CN113058432B - System for carry out moisturizing dilution to concentrate of salt lake brine - Google Patents
System for carry out moisturizing dilution to concentrate of salt lake brine Download PDFInfo
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- CN113058432B CN113058432B CN202110294256.8A CN202110294256A CN113058432B CN 113058432 B CN113058432 B CN 113058432B CN 202110294256 A CN202110294256 A CN 202110294256A CN 113058432 B CN113058432 B CN 113058432B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/422—Electrodialysis
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D36/00—Filter circuits or combinations of filters with other separating devices
- B01D36/003—Filters in combination with devices for the removal of liquids
- B01D36/008—Means to filter or treat the separated liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/40—Mixing liquids with liquids; Emulsifying
- B01F23/405—Methods of mixing liquids with liquids
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/40—Mixing liquids with liquids; Emulsifying
- B01F23/48—Mixing liquids with liquids; Emulsifying characterised by the nature of the liquids
- B01F23/483—Mixing liquids with liquids; Emulsifying characterised by the nature of the liquids using water for diluting a liquid ingredient, obtaining a predetermined concentration or making an aqueous solution of a concentrate
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/40—Mixing liquids with liquids; Emulsifying
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
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Abstract
The invention relates to a system for diluting a concentrated solution of salt lake brine by supplementing water, which comprises: heating mechanism, filtering mechanism, control mechanism, a plurality of dilution tank, a plurality of electrodialysis unit and storage mechanism, wherein heating mechanism connects filtering mechanism, filtering mechanism connects control mechanism, control mechanism connects a plurality of dilution tank to the water yield of control inflow each dilution tank, a plurality of dilution tank series connection are arranged, and communicate each other in proper order in upper portion, a plurality of dilution tank connect respectively in proper order a plurality of electrodialysis unit, just do not communicate each other between a plurality of electrodialysis unit, last dilution tank in a plurality of dilution tank is connected to storage mechanism. The system of the invention obviously improves the speed of overflowing and discharging the concentrated solution from the electrodialysis unit to return the solution, thereby improving the yield of the diluent.
Description
Technical Field
The invention relates to the technical field of preparation of battery-grade lithium carbonate, in particular to a system for supplementing water and diluting a concentrated solution obtained by electrodialysis separation of salt lake brine.
Background
At present, an electrodialysis device is used for separating salt lake brine with high magnesium-lithium ratio. The salt lake brine is mainly a saturated magnesium chloride solution, the magnesium-lithium ratio in the solution is 20:1, and the salt lake brine can be used as a raw material for preparing battery-grade lithium carbonate.
The electrodialysis device mainly adopts an ion selective migration technology, and ions in salt lake brine form directional migration under the action of a direct current electric field, so that the effect of magnesium-lithium separation is achieved. The electrodialysis device comprises a plurality of electrodialysis units (which are not communicated with each other) so as to separate the salt lake brine respectively.
The salt lake brine is subjected to electrodialysis separation to obtain a concentrated solution, wherein the concentrated solution usually contains high-concentration lithium chloride, and the lithium ion content of the concentrated solution is 8-12 g/l. The above concentrate needs to be diluted before use. For this purpose, a certain amount of water is supplied from each of the plurality of dilution tanks (which are sequentially communicated with each other at the upper portions thereof) and introduced into the corresponding electrodialysis unit, and a return concentrate is overflowed from the upper portion of the electrodialysis unit and returned to the corresponding dilution tank through a return concentrate pipe. And under the condition of continuous water supplement, overflowing and discharging the first diluent from the last diluent groove and outputting the first diluent to the storage mechanism. Then, the solution is diluted again in the storage means to obtain a second diluted solution. And the second diluent is used for conveying to the next section, so that the lithium chloride in the second diluent reacts with carbonate to obtain lithium carbonate.
In current makeup dilution systems, water is added only to a first tank of a plurality of dilution tanks and then slowly overflows from the first tank to the next polar tank step by step. The water replenishing device causes that the speed of overflowing and discharging the concentrated solution from the upper part of the electrodialysis unit is slow, the front-end treatment capacity is small, and the treatment speed is slow.
