CN213221252U - Salt lithium separation device applied to brine lithium extraction process - Google Patents
Salt lithium separation device applied to brine lithium extraction process Download PDFInfo
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- CN213221252U CN213221252U CN202021316798.8U CN202021316798U CN213221252U CN 213221252 U CN213221252 U CN 213221252U CN 202021316798 U CN202021316798 U CN 202021316798U CN 213221252 U CN213221252 U CN 213221252U
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Abstract
The utility model discloses a be applied to brine and carry lithium process's salt lithium separator, the device include the frame, are equipped with the filter cloth of reciprocal gyration operation in the frame, are equipped with in proper order along the filter cloth direction of advance: a salt washing liquid conveying mechanism for conveying the salt washing liquid to the salt washing area is distributed above the filter cloth; and a desorption liquid conveying mechanism for conveying desorption liquid to the desorption area is distributed above the filter cloth, and a lithium eluent collecting port is arranged below the desorption area. The applicant reconsiders the adsorption mechanism of the powdery lithium ion selective adsorbent and finds that the bonding strength between lithium ions and other salt ions and the adsorbent is different, so that the filter cake is loaded by using the filter cloth, the contact time between the salt washing liquid and the adsorbent is short in the dynamic operation process of the filter cloth, the salt washing liquid can elute other salt ions firstly, and the lithium ion loss is little; when salt washing is finished, the adsorption capacity of other salt ions on the filter cake is greatly reduced, so that effective salt-lithium separation is realized.
Description
Technical Field
The utility model belongs to the technical field of lithium is carried to brine, in particular to be applied to brine and carry lithium process's salt lithium separator.
Background
The rapid development of the current new energy industry drives the rapid increase of the demand of lithium products, but the high concentration of global lithium resources leads the global lithium product production to have the situation of oligopolism, which leads China to rely on import for a long time in lithium product supply. Along with the increasing importance of China on the development of lithium resources, China has found that the reserve of the lithium resources is 4008 ten thousand tons in terms of lithium chloride, wherein the salt lake resources account for about 71 percent and the ore resources account for about 29 percent, so that the lithium extraction from the salt lake brine has great significance for guaranteeing the development of new energy industries in China.
The selective adsorption method is a main means for extracting lithium from the salt lake brine at present, and can adsorb and separate lithium from a mixed solution containing various ions, and then the lithium ions can be separated from other ions by elution. Because the adsorption method is similar to the traditional water treatment method, the equipment used in the existing lithium extraction adsorption process of brine is basically from the traditional water treatment industry, wherein the adsorption tower is the most common, and molecular sieves or ion sieve type adsorbents such as aluminum series, monoclinic antimonate series, titanate series, manganese oxide series and the like are matched with the adsorption tower. The crystal structure of the selective adsorption material contains a gap structure matched with lithium ions, so that the selective adsorption material has specific selective adsorption on the lithium ions under the condition that various ions exist.
However, many practical problems have been found in the use of selective adsorbents in adsorption columns for lithium extraction from brines: (1) the used selective adsorbent has low capacity, the working capacity is generally less than 10mg/g, the activity is greatly reduced after granulation, and the selective adsorbent is fragile and easy to run off; (2) the quantity of water of thousands of cubic meters is required in the process of extracting lithium from brine per hour, which causes great load on the operation of the adsorption tower; (3) in the production stage, a large number of adsorption towers filled with the adsorbent are required to be constructed, the investment cost is high, thousands of tons of adsorbents are required to be reserved in the investment stage of a ten thousand-ton lithium carbonate production line, and the price is as high as hundreds of millions of yuan; (4) the salt-lithium ratio in the obtained lithium eluent is more than 30:1, and the magnesium-lithium ratio is more than 3:1, which brings great difficulty to the subsequent desalting and purifying process, and the finally obtained lithium product is extremely difficult to meet the requirement of battery-grade lithium carbonate or lithium hydroxide on the content of impurities; (5) more than 20% of lithium ions can be lost in the washing section, so that the lithium recovery rate in the adsorption section is lower than 60%, the lithium recovery rate in the whole process section is lower than 50%, and if high lithium recovery rate is to be obtained, multi-tower series connection and function conversion are required, so that the difficulty of industrial continuous production is greatly increased.
