line, the liquidus point moves from point A to point D, and when it reaches point D, it is also saturated with Car. In the third stage, the liquidus point reaches the co-saturation line of Car and NaCl. During evaporation, Car and NaCl precipitate simultaneously. The liquid phase moves from point D to point F, and the solid phase point moves from the NaCl point to point C. When the liquidus point reaches point F, it is also saturated with MgCl2. This stage is the carnallite precipitation stage. In the fourth stage, the liquidus point reaches point F, and during evaporation, NaCl, Car, and MgCl2 will precipitate together.

[0046] Table 1

[0047] Brine Analysis Name Baumé degree (°Be′) <![CDATA[MgCl2(wt%)]]> KCl (wt%) NaCl (wt%) E-halogen 29.4 25.9 3.2 2.1 First F-brine 35.9 34.62 0.11 0.98 Second F-halogen 35.9 34.62 0.11 0.98 First brine preparation liquid completed 33.1 30.21 0.68 1.3

[0048] A method for producing potassium chloride, comprising:

[0049] (1) Same as step (1) in the above method for improving the utilization rate of brine solution;

[0050] (2) is the same as step (2) in the above method for improving the utilization rate of brine solution;

[0051] (3) After brine is added in the brine adder, low sodium carnallite is generated through instantaneous supersaturation. The carnallite settles naturally to the bottom of the brine adder and is then pumped to a thickener for thickening. The thickener is then pumped to a semi-finished product centrifuge (P-60 type) for further thickening. The carnallite is then pumped to a crystallizer by adding fresh water to decompose and crystallize the carnallite. After settling naturally, the carnallite is pumped to a finished product centrifuge (P-60 type) by a slurry pump. After being ejected from the centrifuge, the product is dried and packaged by a drying drum to obtain potassium chloride.

[0052] Example 2

[0053] The difference from Example 1 is that the ratio of E halogen to the first F halogen is 1:1.12.

[0054] Example 3

[0055] The difference from Example 1 is that the ratio of E halogen to the first F halogen is 1:1.25.

[0056] Example 4

[0057] The difference from Example 1 is that the ratio of E halide to the first F halide is 1:1.5.

[0058] Example 5

[0059] The difference from Example 1 is that the Baume degree of the E halogen is 28°Be′, and the Baume degree of the first F halogen is 37°Be′.

[0060] Example 6

[0061] The difference from Example 1 is that the Baume degree of the E halogen is 33°Be′ and the Baume degree of the first F halogen is 34°Be′.

[0062] Example 7

[0063] The difference from Example 1 is that the Baume degree of the E halogen is 34°Be′, and the Baume degree of the first F halogen is 33°Be′.

[0064] Example 8

[0065] The difference from Example 1 is that the ratio of the first brine-mixed liquid to the second brine is 1:0.5.

[0066] Example 9

[0067] The difference from Example 1 is that the ratio of the first brine-mixed liquid to the second brine is 1:0.9.

[0068] Example 10

[0069] The difference from Example 1 is that the ratio of the first brine-mixed liquid to the second brine is 1:1.

[0070] Example 11

[0071] The difference from Example 1 is that the Baume degree of the first brine solution is 32°Be′, and the Baume degree of the second F brine is 37°Be′.

[0072] Example 12

[0073] The difference from Example 1 is that the Baume degree of the first brine solution is 33°Be′, and the Baume degree of the second F brine is 35°Be′.

[0074] Example 13

[0075] The difference from Example 1 is that the Baume degree of the first brine solution is 34°Be′ and the Baume degree of the second F brine is 34°Be′.

[0076] Example 14

[0077] The difference from Example 1 is that the temperature of the second brine mixing process is 0°C.

[0078] Example 15

[0079] The difference from Example 1 is that the temperature of the second brine mixing process is 25°C.

[0080] Example 16

[0081] The difference from Example 1 is that the temperature of the second brine mixing process is -10°C.