In addition, the ion concentration in the feed liquid in the plurality of dilution tanks is not uniform, the conductivity value and pH value fluctuation of the dilution liquid are large, and the operating current of the electrodialysis device is unstable. This results in unsafe operation of the electrodialysis unit and a lag in capacity.
Disclosure of Invention
Technical problem
The invention aims to provide a novel system for supplementing and diluting a concentrated solution of salt lake brine. The system preheats raw water, and dilutes the concentrated solution return liquid from the electrodialysis units through the control mechanism and the dilution tanks, so that the problems of low speed of overflowing and discharging the concentrated solution return liquid from the electrodialysis units and low yield of the diluted solution can be effectively solved.
Technical scheme
According to one aspect of the invention, a system for supplementing water and diluting a concentrated solution of salt lake brine is provided, and the system comprises: a heating mechanism, a filtering mechanism, a control mechanism, a plurality of dilution tanks, a plurality of electrodialysis units and a storage mechanism,
wherein the heating mechanism is connected with the filtering mechanism,
the filtering mechanism is connected with the control mechanism,
the control mechanism is connected with the plurality of dilution tanks to control the amount of water flowing into each dilution tank,
the plurality of dilution tanks are arranged in series and are communicated with each other in sequence at the upper part,
the plurality of dilution tanks are sequentially and respectively connected with the plurality of electrodialysis units, the electrodialysis units are not communicated with each other,
the last dilution tank of the plurality of dilution tanks is connected to the storage mechanism.
In one embodiment, the heating mechanism is a plate heat exchanger.
In one embodiment, the filter mechanism is a precision bag cartridge filter.
In one embodiment, the control mechanism includes a plurality of valves and a plurality of flow meters.
In one embodiment, the control mechanism comprises a first valve and a first flow meter, and a second valve and a second flow meter, wherein
The rear section of the filtering mechanism is provided with the first valve and a first flowmeter, the first valve is an electric valve, the first flowmeter is an electromagnetic flowmeter,
the second valves and the second flow meters are respectively arranged at the front branch sections of the plurality of dilution tanks to respectively control the water amount flowing into each dilution tank,
the second valve is adjusted manually, and the second flowmeter is a glass rotameter.
In one embodiment, the plurality of dilution tanks is three dilution tanks.
In one embodiment, the storage mechanism is a tank comprising a tank body and a level gauge.
Advantageous effects
Compared with the prior art, the system provided by the invention has the advantages that the raw water is preheated, and the return concentrated solution from the electrodialysis units is respectively diluted through the control mechanism and the dilution tanks, so that the speed of overflowing and discharging the return concentrated solution from the electrodialysis units is obviously increased, and the yield of the diluted solution is further increased.
In addition, the system can also ensure the uniform concentration, the stable conductivity value and the stable pH of the feed liquid in the plurality of dilution tanks, and ensure the stable working current of the electrodialysis device, thereby ensuring the safe and stable operation of the electrodialysis device and further improving the overall productivity of the electrodialysis device.
Drawings
FIG. 1 is a schematic diagram of a prior art single makeup dilution system in which a concentrate of salt lake brine is subjected to single makeup dilution.
FIG. 2 is a schematic diagram of a multi-stage pad-up dilution system according to one embodiment of the present invention, wherein multi-stage pad-up dilution is performed on a concentrate of salt lake brine.
