CN219469849U - Equipment for monitoring concentration of lithium precipitated in brine in real time - Google Patents

Abstract

The utility model discloses equipment for monitoring the concentration of lithium precipitated in real time, which relates to the technical field of lithium mica roasting and extracting equipment, and further comprises iron aluminum fluoride calcium ion removing equipment, real-time ion detecting equipment, lithium carbonate lithium precipitating equipment and an MVR evaporation crystallization device. Through the technical scheme provided by the application, compared with the existing lithium carbonate production equipment, the method can monitor the content of impurities in the filtered brine in real time, effectively remove magnetic metal impurities, ensure the effect of removing impurities from the brine, and improve the yield and quality of lithium carbonate products.

Description

Equipment for monitoring concentration of lithium precipitated in brine in real time

Technical Field

The utility model relates to the technical field of lepidolite roasting lithium extraction equipment, in particular to lithium carbonate production equipment capable of being used for monitoring a brine impurity removal process in real time.

Background

Lithium is the lightest metal element in nature, is known as "21 st century energy metal", and metals and compounds thereof are widely used in the fields of batteries, glass ceramics, aerospace and the like. The upstream is mainly raw material; midstream is a product; downstream is the application result and field, and in recent years, the global demand for lithium carbonate materials has been increasing. The traditional process for extracting lithium carbonate by taking lepidolite as a raw material mainly comprises a salt pressure cooking method, an alkali pressure cooking method, a sulfuric acid method, a sulfate method and the like, the lithium extraction process of the lithium ore can cause high energy consumption and large corrosion to equipment in the production process, and meanwhile, the leached brine needs to be subjected to concentration and impurity removal stages.

The thoroughness of leaching brine impurity removal and the real-time monitoring to impurity ion concentration can efficient promote quality and output of lithium carbonate product, and to salt lake brine, impurity removal technology has directly decided lithium ion and can be high-efficient by heavy lithium output lithium carbonate, and the real-time detection of demagnetization and impurity ion can in time provide equipment or raw materials and need adjust production technical direction, therefore, need a lithium carbonate production facility that can be used for real-time monitoring brine impurity removal process.

Disclosure of Invention

In order to solve the technical problems in the background technology, the utility model provides equipment for monitoring the concentration of the precipitated lithium in real time.

The utility model provides equipment for monitoring the concentration of lithium precipitated in real time, which comprises precipitating, impurity removing and batching equipment, iron aluminum fluoride calcium ion removing equipment, real-time ion detecting equipment, lithium carbonate lithium precipitating equipment and an MVR evaporation crystallization device;

the discharge end of the precipitation impurity removal batching equipment is connected with the feed end of the iron aluminum fluoride calcium ion removal equipment, the discharge end of the iron aluminum fluoride calcium ion removal equipment is connected with the feed end of the real-time ion detection equipment, the discharge end of the real-time ion detection equipment is connected with the feed end of the lithium carbonate precipitation equipment, and the discharge end of the lithium carbonate precipitation equipment is connected with the feed end of the MVR evaporation crystallization device.

Preferably, the precipitation impurity removal batching equipment comprises a first batching tank, a second batching tank and a third batching tank, wherein the discharge end of the first batching tank is connected with the feed end of the second batching tank, the discharge end of the second batching tank is connected with the feed end of the third batching tank, and the discharge end of the third batching tank is connected with the feed end of the iron-aluminum-fluorine-calcium ion removal equipment.

Preferably, the iron aluminum fluoride calcium ion removing device comprises a transfer kettle, a first pressure plate filter, a second pressure plate filter, a pipeline demagnetizing device and an ion exchange resin device, wherein the pipeline demagnetizing device can adsorb out magnetic substances which cannot be filtered in the plate filter, the feeding end of the transfer kettle is connected with the discharging end of the precipitation impurity removing and proportioning device, the discharging end of the transfer kettle is connected with the feeding end of the first pressure plate filter, the discharging end of the first pressure plate filter is connected with the feeding end of the second pressure plate filter, the discharging end of the second pressure plate filter is connected with the feeding end of the pipeline demagnetizing device, and the discharging end of the pipeline demagnetizing device is connected with the feeding end of the ion exchange resin device.