In recent years, there has been reported a method for extracting lithium from brine by using a powder adsorbent, which does not require granulation, has a much higher adsorption capacity than a granular adsorbent, and can significantly reduce the adsorption reaction time and the amount of the adsorbent used. At present, there are documents or patent reports that powder adsorbent is combined with plate-and-frame filter press, centrifuge, precise filtration or ceramic membrane for adsorption and desorption. However, the existing operation lacks understanding and attention on the washing process of the adsorbent in the process of extracting lithium from brine, so that the existing lithium extracting process from brine cannot obtain lithium eluent with low salt-lithium ratio.
SUMMERY OF THE UTILITY MODEL
The invention aims at providing a salt lithium separation device applied to a process of extracting lithium from brine, which is suitable for extracting lithium from brine by adopting a powdery lithium ion selective adsorbent, and the working principle of the salt lithium separation device is matched with the adsorption mechanism of the powdery lithium ion selective adsorbent.
In order to achieve the purpose, the technical scheme of the utility model is as follows:
the utility model provides a be applied to brine and carry lithium process's salt lithium separator, includes the frame, the frame on be equipped with the filter cloth of reciprocal gyration operation, be equipped with in proper order along the filter cloth advancing direction:
a salt washing liquid conveying mechanism for conveying the salt washing liquid to the salt washing area is distributed above the filter cloth;
and a desorption liquid conveying mechanism for conveying desorption liquid to the desorption area is distributed above the filter cloth, and a lithium eluent collecting port is arranged below the desorption area.
The utility model utilizes the filter cloth which is in reciprocating rotation operation to bear the filter cake, and the filter cake is formed by the adsorbent which is firstly mixed with brine for adsorption and then separated from the brine; according to different mechanisms arranged above the filter cloth, a salt washing area and a desorption area which are sequentially arranged along the advancing direction of the filter cloth are formed on the filter cloth, wherein the salt washing area is used for washing salt, and the desorption area is used for washing lithium, which is designed according to the adsorption mechanism of the amorphous hydroxide adsorbent. The applicant researches and discovers that during adsorption, other salt ions in brine extrude lithium ions into crystal lattices of the powdery lithium ion selective adsorbent to form a molecular sieve, and the other salt ions do not enter the crystal lattices of the powdery lithium ion selective adsorbent, so that the bonding strength between the lithium ions and the other salt ions and the adsorbent is different. Because the whole salt washing process is carried out in the dynamic operation process of the filter cloth, the contact time of the salt washing liquid and the adsorbent is short, when the salt washing liquid passes through a filter cake in a short time, the salt washing liquid can elute other salt ions firstly, lithium ions are still remained in crystal lattices of the adsorbent, and the loss of the lithium ions is little; when salt washing is finished, the adsorption capacity of other salt ions on the filter cake is greatly reduced, so that the concentration of the lithium eluent obtained in the desorption region is greatly increased, and effective salt and lithium separation is realized.
In the above-mentioned salt lithium separation device applied to the brine lithium extraction process, the salt washing liquid conveying mechanism is provided with at least two liquid outlet ends arranged along the filter cloth advancing direction. The liquid outlet ends arranged along the advancing direction of the filter cloth can realize 'salt washing for a plurality of times with small dosage', compared with a single liquid outlet end, the liquid outlet ends are arranged to achieve the same salt washing effect, the using amount of the salt washing liquid is less, and higher salt washing efficiency can be obtained under the condition that the same amount of the salt washing liquid is adopted.