Reference numerals
1000: single moisturizing dilution system
110: filtering mechanism
120: control mechanism
130A, 130B, 130C: dilution tank
140A, 140B, 140C: electrodialysis unit
150: storage mechanism
101: valve gate
102: flow meter
11: raw material water
12: filtered water
13: acid liquor
14: salt lake brine
15a, 15b, 15 c: feeding liquid
16a, 16b, 16 c: returning of concentrated solution
17a, 17b, 17 c: desalting solution
18 a: first diluent
18 b: second diluent
2000: multi-section water replenishing dilution system
200: heating mechanism
210: filtering mechanism
220: control mechanism
230A, 230B, 230C: dilution tank
240A, 240B, 240C: electrodialysis unit
250: storage mechanism
201: first valve
202: first flowmeter
203A, 203B, 203C, a second valve
204A, 204B, 204C: second flowmeter
20 a: steam generation
20 b: condensed water
21 a: raw material water
21 b: heated water
22: filtered water
23: acid liquor
24: salt lake brine
25a, 25b, 25 c: feeding liquid
26a, 26b, 26 c: returning of concentrated solution
27a, 27b, 26 c: desalting solution
28: diluent liquid
Detailed Description
The system for multi-stage water-replenishing dilution of concentrated solution of salt lake brine according to the invention will be described in detail below with reference to the single water-replenishing dilution system of the prior art,
the terms or words used in the present specification and claims should not be construed restrictively as general or dictionary definitions, and should be construed as meanings and concepts corresponding to technical ideas of the present invention on the basis of the principle that the inventor can appropriately define concepts of the terms to describe the invention in the best possible manner.
1. Single moisturizing dilution system of prior art
As shown in fig. 1, the single refill dilution system 1000 generally includes: a filtration mechanism 110, a control mechanism 120, dilution tanks 130A, 130B, 130C, electrodialysis units 140A, 140B, 140C, and a storage mechanism 150. The control mechanism 120 includes a valve 101 and a flow meter 102.
The primary configuration of the single refill dilution system 1000 is as follows.
The filtering mechanism 110 is typically a cartridge filter, such as a precision bag cartridge filter, and is mainly used for filtering 1 micron-sized fine particles in the raw water 11. The raw water 11 is filtered by the filter mechanism 110 to obtain filtered water 12.
The control mechanism 120 generally includes a valve 101 and a flow meter 102, wherein the valve 101 may be an electrically-actuated regulator valve and the flow meter 102 may be an electromagnetic flow meter. Specifically, the filtered water 12 is fed to the dilution tank 130A through the control mechanism 120, and the acid solution 13 is added to the dilution tank 130A to adjust the pH of the feed liquid in the dilution tanks 130A, 130B, and 130C. When the pH of the feed liquid in the dilution tank 130C reaches a process-required value (for example, pH 3 to 5), the addition of the acid liquid 13 is stopped.
Further, the feed liquids 15a, 15B, and 15C from the dilution tanks 130A, 130B, and 130C are fed from the lower part of each dilution tank to the lower parts of the electrodialysis cells 140A, 140B, and 140C, respectively. The location of the feed solution entering the electrodialysis unit can be different from the location of the salt lake brine entering the electrodialysis unit.
The concentrated liquid returns 16a, 16B, and 16C are overflowed from the return regions at the upper portions of the electrodialysis units 140A, 140B, and 140C, respectively, and returned to the upper portions of the dilution tanks 130A, 130B, and 130C through return pipes, respectively, to be diluted.
When the filtered water 12 is continuously supplied to the dilution tank 130A, the liquid level of the feed liquid in the dilution tank 130A rises, and the feed liquid sequentially overflows to the next dilution tank through upper communication parts of the dilution tanks 130A, 130B, and 130C.
The first diluted solution 18a overflows from the upper portion of the last dilution tank 130C, and is sent to the storage mechanism 150. At the same time, the raw material water 11 is replenished again to the upper part of the storage means 150 to perform further dilution so that the lithium ion content of the second diluted solution 18b discharged from the lower part of the storage means 150 reaches the process requirement of the next stage (for example, the lithium ion content is 3.5 to 4.5 g/l).
In the single refill dilution system of the prior art described above, only the dilution tank 130A is refilled with water. After the liquid level in the dilution tank 130A rises, the feed liquid overflows from the dilution tank 130A to the dilution tank 130B and the dilution tank 130C in this order. Further, the feed liquid in the dilution tank 130C is overflowed and discharged to obtain the first diluted liquid 18 a. The first diluted solution 18a is transferred to the storage mechanism 150, and at the same time, the second water-replenishing dilution is performed again through the upper portion of the storage mechanism 150, so that the final second diluted solution 18b is obtained.