Preferably, the pipeline demagnetizing device comprises a feeding port of brine, a discharging port of the brine and a step-entering strong magnetic rod, wherein the step-entering strong magnetic rod is used for removing magnetic impurities, the feeding port of the brine is connected with the discharging end of the second pressing plate filter, and the discharging port of the brine is connected with the feeding end of the ion exchange resin device.

Preferably, the pipeline demagnetizing device consists of one or more of permanent magnetic equipment and electromagnetic equipment.

Preferably, the real-time ion detection device comprises an ion component and concentration monitoring device, and the ion component and concentration monitoring device is used for monitoring the ion component and concentration in the brine filtrate after impurity removal.

Preferably, the ion component and concentration monitoring device is composed of several of an atomic absorption spectrophotometer, an ICP and a point position titrator.

Preferably, the lithium carbonate precipitation equipment comprises a fourth proportioning tank, a buffer tank, a third pressing plate filter and drying equipment, wherein the third pressing plate filter is used for generating lithium carbonate products and filtrate, and the lithium carbonate products and filtrate generated by the third pressing plate filter respectively enter the drying equipment and the MVR evaporation crystallization device.

Preferably, the MVR evaporation crystallization device comprises a fifth proportioning tank and an MVR device, wherein the discharge end of the fifth proportioning tank is connected with the feed end of the MVR device, and the MVR device is used for evaporating and crystallizing the lithium-precipitated brine.

1. According to the equipment for monitoring the concentration of the precipitated lithium in real time, which is provided by the utility model, the defect in the impurity removal process can be efficiently regulated by utilizing the ion component and the concentration monitoring device to monitor the impurity component and the impurity content of the purified brine, the impurity removal capacity can be further supplemented by the pipeline magnetic removal device, the impurity removal effect of the brine is ensured, and therefore, the yield of certain lithium carbonate is improved, and the quality is improved.

2. The equipment for monitoring the concentration of the lithium precipitation in real time can effectively realize multi-component utilization, and has the advantages of simple operation flow, low investment cost and high production efficiency.

Additional aspects and advantages of the utility model will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the utility model.

Drawings

FIG. 1 is a front view of the present utility model;

FIG. 2 is a schematic diagram of a pipeline demagnetizing device according to the present utility model.

In the figure, 10, precipitating and impurity-removing batching equipment; 11. a first material distribution groove; 12. a second material distribution groove; 13. a third material distribution groove;

20. iron aluminum fluorine calcium ion removing equipment; 21. a transfer kettle; 22. a first platen filter; 23. a second platen filter; 24. a pipeline demagnetizing device; 241. a feed inlet; 242. a discharge port; 243. step-in strong magnetic rod; 25. an ion exchange resin device;

30. a real-time ion detection device; 31. ion component and concentration monitoring device;

40. lithium carbonate lithium precipitation equipment; 41. a fourth material mixing tank; 42. a buffer tank; 43. a third platen filter; 44. a drying device;

50. MVR evaporation crystallization device; 51. a fifth material mixing tank; 52. MVR device;

61. a first dispensing centrifugal pump; 62. a second dispensing centrifugal pump; 63. a third dosing centrifugal pump; 64. a first precipitation underflow pump; 65. a first filtering centrifugal pump; 66. a first buffer centrifugal pump; 67. a second buffer centrifugal pump; 68. a second precipitation underflow pump; 69. a second filtering centrifugal pump.

Detailed Description

Embodiments of the present utility model are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar symbols indicate like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are exemplary only for explaining the present utility model and are not to be construed as limiting the present utility model.

It is to be understood that the terms "center," "longitudinal," "transverse," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counter-clockwise," "axial," "radial," "circumferential," and the like are directional or positional relationships as indicated based on the drawings, merely to facilitate describing the utility model and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be configured and operated in a particular orientation, and therefore should not be construed as limiting the utility model.

Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present utility model, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.

In the present utility model, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; may be mechanically connected, may be electrically connected or may be in communication with each other; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art according to the specific circumstances.

In the present utility model, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.

Referring to fig. 1-2, the utility model provides a device for monitoring the concentration of lithium precipitated in real time, which comprises a precipitation impurity removal batching device 10, an iron aluminum fluorine calcium ion removal device 20, a real-time ion detection device 30, a lithium carbonate precipitation lithium device 40 and an MVR evaporation crystallization device 50;

the discharge end of the precipitation impurity removal batching equipment 10 is connected with the feed end of the iron aluminum fluoride calcium ion removal equipment 20, the discharge end of the iron aluminum fluoride calcium ion removal equipment 20 is connected with the feed end of the real-time ion detection equipment 30, the discharge end of the real-time ion detection equipment 30 is connected with the feed end of the lithium carbonate precipitation equipment 40, and the discharge end of the lithium carbonate precipitation equipment 40 is connected with the feed end of the MVR evaporation crystallization device 50.