[0082] Example 17

[0083] The difference from Example 1 is that the weight percentage and Baume degree of each component in the above-mentioned E-halogen, F-halogen and first brine-mixing solution in Example 17 are shown in Table 2.

[0084] Table 2

[0085] Brine Analysis Name <![CDATA[MgCl2(wt%)]]> KCl (wt%) NaCl (wt%) E-halogen 23 2.0 1.8 First F-brine 32 0.15 0.2 Second F-halogen 32 0.15 0.2 First brine preparation liquid completed 30.21 0.68 1.3

[0086] Example 18

[0087] The difference from Example 1 is that the weight percentage and Baume degree of each component in the above-mentioned E-halogen, F-halogen and first brine-mixing solution in Example 18 are shown in Table 3.

[0088] Table 3

[0089] Brine Analysis Name <![CDATA[MgCl2(wt%)]]> KCl (wt%) NaCl (wt%) E-halogen 27 3 3.2 First F-brine 37 0.45 0.6 Second F-halogen 37 0.45 0.6 First brine preparation liquid completed 30.85 0.72 1.75

[0090] Example 19

[0091] The difference from Example 1 is that the weight percentage and Baume degree of each component in the above-mentioned E-halogen, F-halogen and first brine-mixing solution in Example 18 are shown in Table 4.

[0092] Table 4

[0093] Brine Analysis Name <![CDATA[MgCl2(wt%)]]> KCl (wt%) NaCl (wt%) E-halogen 22 1.5 1.5 First F-brine 31 0.1 0.15 Second F-halogen 31 0.1 0.15 First brine preparation liquid completed 26.9 0.54 2.34

[0094] Comparative Example 1

[0095] A method for producing potassium chloride, comprising:

[0096] (1) At 15℃, E brine and F brine were mixed at a ratio of 1:1.15, and the mixture was stirred and allowed to settle. The stirring time was 20 min and the rotation speed was 45 r / min. After stirring, the mixture was allowed to settle at 15℃ for 36 h to obtain the mixed brine liquid and carnallite.

[0097] The carnallite obtained in step (1) comprises 32.7 wt% MgCl2, 23.57 wt% KCl, 4.68 wt% NaCl and the balance water, by weight percentage.

[0098] (2) The brine solution is discharged as waste liquid;

[0099] (3) Same as step (3) in Example 1, potassium chloride is obtained.

[0100] The components of the first brine-mixed liquid and the second first brine-mixed liquid obtained in all the above embodiments of this application, as well as the brine-mixed liquid obtained in the comparative example, were analyzed. The results are shown in Table 5.

[0101] Table 5

[0102]

[0103]

[0104] As can be seen from the above description, the embodiments of the present invention achieve the following technical effects:

[0105] Comparing Example 1 and Comparative Example 1, it can be seen that, compared to the traditional method of directly discharging the brine-mixing completed liquid as waste, this application performs a second brine-mixing with fresh second brine (F) obtained during the brine-mixing-cold crystallization process. This allows potassium chloride to be extracted from the first brine-mixing completed liquid. By reusing the first brine-mixing completed liquid, its utilization rate is improved, thereby recovering potassium chloride and reducing potassium chloride loss. Applying this method to the field of potassium chloride production enables the preparation of potassium chloride using second carnallite, thereby reducing potassium chloride loss.

[0106] Comparing Examples 1 to 4, it can be seen that the ratio of E halogen to the first F halogen is not limited to the preferred range of this application. Limiting it to the preferred range of this application is beneficial to improving the generation rate of the first halogen-mixed liquid, thereby improving the recovery rate of potassium chloride.

[0107] Comparing Examples 1, 5 to 7, it can be seen that the Baumé degree of the E halogen and the first F halogen includes, but is not limited to, the preferred range of this application. Limiting them to the preferred range of this application is beneficial to further improve the generation rate and recycling rate of the first halogenated liquid.