The disadvantage of this single make-up dilution system is the slow overflow rate of the concentrate return 16a, 16b, 16c, the low front-end throughput and the slow processing rate.
Further, the concentrations of the feed liquids in the three diluting tanks 130A, 130B and 130C are not uniform, and the conductivity values and pH fluctuations are large. Moreover, the operating current of the electrodialysis cells 140A, 140B, 140C is unstable. This results in unsafe operation of the electrodialysis unit and a lag in capacity.
Further, the temperature of the raw material water is low, and after the raw material water is supplied to the dilution tank, the temperature of the feed liquid in the dilution tank is lowered, and further, the temperature of the feed liquids 15a, 15B, and 15C is lowered, and the temperature of the concentrated liquid in the electrodialysis cells 140A, 140B, and 140C is lowered. Therefore, the electrodialysis units 140A, 140B and 140C have slow separation speed and poor separation effect on the salt lake brine 14, and the working current of the electrodialysis units is unstable and unsafe to operate.
In addition, since the concentration of the obtained first diluted solution 18a is too high to reach the process requirement value, it is necessary to perform the second dilution with additional water in the upper part of the stock mechanism 150 to obtain the final second diluted solution 18 b. This way the temperature of the final second dilution liquid 18b is further reduced. Further, the supplemented raw water 11 is not subjected to any filtration treatment, and therefore contaminates the first diluting solution 18 a.
2. The invention discloses a multi-stage water replenishing dilution system
As shown in fig. 2, the present invention improves upon the single refill dilution system of fig. 1, the improvement consisting essentially of: a heating mechanism 200 is added; a new control mechanism 220 is used, wherein the three dilution tanks are all subjected to water replenishing dilution; and the replenishment of the raw material water in the upper part of the storage mechanism 250 is cancelled.
In one embodiment, the multi-stage refill dilution system 2000 of the present invention generally comprises: a heating means 200, a filtering means 210, a control means 220, dilution tanks 230A, 230B, 230C, electrodialysis units 240A, 240C, and a storage means 250. The control mechanism 220 basically includes a first valve and a first flow meter, and a second valve and a second flow meter.
The multi-stage refill water dilution system 2000 is configured in detail as follows.
(2.1) heating mechanism
The heating mechanism 200 may be a plate heat exchanger. Wherein, the steam 20a with the temperature of about 100-130 ℃ is introduced into the heating mechanism 200 to heat the raw material water 21a, and the heated water 21b is obtained.
The piping that carries the raw water 21a and the heated water 21b is typically of upvc material, the upvc plastic pipe having a maximum heat resistance temperature of about 40 ℃. If the steam temperature is too high, the temperature of the heated water 21b is too high, so that the pipeline can be scalded and damaged; if the steam temperature is too low, the effect of heating the raw material water 21a is not obtained. The temperature of the steam 20a may be appropriately determined according to production experience so that the temperature of the heated water 21b is maintained within a range of 30-35 c to meet safe production requirements.
The pipelines of the steam inlet and the condensate outlet are made of carbon steel, and the highest heat-resistant temperature is about 300 ℃.
The steam 20a condenses to form condensed water 20b, which can be further recycled.
The heating mechanism 200 is connected to a filtering mechanism 210.
(2.2) Filter mechanism
The filter mechanism 210 may be a cartridge filter, which may be titanium or steel-lined rubber. In particular, the filtering mechanism 210 may be a precise bag type cartridge filter, which contains 8 filter cartridges and is equipped with a 1 μm filter bag, and is mainly used for filtering 1 micron-sized fine particles in the makeup water.
The filtering mechanism 210 is used for filtering the heated water 21b to obtain filtered water 22.
The filtering mechanism 210 is connected to a control mechanism 220.