Further, the precipitation impurity removal batching apparatus 10 comprises a first batching chute 11, a second batching chute 12 and a third batching chute 13, wherein the discharge end of the first batching chute 11 is connected with the feed end of the second batching chute 12, the discharge end of the second batching chute 12 is connected with the feed end of the third batching chute 13, the discharge end of the third batching chute 13 is connected with the feed end of the iron-aluminum-fluorine-calcium ion removing apparatus 20, brine sequentially passes through the first batching chute 11, the second batching chute 12 and the third batching chute 13, the first batching chute 11 is connected with the second batching chute 12 through a first batching centrifugal pump 61, and the second batching chute 12 is connected with the third batching chute 13 through a second batching centrifugal pump 62.

Further, the iron aluminum fluoride calcium ion removing device 20 comprises a transfer kettle 21, a first pressure plate filter 22, a second pressure plate filter 23, a pipeline demagnetizing device 24 and an ion exchange resin device 25, the pipeline demagnetizing device 24 can adsorb out magnetic substances which are not filtered in the plate filter, further, the purity of a lithium carbonate product is effectively improved, the feeding end of the transfer kettle 21 is connected with the discharging end of the precipitation impurity removing batching device 10, the discharging end of the transfer kettle 21 is connected with the feeding end of the first pressure plate filter 22, the discharging end of the first pressure plate filter 22 is connected with the feeding end of the second pressure plate filter 23, the discharging end of the second pressure plate filter 23 is connected with the feeding end of the pipeline demagnetizing device 24, the discharging end of the pipeline demagnetizing device 24 is connected with the feeding end of the ion exchange resin device 25, the third batching centrifugal pump 63 is connected with the transfer kettle 21, the transfer kettle 21 is connected with the first pressure plate filter 22 through the first precipitation pump 64, and the underflow filter 23 is connected with the second pressure plate filter 23 through the first filtering centrifugal pump 65.

Further, the pipeline demagnetizing device 24 comprises a feeding hole 241 of the brine, a discharging hole 242 of the brine and a step-in strong magnetic rod 243, the step-in strong magnetic rod 243 is used for removing magnetic impurities, the purity of the lithium carbonate product is improved, the feeding hole 241 of the brine is connected with the discharging end of the second pressing plate filter 23, the discharging hole 242 of the brine is connected with the feeding end of the ion exchange resin device 25, the pipeline demagnetizing device 24 comprises a tank body, the feeding hole 241 of the brine and the discharging hole 242 of the brine are formed in the tank body, and the step-in strong magnetic rod 243 is fixedly connected to the inner wall of the tank body.

Further, the pipe demagnetizing device 24 is composed of one or more of a permanent magnet device and an electromagnetic device.

Further, the real-time ion detection apparatus 30 includes an ion component and concentration monitoring device 31, and the ion component and concentration monitoring device 31 is used for monitoring the ion component and concentration in the brine filtrate after impurity removal.

Further, the ion component and concentration monitoring device 31 is composed of several components of an atomic absorption spectrophotometer, an ICP and a point titration apparatus, wherein the ICP refers to an existing ICP-AES analyzer, and is mainly used for qualitative and quantitative analysis of inorganic elements, and the ICP-AES inductively coupled atomic emission spectrometer is used as a large-scale precise inorganic analysis instrument.

Further, the lithium carbonate precipitation device 40 comprises a fourth proportioning tank 41, a buffer tank 42, a third pressing plate filter 43 and a drying device 44, wherein the third pressing plate filter 43 is used for generating a lithium carbonate product and filtrate, and the lithium carbonate product and filtrate generated by the third pressing plate filter 43 respectively enter the drying device 44 and the MVR evaporation crystallization device 50;

further, brine flowing through the ion component and concentration monitoring device 31 enters the fourth proportioning tank 41 through the first buffer centrifugal pump 66, the fourth proportioning tank 41 is connected with the buffer tank 42 through the second buffer centrifugal pump 67, the buffer tank 42 is connected with the third pressure plate filter 43 through the second precipitation underflow pump 68, the third pressure plate filter 43 is connected with the MVR evaporative crystallization device 50 through the second filter centrifugal pump 69, and lithium carbonate products generated in the third pressure plate filter 43 enter the drying equipment 44.