In the salt and lithium separation device applied to the brine lithium extraction process, all the liquid outlet ends are uniformly arranged along the advancing direction of the filter cloth by taking the starting end of the salt washing area as a starting point, and the liquid outlet end at the tail end of the queue is positioned at the upstream of the tail end of the salt washing area. Because the filter cloth is in continuous operation, a certain time is reserved for the salt washing liquid to pass through the filter cake, the full salt washing is ensured, and the salt elution liquid is also ensured not to enter a desorption area.
The applicant researches and discovers that the adsorbent trapping lithium ions still has lithium ion loss in the salt washing process, but the higher the salt concentration of the salt washing solution, the lower the lithium ion loss rate. Therefore, in the salt-lithium separation device applied to the brine lithium extraction process, the salt concentration of the salt washing solution conveyed by the liquid outlet end is gradually increased along the direction opposite to the filter cloth advancing direction.
Along the opposite direction of filter cloth advancing direction, the higher the concentration of lithium ion on the adsorbent is, consequently the utility model discloses also corresponding set the salt concentration of salt washing liquid to gradient elution from low to high to reduce the loss of lithium ion on the adsorbent as far as possible. Preferably, in the above salt-lithium separation device applied to the process of extracting lithium from brine, the salt washing liquid conveying mechanism includes a salt washing liquid primary supply assembly and at least one salt washing liquid circulation assembly, and the salt washing liquid primary supply assembly and the salt washing liquid circulation assembly are sequentially connected in series along the opposite direction of the forward direction of the filter cloth. Therefore, the salt concentration of the salt washing liquid conveyed from the liquid outlet end in the direction opposite to the advancing direction of the filter cloth is gradually increased, and the using amount of the salt washing liquid can be saved.
In the above-mentioned salt lithium separator applied to the brine lithium extraction process, the outlet ends of the salt-washing liquid primary supply component and the salt-washing liquid circulation component are both located above the salt-washing area, a salt-washing liquid collection port corresponding to each outlet end is arranged below the salt-washing area, the liquid inlet end of the salt-washing liquid primary supply component is connected with the salt-washing liquid storage tank, and the liquid inlet end of the salt-washing liquid circulation component is connected with the salt-washing liquid primary supply component or the salt-washing liquid collection port corresponding to the previous salt-washing liquid circulation component.
The supply of the salt washing liquid is carried out along the reverse direction of the advancing direction of the filter cloth, the salt washing liquid of the salt washing liquid circulating assembly is collected from a salt washing liquid collecting port of the salt washing liquid primary supply assembly or the previous salt washing liquid circulating assembly, and the salt washing liquid passes through at least one time of salt washing, so the salt concentration of the salt washing liquid at the liquid outlet end of the salt washing liquid circulating assembly is always higher than that of the salt washing liquid primary supply assembly or the previous salt washing liquid circulating assembly, and the reverse elution of the concentration gradient of the salt washing liquid is realized.
Applicants have found that the adsorbent that has captured lithium ions still suffers from lithium ion loss during salt washing, but the shorter the washing time, the lower the rate of lithium ion loss. Therefore, in the salt lithium separation device applied to the brine lithium extraction process, the salt eluent collecting opening is provided with the vacuumizing mechanism. The vacuumizing mechanism can increase the speed of the salt washing liquid passing through the adsorbent, shorten the contact time of the salt washing liquid and the adsorbent, and reduce the lithium amount taken away by the salt washing liquid as much as possible.
Similarly, in the above-mentioned salt-lithium separation device applied to the brine lithium extraction process, a desorption liquid conveying mechanism for conveying desorption liquid to the desorption area is arranged above the filter cloth, and the desorption liquid conveying mechanism has at least two liquid outlet ends arranged along the filter cloth advancing direction. The liquid outlet ends arranged along the advancing direction of the filter cloth can realize 'small-dose multiple desorption', compared with a single liquid outlet end, the liquid outlet ends are arranged to achieve the same desorption effect, the consumption of desorption liquid is less, and higher desorption efficiency can be obtained under the condition of adopting the same amount of desorption liquid.