(2.3) control mechanism, multiple dilution tanks, and multiple electrodialysis units
The control mechanism 220 is connected with a plurality of dilution tanks, to control the amount of water flowing into each dilution tank,
the plurality of dilution tanks are arranged in series and are communicated with each other in sequence at the upper part,
the plurality of dilution tanks are sequentially and respectively connected with the plurality of electrodialysis units, and the plurality of electrodialysis units are not communicated with each other.
The flow rate of the filtered water 22 is controlled by the control means 220, and the filtered water is divided into a plurality of portions and added to a plurality of dilution tanks. Simultaneously, adding an acid solution to the plurality of dilution tanks.
And respectively carrying out electrodialysis separation on the salt lake brine by using a plurality of electrodialysis units to obtain corresponding concentrated solutions. The electrodialysis units are sequentially and respectively communicated with the dilution tanks, and the electrodialysis units are not communicated with each other.
Further, the feed liquid in the plurality of dilution tanks is supplied from the lower portion of each dilution tank to the lower portion of the corresponding electrodialysis unit, respectively, to overflow the concentrate returning liquid from the upper portion of the electrodialysis unit and convey the concentrate returning liquid to the upper portion of the corresponding dilution tank for dilution,
in addition, the feed liquid in the plurality of dilution tanks is sequentially overflowed from the upper part of the dilution tank to the next dilution tank from the first dilution tank.
The control mechanism 220 may include a plurality of valves and a plurality of flow meters. For example, the control mechanism 220 may include a first valve 201 and a first flow meter 202, and a second valve 203A, 203B, 203C and a second flow meter 204A, 204B, 204C.
A first valve 201, which may be an electric valve, and a first flow meter 202, which may be an electromagnetic flow meter, may be provided at a rear stage of the filter mechanism 210. The first valve 201 is used to control the flow rate of the filtered water 22, and the first flow meter 202 is used to display the flow rate of the filtered water 22.
In the embodiment shown in fig. 2, the filtered water 22 is split into three branches after the first valve 201 and the first flow meter 202, and is added to the dilution tanks 230A, 230B, 230C, respectively. In addition, according to other embodiments, the filtered water 22 may be split into two or more than four branches.
In the embodiment shown in fig. 2, three dilution tanks are provided. Furthermore, according to other embodiments, two or more dilution tanks may be provided.
Referring to fig. 2, second valves 203A, 203B, and 203C and second flow meters 204A, 204B, and 204C may be provided in the branching front stages of the three dilution tanks, respectively.
The second valves 203A, 203B, 203C may be manually adjustable and the second flow meters 204A, 204B, 204C may be glass rotameters. The second valves 203A, 203B, 203C are respectively used for controlling the corresponding flow rates, and the second flow meters 204A, 204B, 204C are respectively used for displaying the corresponding flow rates.
Specifically, the flow through the second flow meters 204A, 204B, 204C may be distributed in a stepwise decreasing manner based on the total flow through the first flow meter 202. That is, the amount of water added to the plurality of dilution tanks is reduced stepwise.
In addition, acid solution 23 is delivered to dilution tanks 230A, 230B, and 230C, respectively, to control conductivity and pH of the feed solution in the three tanks 230A, 230B, and 230C.
In one embodiment, the acid solution 23 may come from the same or different dilute acid solution storage tanks and be delivered by a delivery pump, as desired.
In one embodiment, the dilution mechanism includes dilution wells 230A, 230B, 230C. The diluting mechanism can be made of glass fiber reinforced plastic, and three diluting grooves 230A, 230B and 230C can be arranged in series inside the diluting mechanism, wherein the upper parts of the three grooves are communicated with each other in sequence. The dilution mechanism may also include a level meter (e.g., a differential pressure level meter) for monitoring the feed liquid level in the dilution wells 230A, 230B, 230C.
A plurality of electrodialysis units are provided so as to communicate the plurality of dilution tanks one-to-one, respectively. The electrodialysis units form an electrodialysis device, wherein the electrodialysis units are not communicated with each other. Each electrodialysis unit can be composed of an electrodialyzer, a membrane stack, a circulating device and an automatic control system.