Further, the MVR evaporation crystallization device 50 includes a fifth dosing tank 51 and an MVR device 52, a discharge end of the fifth dosing tank 51 is connected with a feed end of the MVR device 52, the MVR device 52 is used for evaporating and crystallizing brine after precipitating lithium, high-value utilization of byproducts such as potassium salt and sodium salt is achieved, the MVR device is an MVR evaporator, filtered ion solution reaches a downstream buffer tank 42 along with a second buffer centrifugal pump 67 through a fourth dosing tank 41, the buffer tank 42 is connected with a third platen filter 43 through a second precipitation underflow pump 68, a lithium carbonate collecting port of the third platen filter 43 is connected with a drying device 44, then the ion solution enters the downstream MVR evaporation crystallization device 50 from a filtrate outlet of the third platen filter 43 through a second filter centrifugal pump 69, the MVR evaporation crystallization device includes the fifth dosing tank 51 and the MVR device 52, and the fifth dosing tank 51 is added with sulfuric acid for decarburization to decarbonize the filtrate and obtain a crystalline salt product through MVR.

The embodiment is in the working process:

the method comprises the steps of respectively feeding brine leached from ores such as lepidolite or the like or salt lake brine and an alkali precipitant into a first proportioning tank 11 from a brine inlet and a hydroxide precipitant inlet according to a certain proportion, wherein the brine is a plurality of compositions in the brine leached from the lepidolite or the salt lake brine, the lepidolite comprises lepidolite, lithium porcelain clay and spodumene, aluminum and iron are removed in the step, then the mixed brine enters a second proportioning tank 12 through a centrifugal pump, the calcium ion precipitant is added into the second proportioning tank 12 for stirring, fluorine can be removed in the step, the stirred mixed brine enters a third proportioning tank 13 through the centrifugal pump, and meanwhile, the carbonate precipitant is added, so that calcium and magnesium are removed in the step for the first time;

the mixed brine enters a transfer kettle 21 through a centrifugal pump, an underflow outlet with sediment at the middle lower part of the transfer kettle 21 enters a plate press filter through an underflow pump to remove sediment impurities such as ferric hydroxide, aluminum hydroxide, calcium fluoride, calcium carbonate and the like, then the brine subjected to primary impurity removal enters a second plate press filter through a first filter centrifugal pump 65 to carry out fine impurity removal, a partially clarified mixed brine overflow outlet on the transfer kettle 21 enters the second plate press filter, and the brine subjected to fine impurity removal through the second plate press filter can remove residual magnetic metals such as iron and compounds thereof in the brine through a pipeline magnetic removal device 24;

the purified brine flowing through the ion component and concentration monitoring device 31 can be monitored in real time, the removal condition of impurity ions is mastered, and the steps can be regulated in real time and efficiently so as to improve the purity and yield of lithium carbonate;

the obtained purified brine enters a fourth proportioning tank 41 through a first buffer centrifugal pump 66, sodium carbonate precipitant is added into the fourth proportioning tank 41 for stirring, the uniformly mixed solution enters a buffer tank 42 through a second buffer centrifugal pump 67, under the action of steam heating, when the steam is heated to 90-100 ℃, the brine carries out precipitation reaction, the reaction temperature is preferably 95 ℃, the reacted mixed solution enters a brine inlet of a third plate pressure filter through a second precipitation underflow pump 68, and the precipitate filtered by the third plate pressure enters a drying device for heating, drying and collecting lithium carbonate products;

the filtered lithium precipitation mother liquor enters a brine inlet of the fifth proportioning tank 51 through a second filtering centrifugal pump 69, and enters the MVR device 52 after acid addition and carbon removal, and solution evaporation is carried out to form sodium potassium salt.

The foregoing is only a preferred embodiment of the present utility model, but the scope of the present utility model is not limited thereto, and any person skilled in the art, who is within the scope of the present utility model, should make equivalent substitutions or modifications according to the technical scheme of the present utility model and the inventive concept thereof, and should be covered by the scope of the present utility model.