In the above-mentioned salt lithium separation device applied to the brine lithium extraction process, all the liquid outlet ends are uniformly arranged along the filter cloth advancing direction with the beginning end of the desorption area as the starting point, and the liquid outlet end at the queue tail end is located at the upstream of the tail end of the desorption area. Because the filter cloth is in continuous operation, a certain time is reserved for the desorption liquid to pass through the filter cake, the full desorption is ensured, and the loss of the lithium eluent is also avoided.
In the above salt-lithium separation device applied to the brine lithium extraction process, the desorption liquid conveying mechanism comprises a desorption liquid preliminary supply component and at least one desorption liquid circulation component, and the desorption liquid preliminary supply component and the desorption liquid circulation component are sequentially connected in series along the reverse direction of the filter cloth advancing direction.
The applicant has found that the lower the salt ion concentration in the desorption solution, the higher the lithium elution efficiency. Therefore, the desorption liquid primary supply component and the desorption liquid circulating component are sequentially connected in series along the reverse direction of the filter cloth advancing direction, and the concentration of salt ions on the filter cake is lower and lower along the filter cloth advancing direction, so that the concentration of the salt ions in the lithium eluent is lower and lower along the filter cloth advancing direction; when the reverse elution is carried out, the 'low-salt lithium washing' is realized, and the consumption of the desorption liquid is greatly saved.
In the above-mentioned salt lithium separator applied to the brine lithium extraction process, the desorption liquid initial supply assembly and the liquid outlet end of the desorption liquid circulation assembly are both located above the desorption area, a lithium eluent collection port corresponding to each liquid outlet end is arranged below the desorption area, the liquid inlet end of the desorption liquid initial supply assembly is connected with the desorption liquid storage tank, and the liquid inlet end of the desorption liquid circulation assembly is connected with the lithium eluent collection port corresponding to the desorption liquid initial supply assembly or the previous desorption liquid circulation assembly.
Compared with the prior art, the beneficial effects of the utility model are embodied in:
(1) the utility model utilizes the filter cloth which is in reciprocating rotation operation to bear the filter cake, and the filter cake is formed by the adsorbent which is firstly mixed with brine for adsorption and then separated from the brine; according to different mechanisms arranged above the filter cloth, a salt washing area and a desorption area which are sequentially arranged along the advancing direction of the filter cloth are formed on the filter cloth; because the whole salt washing process is carried out in the dynamic operation process of the filter cloth, the contact time of the salt washing liquid and the adsorbent is short, when the salt washing liquid passes through a filter cake in a short time, the salt washing liquid can elute other salt ions firstly, lithium ions are still remained in crystal lattices of the adsorbent, and the loss of the lithium ions is little; when salt washing is finished, the adsorption capacity of other salt ions on the filter cake is greatly reduced, so that the concentration of the lithium eluent obtained in the desorption region is greatly increased, and effective salt and lithium separation is realized.
(2) The utility model discloses in, wash salt solution conveying mechanism has two at least play liquid ends of arranging along filter cloth direction of advance, and a plurality of play liquid ends of arranging along filter cloth direction of advance can realize "salt is washed many times to the small dose", compare with a single play liquid end, set up a plurality of play liquid ends when reaching the same salt effect of washing, the quantity of washing salt solution still less, and then can obtain higher salt efficiency of washing under the condition that adopts the equivalent to wash salt solution.
(3) In the utility model, along the reverse direction of the filter cloth advancing direction, the salt concentration of the salt washing liquid conveyed by the liquid outlet end is gradually increased; this is because the applicant researches and discovers that the adsorbent which has trapped lithium ions still has lithium ion loss in the salt washing process, but the higher the salt concentration of the salt washing solution, the lower the lithium ion loss rate; because along the filter cloth direction of advance's opposite direction, the concentration of lithium ion is higher on the adsorbent, consequently the utility model discloses also corresponding set the salt concentration of salt washing liquid to gradient elution from low to high to reduce the loss of lithium ion on the adsorbent as far as possible.