Referring to fig. 2, salt lake brine 24 is fed from the lower portions of electrodialysis units 240A, 240B, 240C, respectively. The salt lake brine 24 can come from the same or different brine storage tanks according to process requirements and is conveyed to the corresponding electrodialysis units by a conveying pump. The salt lake brine 24 is obtained by filtering and heating a salt lake brine raw material conventionally, and the temperature of the salt lake brine is about 28-32 ℃.
The feed solutions 25a, 25B, 25C are taken from the lower part of the dilution tanks 230A, 230B, 230C and are delivered to the lower part of the electrodialysis cells 240A, 240B, 240C, respectively. The location of the feed solution entering the electrodialysis unit can be different from the location of the salt lake brine entering the electrodialysis unit.
The concentrated liquid returns 26a, 26B, and 26C overflow and are discharged from the return regions at the upper parts of the electrodialysis cells 240A, 240B, and 240C, respectively, and are returned to the upper parts of the dilution tanks 230A, 230B, and 230C through return pipes, respectively, to be diluted.
Further, desalted liquids 27a, 27B, and 27C are also obtained from the desalted liquid regions above the electrodialysis cells 240A, 240B, and 240C, respectively, and can be recovered and reused after being discharged.
Among the plurality of dilution tanks, the level of the feed liquid in the dilution tank 230A (which is the first dilution tank) is highest, and thus the feed liquid overflows from the upper portion of the dilution tank 230A and is transferred to the dilution tank 230B (the next dilution tank). Similarly, the feed liquid overflows from the upper portion of the dilution tank 230B and is transferred to the dilution tank 230C (the last dilution tank).
As can be seen from fig. 2, for the dilution tank 230A, filtered water, the acid liquid 23, and the concentrated liquid back-up 26a are input thereto to form a feed liquid; further, the feed liquid 25a is supplied from the dilution tank 230A to the electrodialysis cell 240A, and the feed liquid is overflowed to the subsequent dilution tank 230B. Dilution tanks 230A and 230B have similar inputs and outputs.
The last dilution tank of the plurality of dilution tanks is connected to a storage mechanism to deliver the final dilution liquid.
(2.4) storage mechanism
When the filtered water 22 is continuously supplied to the dilution tanks 230A, 230B, and 230C, the feed liquid level in the triple tank 230A, 230B, and 230C rises rapidly, and the final dilution liquid 28 is discharged by overflowing the upper portion of the last dilution tank 230C and is sent to the storage means 250.
As described above, the diluent 28 is preferably controlled to a temperature in the range of 28 to 32 ℃.
In addition, the lithium ion content of the diluent 28 is required to meet the process requirements of the next process section (e.g., lithium ion content of 3.5-4.5g/l)
The storage mechanism may be a tank, which may include a tank body and a level gauge.
In one embodiment, the multi-stage water dilution system 2000 may be implemented by upvc piping.
In one embodiment, the multi-stage refill water dilution system 2000 may additionally include one or more valves, transfer pumps, pH meters, conductivity meters, level meters, and flow meters as desired.
Examples
Hereinafter, the present invention will be described in detail with reference to examples. However, the embodiments of the present invention may be modified into various other forms, and the scope of the present invention should not be construed as being limited to the embodiments described below. Embodiments of the present invention are provided to more fully describe the invention to those of ordinary skill in the art.
The experimental procedures in the following examples are generally conventional in the art or according to the manufacturer's recommendations if specific conditions are not indicated; the raw materials and equipment used are those commercially available from conventional markets and the like unless otherwise specified.
Comparative example 1
Referring to fig. 1, a prior art single makeup dilution system is used to makeup dilute a concentrate of salt lake brine.
First, raw material water 11(30.00 m) from a raw material water reservoir was supplied 3 /h，15 ℃ C.) was fed to a precision security filter (8 bags from Hippon Industrial technology Co., Ltd., inner bag of three-layer bag of 1 μm in which removal rate of fine particles was 90%, material: TA8) to yield filtered water 12.