Claims (9)

1. The equipment for monitoring the concentration of the lithium precipitation in real time comprises precipitation impurity removal batching equipment (10), and is characterized by further comprising iron aluminum fluoride calcium ion removal equipment (20), real-time ion detection equipment (30), lithium carbonate precipitation equipment (40) and an MVR evaporation crystallization device (50);

the discharge end of precipitation edulcoration dispensing equipment (10) is connected with the feed end of iron aluminum fluoride calcium ion desorption equipment (20), and the discharge end of iron aluminum fluoride calcium ion desorption equipment (20) is connected with the feed end of real-time ion detection equipment (30), the discharge end of real-time ion detection equipment (30) is connected with the feed end of lithium carbonate heavy lithium equipment (40), and the discharge end of lithium carbonate heavy lithium equipment (40) is connected with the feed end of MVR evaporation crystallization device (50).

2. The device for monitoring the concentration of precipitated lithium in real time according to claim 1, characterized in that the precipitation and impurity removal dosing device (10) comprises a first dosing tank (11), a second dosing tank (12) and a third dosing tank (13), wherein the discharge end of the first dosing tank (11) is connected with the feed end of the second dosing tank (12), the discharge end of the second dosing tank (12) is connected with the feed end of the third dosing tank (13), and the discharge end of the third dosing tank (13) is connected with the feed end of the iron aluminum fluorine calcium ion removal device (20).

3. The device for monitoring the concentration of lithium precipitated in real time according to claim 1, wherein the iron aluminum fluoride ion removal device (20) comprises a transfer kettle (21), a first pressure plate filter (22), a second pressure plate filter (23), a pipeline demagnetizing device (24) and an ion exchange resin device (25), the pipeline demagnetizing device (24) can adsorb out magnetic substances which cannot be filtered in the pressure plate filter, the feeding end of the transfer kettle (21) is connected with the discharging end of the precipitation impurity removal batching device (10), the discharging end of the transfer kettle (21) is connected with the feeding end of the first pressure plate filter (22), the discharging end of the first pressure plate filter (22) is connected with the feeding end of the second pressure plate filter (23), the discharging end of the second pressure plate filter (23) is connected with the feeding end of the pipeline demagnetizing device (24), and the discharging end of the pipeline demagnetizing device (24) is connected with the feeding end of the ion exchange resin device (25).

4. A device for monitoring the concentration of lithium precipitated in brine in real time according to claim 3, characterized in that the pipe demagnetizing device (24) comprises a feed inlet (241) of brine, a discharge outlet (242) of brine and a step-in strong magnetic rod (243), the step-in strong magnetic rod (243) is used for removing magnetic impurities, the feed inlet (241) of brine is connected with the discharge end of the second pressure plate filter (23), and the discharge outlet (242) of brine is connected with the feed end of the ion exchange resin device (25).

5. A device for monitoring the concentration of precipitated lithium in brine in real time according to claim 3, characterized in that the pipe demagnetizing means (24) consist of one or more of permanent magnetic devices and electromagnetic devices.

6. The apparatus for monitoring the concentration of lithium precipitated in brine in real time according to claim 1, characterized in that the real-time ion detection apparatus (30) comprises an ion component and concentration monitoring device (31), the ion component and concentration monitoring device (31) being used for monitoring the ion component and concentration in the brine filtrate after impurity removal.

7. The apparatus for monitoring the concentration of precipitated lithium in brine in real time according to claim 6, characterized in that said ionic composition and concentration monitoring device (31) is composed of several of atomic absorption spectrophotometers, ICP and point titrators.

8. The device for monitoring the concentration of the lithium precipitated in the brine in real time according to claim 1, wherein the lithium carbonate precipitation device (40) comprises a fourth proportioning tank (41), a buffer tank (42), a third pressure plate filter (43) and a drying device (44), the third pressure plate filter (43) is used for generating a lithium carbonate product and a filtrate, and the lithium carbonate product and the filtrate generated by the third pressure plate filter (43) respectively enter the drying device (44) and the MVR evaporation crystallization device (50).

9. The device for monitoring the concentration of lithium precipitated in brine in real time according to claim 1, wherein the MVR evaporation crystallization device (50) comprises a fifth proportioning tank (51) and an MVR device (52), a discharging end of the fifth proportioning tank (51) is connected with a feeding end of the MVR device (52), and the MVR device (52) is used for evaporating and crystallizing the brine after lithium precipitation.