(4) The utility model discloses in, this wash salt solution conveying mechanism just supplies subassembly and at least one wash salt solution circulation subassembly including washing salt solution, washes salt solution and just supplies subassembly and wash salt solution circulation subassembly and establish ties in proper order along the opposite direction of filter cloth advancing direction. Therefore, the salt concentration of the salt washing liquid conveyed from the liquid outlet end in the direction opposite to the advancing direction of the filter cloth is gradually increased, and the using amount of the salt washing liquid can be saved.
(5) In the utility model, the desorption liquid conveying mechanism is provided with at least two liquid outlet ends which are arranged along the advancing direction of the filter cloth; the liquid outlet ends arranged along the advancing direction of the filter cloth can realize 'small-dose multiple desorption', compared with a single liquid outlet end, the liquid outlet ends are arranged to achieve the same desorption effect, the consumption of desorption liquid is less, and higher desorption efficiency can be obtained under the condition of adopting the same amount of desorption liquid.
(6) The utility model discloses in, desorption liquid conveying mechanism just supplies subassembly and at least one desorption liquid circulation subassembly including desorption liquid, desorption liquid just supply the subassembly and dissolve the opposite direction of imbibition circulation subassembly along the filter cloth advancing direction and establish ties in proper order. This is because the concentration of salt ions on the filter cake is lower and lower along the filter cloth advancing direction, and therefore the concentration of salt ions in the lithium eluent is lower and lower along the filter cloth advancing direction; when the reverse elution is carried out, the 'low-salt lithium washing' is realized, and the consumption of the desorption liquid is greatly saved.
Drawings
Fig. 1 is a schematic structural diagram of a salt-lithium separation device applied to a brine lithium extraction process of the present invention;
fig. 2 is a schematic view of a second structure of a salt-lithium separation device applied to a brine lithium extraction process of the present invention;
fig. 3 is a third schematic structural diagram of the salt-lithium separation device applied to the brine lithium extraction process of the present invention.
Detailed Description
The technical solution of the present invention will be further described in detail with reference to the accompanying drawings and the detailed description.
Example 1
As shown in fig. 1, the present embodiment is a salt lithium separation device applied to a process of extracting lithium from brine, the salt lithium separation device of the present embodiment is obtained by improving an existing belt vacuum filter, the focus of the present embodiment is detailed description of the improvement point, other undescribed parts are the same as the structure of the existing belt vacuum filter on the market, and the present embodiment is not repeated.
As shown in fig. 1, the salt-lithium separation device applied to the brine lithium extraction process of the embodiment includes a frame 1, a filter cloth 2 that performs reciprocating rotation operation is disposed on the frame 1, the reciprocating rotation operation of the filter cloth 2 is driven by a driving mechanism 3 disposed on the frame 1, and the driving mechanism 3 may include conventional: a driving wheel 31 and a driven wheel 32 rotatably connected to the frame 1, wherein the driving wheel 31 is driven by a circumferential driver (not shown), and the filter cloth 2 is surrounded between the driving wheel 31 and the driven wheel 32.
The filter cloth 2 of the embodiment is preferably a filter cloth 2 with large ventilation volume, and the ventilation volume of the filter cloth 2 is more than 500L/m2S and a retention on the adsorbent of greater than 90%.
As shown in fig. 1, a liquid collecting box 4 positioned below the filter cloth 2 is fixedly installed on the frame 1 between the driving wheel 31 and the driven wheel 32, the top of the liquid collecting box 4 may be provided with an opening, or may not be provided with an opening, but the top of the liquid collecting box 4 is provided with a plurality of filter holes; whether the liquid collecting box is opened or not, a blocking mechanism (not shown in the figure) should be arranged at the top of the liquid collecting box 4, so that liquid is prevented from leaking from two sides of the top of the liquid collecting box 4, and the liquid is ensured to completely enter the liquid collecting box 4.