The filtered water 12 is then conveyed by means of a control device 120 (comprising an electrovalve 101 and an electromagnetic flowmeter 102) to a dilution device (from Jiangsu Mediterranean chemical and chemical plants, Ltd., glass fiber reinforced plastics, volume 24 m) 3 ) Comprises three dilution tanks 130A, 130B, 130C arranged in series. A30% hydrochloric acid solution (0.05 m) was added to the dilution tank 130A 3 And/h) the pH of the feed liquid in the dilution tanks 130A, 130B, 130C is set to 3.
In addition, brine from a brine storage pond (100.00 m) was fed to three electrodialysis units 140A, 140B, 140C (model SS-0 from ASTOM, Japan) which were not communicated with each other, respectively 3 H, 30 ℃). After being separated by electrodialysis units 140A, 140B and 140C, corresponding concentrated solutions are respectively obtained.
At the same time, the feed liquids (30 m) from the lower parts of the dilution tanks 130A, 130B, 130C, respectively 3 H) to the lower parts of the electrodialysis cells 140A, 140B, 140C, respectively.
The concentrated liquid returns 16a, 16B, and 16C are overflowed from the upper portions of the electrodialysis units 140A, 140B, and 140C, respectively, and returned to the upper portions of the dilution tanks 130A, 130B, and 130, respectively.
When the filtered water 12 is continuously supplied to the dilution tank 130A, the liquid level of the feed liquid in the dilution tank 130A rises, and the feed liquid overflows in order through the upper communication parts of the dilution tanks 130A, 130B, and 130C.
The first diluent 18a overflows the upper part of the dilution tank 130C, and is sent to a diluent storage tank as the storage means 150. At the same time, the raw water 11(20.00 m) was supplied again to the upper part of the diluting liquid storage tank 3 H) for further dilution, storing from the dilutionThe lower part of the tank discharges the second diluent 18b as the final diluent.
Example 1
Referring to fig. 2, in comparison with the single refill diluting system of the prior art in comparative example 1, in the multi-stage refill diluting system of this embodiment, a heating mechanism 200 is additionally provided, and a new control mechanism 220 is used, in which all of the diluting compartments 230A, 230B, 230C are separately refilled and diluted, and the water inflow amounts of the diluting compartments 230A, 230B, 230C are distributed in stepwise decreasing manner, and the raw material water replenishment at the upper portion of the storage mechanism 250 is cancelled.
The workflow of this embodiment is as follows.
First, raw material water 21a (50.00 m) from a raw material water reservoir was supplied 3 H, 15 ℃ C. was fed to a plate heat exchanger (TA from Afaha technologies Ltd.) as the heating means 200, and 120 ℃ steam 20a (1 m) from a gas supply facility was introduced into the plate heat exchanger 3 H) to heat the raw material water 21a to obtain heated water 21b having a temperature of 33 ℃.
Then, the heated water 21b was passed through a precision cartridge filter (8-pack, three-pack, 1 μm inner pack, from Nippon Industrial and technology Co., Ltd., 8 packs) as a filter means 210, and the removal rate of fine particles was 90%, material: TA8), to obtain filtered water 22 having a turbidity of 0.5 to 1 NTU.
The filtered water 22 is divided into three branches after passing through the first valve 201 and the first flowmeter 202, and then passes through the second valves 203A, 203B, 203C and the second flowmeters 204A, 204B, 204C, respectively, so as to be added into the dilution mechanism (from Jiangsu Mitsui metallurgy equipment, Inc., glass fiber reinforced plastics, volume 24 m) 3 ) In three dilution tanks 230A, 230B, 230C arranged in series.
Specifically, the total flow rate (50 m) according to the first flow meter 202 3 H) of the second valve 203A, 203B, 203C to a second flow meter 204A of 25.00m 3 H, the second flowmeter 204B is 15.00m 3 H, the second flowmeter 204C is 10.00m 3 /h。
In addition, the dilution wells 230A, 230B, and 2 are filled with the solution30% hydrochloric acid solution (0.05 m) was added to 30C 3 H) so that the pH of the feed liquid in the dilution tanks 230A, 230B, 230C is 3.