[0108] Comparing Examples 1, 8 to 10, it can be seen that the ratio of the first brine-mixed liquid to the second brine is not limited to the preferred range of this application. Limiting it to the preferred range of this application is beneficial to improving the brine-mixing effect of the second brine, thereby improving the recovery rate of the first brine-mixed liquid, and further improving the recovery rate of potassium chloride.

[0109] Comparing Examples 1, 11 to 13, it can be seen that the Baumé degree of the first brine-mixed liquid and the second F brine includes, but is not limited to, the preferred range of this application. Limiting it to the preferred range of this application is beneficial to further improve the potassium chloride recovery rate.

[0110] Comparing Examples 1, 14 to 16, it can be seen that the temperature of the second brine addition process includes, but is not limited to, the preferred range of this application. Limiting it to the preferred range of this application is beneficial to improving the brine addition effect of the second brine addition, thereby improving the recovery rate of the first brine addition solution, and further improving the potassium chloride recovery rate.

[0111] Comparing Examples 1, 17 to 19, it can be seen that, compared with other ranges, limiting the content of each component in the E-halogen, F-halogen and the first brine-mixing solution to the preferred range of this application is beneficial to improving the recovery rate of the first brine-mixing solution, thereby improving the yield of potassium chloride obtained by the subsequent potassium chloride preparation process.

[0112] It should be noted that the terms "first," "second," etc., used in the specification and claims of this application are used to distinguish similar objects and are not necessarily used to describe a specific order or sequence. It should be understood that such terms can be used interchangeably where appropriate so that the embodiments of this application described herein can be implemented, for example, in a sequence other than those described herein.

[0113] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A method for improving the utilization of a brine-replacement completion fluid, characterized by, The method for improving utilization of a mixed halite solution comprises: first mixing E halite with first F halite to obtain first mixed halite solution and first carnallite; second mixing the first mixed halite solution with second F halite to obtain second mixed halite solution and second carnallite; wherein the mixing ratio of the first mixed halite solution to the second F halite is 1:(0.5-0.9); the temperature of the second mixing process is 0-25°C.

2. The method for improving utilization of a completed liquid for a halogen exchange according to claim 1, characterized by, the mixing ratio of the E halite to the first F halite is 1:(1.12-1.25); the E halite has a Baume degree of 28-33°Be', and the first F halite has a Baume degree of 34-37°Be'.

3. The method for improving the utilization rate of the produced liquid according to claim 1 or 2, characterized in that, the first mixed halite solution has a Baume degree of 32-33°Be', and the second F halite has a Baume degree of 35-37°Be'.

4. The method for improving utilization of a completed liquid for a brine exchange according to claim 3, characterized by, when the temperature of the second mixing is 20°C, the mixing ratio of the first mixed halite solution to the second F halite is 1:(0.5-0.6).

5. The method for improving the utilization rate of the produced liquid according to claim 1 or 2, characterized in that, the E halite comprises 23-27wt% magnesium chloride, 2-3wt% potassium chloride, 1.8-3.2wt% sodium chloride, and the rest is water, based on the weight percentage of the E halite.

6. The method of improving the utilization of the produced brine according to claim 5, characterized in that, the first F halite or the second F halite comprises 32-37wt% magnesium chloride, 0.15-0.45wt% potassium chloride, 0.2-0.6wt% sodium chloride, and the rest is water, based on the weight percentage.

7. The method for improving the utilization rate of the produced liquid according to claim 1 or 2, characterized in that, the first mixing and the second mixing further comprise stirring process and standing and precipitation process in sequence, to obtain the second mixed halite solution and the first carnallite.

8. The method of improving the utilization of the produced brine according to claim 7, characterized in that, the stirring process has a time of 30-50min and a rotation speed of 30-50r / min.

9. The method of improving the utilization of the produced brine according to claim 8, characterized in that, the standing and precipitation process has a time of 15-20min and a temperature of 0-25°C.

10. Application of the method for improving utilization of a mixed halite solution according to any one of claims 1-9 in the field of producing potassium chloride.

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