As shown in fig. 1, a solid-liquid separation zone 100, a salt washing zone 200, and a desorption zone 300 are formed in the frame 1 in this order along the forward direction of the filter cloth 2, depending on the mechanism provided above the filter cloth 2. In order to adapt to the subareas, the liquid collection box 4 is also internally provided with partition plates 41 which are uniformly arranged along the advancing direction of the filter cloth 2, and the partition plates 41 divide the liquid collection box 4 into a plurality of liquid collection cavities 42; the lengths of the solid-liquid separation zone 100, the salt washing zone 200 and the desorption zone 300 are all multiples of the length of the liquid collection chamber 42, and of course, the specific multiples of the solid-liquid separation zone 100, the salt washing zone 200 and the desorption zone 300 may be the same or different, depending on the specific design requirements.
As shown in FIG. 1, in the present embodiment, the solid-liquid separation zone 100 has a length corresponding to the length of four liquid collecting chambers 42, and the salt washing zone 200 and the desorption zone 300 have a length corresponding to the length of three liquid collecting chambers 42. The length of each functional area is set to be the multiple of the length of the liquid collecting cavity 42, so that the corresponding liquid of each functional area can enter the corresponding liquid collecting cavity 42.
In this embodiment, the length of the liquid collection chamber 42 can be specifically set according to specific needs.
As can be seen from FIG. 1, in the three functional zones of this embodiment, a mixing and adsorbing mechanism 5 is arranged above the filter cloth 2 in the solid-liquid separation zone 100; the mixed adsorption mechanism 5 comprises a mixing tank 51, the top of the mixing tank 51 is provided with a brine feed port 52 and an adsorbent feed port 53, raw brine and an adsorbent respectively enter the mixing tank 51 through the corresponding feed ports, and under the action of a stirring assembly 54, the adsorbent and the raw brine are mixed and adsorbed in the mixing tank 51 to obtain an adsorbent brine mixture; the adsorbent brine mixture is discharged from the mixing tank 51 and is conveyed to the filter cloth 2 of the solid-liquid separation zone 100; due to the filtering effect of the filter cloth 2, the adsorbent which has adsorbed various ions in the brine is separated from the brine, the adsorbent is remained on the filter cloth 2, and the brine passes through the filter cloth 2 and enters the corresponding liquid collection cavity 42.
As shown in fig. 1, a brine recovery port 43 is formed at the bottom of each liquid collection cavity 42 corresponding to the solid-liquid separation zone 100, each brine recovery port 43 is connected to a brine filtering barrel 44 through a pipeline, the brine filtering barrel 44 is connected to a vacuum pumping mechanism (such as a vacuum pump, not shown in the figure), brine can rapidly pass through the filter cloth 2 to enter the liquid collection cavity 42 and the brine filtering barrel 44 under the action of the vacuum pumping mechanism, and the adsorbent can form a filter cake with a thickness of about 1.5-4 cm on the filter cloth 2.
As can be seen from fig. 1, in order to ensure sufficient collection of brine, the discharge end of the mixed adsorption mechanism 5 is located at the initial end of the solid-liquid separation zone 100 (i.e. the end away from the salt-washing zone 200), so as to ensure that all brine enters the liquid collection chamber 42 corresponding to the solid-liquid separation zone 100 and does not enter the downstream salt-washing zone 200.
Since the adsorbent used in this embodiment is a powdered adsorbent (amorphous aluminum hydroxide adsorbent with a particle size of 75 μm), it is difficult for the filter cloth 2 to completely block the adsorbent, and the collected brine may contain more or less of the adsorbent. At this time, the adsorbent should be separated from the collected brine by using a screening device such as a magnetic separator 500, a precision filter, etc., and then the brine is returned to the salt pan or the salt lake.