Further, the salt lake brine 24(100.00 m) from the brine storage tank was fed to three electrodialysis units 240A, 240B, 240C (from ASTOM corporation, model SS-0, Japan) which were not communicated with each other, respectively 3 H, 30 ℃). After being separated by electrodialysis units 240A, 240B and 240C, corresponding concentrated solutions are respectively obtained.
At the same time, the feed liquid (30.00 m) from the lower part of the dilution tanks 230A, 230B, 230C was supplied 3 H) to the lower parts of electrodialysis cells 240A, 240B, 240C, respectively.
Concentrated liquid returns 17a, 17B, and 17C overflow and are discharged from the upper portions of the electrodialysis cells 240A, 240B, and 240C, respectively, and are returned to the upper portions of the dilution tanks 230A, 230B, and 230C, respectively.
When the filtered water 22 is continuously supplied to the three dilution tanks 230A, 230B, and 230C, the liquid level of the feed liquid in the three tanks rapidly rises, and the feed liquid sequentially overflows through the upper communication parts of the three tanks.
The final dilution liquid 28 was discharged in the upper part of the dilution tank 230C by overflow and transferred to a dilution liquid storage tank (from Koshihikari-Katsui-Kabushiki Kaisha, Ltd., glass fiber reinforced plastic, volume: 3.5 m) as a storage means 250 3 ) In (1).
Experimental example 1
The operation of each mechanism and device in comparative example 1 and example 1 was controlled by feedback data provided by a DCS (program control system in thunberg university) and each data was measured and summarized in table 1 below.
TABLE 1
As can be seen from table 1, in the case where the total amount of make-up water, the flow rate of the hydrochloric acid solution, and the flow rate of the salt lake brine added were all the same, respectively, the final dilution of example 1 was significantly improved in yield and had the same lithium ion content as compared to comparative example 1. This fully demonstrates that the multi-stage water-replenishing dilution system of the invention can significantly improve the diluent yield.
Although the preferred embodiments of the present invention have been disclosed for illustrative purposes, those skilled in the art will appreciate that various modifications, additions and substitutions are possible, without departing from the scope and spirit of the invention as disclosed in the accompanying claims.
Claims (7)
1. A system for replenishing dilution of a concentrate of salt lake brine, the system comprising: a heating mechanism, a filtering mechanism, a control mechanism, a plurality of dilution tanks, a plurality of electrodialysis units and a storage mechanism,
wherein the heating mechanism is connected with the filtering mechanism,
the filtering mechanism is connected with the control mechanism,
the control mechanism is connected with the plurality of dilution tanks to control the amount of water flowing into each dilution tank,
the plurality of dilution tanks are arranged in series and are communicated with each other in sequence at the upper part,
the plurality of dilution tanks are sequentially and respectively connected with the plurality of electrodialysis units, the electrodialysis units are not communicated with each other,
the last dilution tank of the plurality of dilution tanks is connected to the storage mechanism.
2. The system of claim 1, wherein the heating mechanism is a plate heat exchanger.
3. The system of claim 1, wherein the filtering mechanism is a precision bag cartridge filter.
4. The system of claim 1, wherein the control mechanism comprises a plurality of valves and a plurality of flow meters.
5. The system of claim 1, wherein the control mechanism comprises a first valve and a first flow meter, and a second valve and a second flow meter, wherein
The rear section of the filtering mechanism is provided with the first valve and a first flowmeter, the first valve is an electric valve, the first flowmeter is an electromagnetic flowmeter,
the second valves and the second flow meters are respectively arranged at the front branch sections of the plurality of dilution tanks to respectively control the water amount flowing into each dilution tank,
the second valve is adjusted manually, and the second flowmeter is a glass rotameter.
6. The system of claim 1, wherein the plurality of dilution tanks is three dilution tanks.
7. The system of claim 1, wherein the storage mechanism is a tank comprising a tank body and a level gauge.
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