As shown in fig. 1, in the salt-washing zone 200, a salt-washing liquid conveying mechanism 6 is disposed above the filter cloth 2, and the salt-washing liquid conveying mechanism 6 is used for applying a salt-washing liquid to the filter cake entering the salt-washing zone 200 along with the filter cloth 2. The salt washing solution used in this embodiment may be fresh water or other solution with low salinity. The salt washing liquid conveying mechanism 6 adopts liquid conveying equipment commonly used in the prior art, and only needs to ensure uniform transfusion in the vertical direction, and can comprise a salt washing liquid conveying pipe 61 connected with a salt washing liquid storage tank (not shown in the figure), wherein a salt washing liquid conveying pump (not shown in the figure) is installed on the salt washing liquid conveying pipe 61, a water distribution disc (not shown in the figure) can be installed at the liquid outlet end of the salt washing liquid conveying pipe 61, the water distribution diameter of the water distribution disc is equivalent to the width of a filter cake, and the salt washing effect is ensured.
Similarly, the bottom of each liquid collecting cavity 42 corresponding to the salt washing area 200 is provided with a salt eluent collecting port 45, each salt eluent collecting port 45 is connected with a salt eluent pumping barrel 46 through a pipeline, the salt eluent pumping barrel 46 is connected with a vacuum pumping mechanism (such as a vacuum pump), under the action of the vacuum pumping mechanism, the salt washing liquid can rapidly penetrate through the filter cake, and the contact time of the salt washing liquid and the filter cake is controlled within 10 seconds (preferably 1-2 seconds).
Likewise, to ensure adequate collection of the salt eluate, the outlet end of the salt eluate delivery mechanism 6 is at the beginning of the salt elution zone 200 (i.e., the end proximate the solid-liquid separation zone 100), ensuring that all of the salt eluate enters the liquid collection chamber 42 corresponding to the salt elution zone 200 and not the downstream desorption zone 300.
According to the research of the applicant, as the brine is a high-salt even salt saturated solution, when the brine is mixed with the adsorbent, various salt ions including lithium ions can be adsorbed on the adsorbent; however, the adsorption mechanism of lithium ions is different from that of other salt ions, lithium ions are squeezed into crystal lattices of the powdery lithium ion selective adsorbent by the salt in the brine to form a molecular sieve, and other salt ions cannot enter the crystal lattices of the powdery lithium ion selective adsorbent, so that the bonding strength between the lithium ions and the adsorbent is different from that between the other salt ions and the adsorbent. Because the combination of salt ions and the adsorbent is weak, in the salt washing area 200, the filter cake is quickly washed by the salt washing liquid in a short time, so that the salt ions can be taken away to the maximum extent, the lithium ions can be taken away to the minimum extent, and the purpose of 'throwing salt and leaving lithium' is achieved.
The collected salt eluent can be sent to a salt lake or a salt pan after being subjected to the recovery of the adsorbent, or can be used in other processes.
As shown in fig. 1, a desorption liquid delivery mechanism 7 is disposed above the filter cloth 2 in the desorption zone 300, and the desorption liquid delivery mechanism 7 is used for delivering a desorption liquid to the filter cake entering the desorption zone 300 along with the filter cloth 2, wherein the desorption liquid used in the present embodiment may be fresh water or other solution with lower salinity. The desorption liquid conveying mechanism 7 may be a liquid conveying device commonly used in the art as long as uniform liquid conveyance in the vertical direction is ensured, and may be of the same structure as the aforementioned wash salt liquid conveying mechanism 6.
Similarly, the bottom of each liquid collecting cavity 42 corresponding to the desorption area 300 is provided with a lithium eluent collecting port 47, each lithium eluent collecting port 47 is connected with a lithium eluent pumping barrel 48 through a pipeline, the lithium eluent pumping barrel 48 is connected with a vacuum pumping mechanism (such as a vacuum pump), and the desorption liquid can rapidly pass through the filter cake under the action of the vacuum pumping mechanism, so that the contact time of the desorption liquid and the filter cake is controlled within 10 seconds, preferably 1-2 seconds.
Likewise, to ensure sufficient collection of the lithium eluate, the liquid outlet end of the desorption liquid delivery mechanism 7 is located at the beginning of the desorption region 300 (i.e., the end near the salt elution region 200), ensuring that all the lithium desorption liquid enters the liquid collection chamber 42 corresponding to the desorption region 300.
After the ions except lithium on the adsorbent are pre-eluted through the salt eluting region 200, the salt-lithium ratio on the adsorbent is greatly reduced, and at the moment, the lithium ions on the adsorbent are eluted by desorption liquid, so that lithium eluent with higher lithium concentration can be obtained.
Similarly, the lithium eluate is inevitably doped with an adsorbent, so that the adsorbent needs to be separated from the collected lithium eluate by using a screening device such as a magnetic separator and a precision filter, and then the lithium eluate is sent to the next refining process.
At the end point of the filter cloth advancing direction, the desorbed adsorbent is collected by the adsorbent recovery mechanism 8 and sent to the mixed adsorption mechanism 5 for recycling.
The application method of the belt filter in the adsorption method for extracting lithium from brine comprises the following steps:
(1) uniformly mixing the adsorbent and brine in a mixed adsorption mechanism 5;
feeding the adsorbent and the brine into a mixing tank 51 in proportion, starting a stirring assembly, uniformly stirring the adsorbent and the brine, and adsorbing various ions in the brine by the adsorbent in the stirring process; when the production line is initially started, the adsorbent and brine are stirred in the mixing tank 51 for a period of time (about several minutes) and then discharged, so as to ensure effective adsorption of the adsorbent; after the production line begins to operate, the adsorbent and the brine can be continuously fed, and the adsorbent and brine mixture can also be continuously discharged.
(2) Conveying the adsorbent brine mixture to a solid-liquid separation zone 100 to separate the adsorbent from the brine and make the adsorbent into a filter cake on a filter cloth 2;
after the adsorbent is adsorbed, discharging the adsorbent brine mixture from the mixing tank 51, wherein the discharge end of the mixing tank 51 is positioned at the starting end of the solid-liquid separation zone 100, the adsorbent brine mixture discharged from the mixing tank 51 gradually falls on the running filter cloth 2, and under the assistance of a vacuumizing mechanism, the brine passes through the filter cloth 2 and enters the corresponding liquid collection cavity 42, and is collected into a brine leaching barrel 44 through each brine recovery port 43; the recovered brine can be returned to a salt lake or a salt pan after being separated by an adsorbent;
on the filter cloth 2 running at a constant speed, the adsorbent discharged at a constant speed forms a filter cake with the thickness of about 1.5-4 cm under the action of a vacuum pumping mechanism; due to the continuous discharge, the filter cake extends over the entire travel of the filter cloth 2.
(3) The filter cake goes to a salt washing area 200 along with the filter cloth 2, in the salt washing area 200, a salt washing liquid conveying mechanism 6 conveys the salt washing liquid to the filter cake, so that ions adsorbed on the filter cake except lithium are eluted, and a salt eluent is collected;
the salt washing liquid is applied to the filter cake from the starting end of the salt washing area 200, and only needs 1-2 seconds for the salt washing liquid to pass through the filter cake with the assistance of a vacuumizing mechanism, and the salt is thrown and lithium is left as far as possible;
the collected salt eluent can be sent to a salt lake or a salt pan, or used in other processes;
(4) the filter cake goes to the desorption area 300 along with the filter cloth 2, and in the desorption area 300, a desorption liquid conveying mechanism 7 conveys desorption liquid to the filter cake to enable lithium ions adsorbed on the filter cake to be eluted, and lithium eluent is collected;
the desorption liquid is distributed to the filter cloth 2 from the starting end of the desorption area 300, and passes through the filter cake with the assistance of the vacuum pumping mechanism, so that lithium is eluted from the adsorbent; the collected lithium eluent is sent to a downstream procedure for refining and purification after passing through a separation adsorbent;
(5) and at the end point of the advancing direction of the filter cloth 2, conveying the desorbed adsorbent to a mixed adsorption mechanism 5, and performing a new cycle of lithium extraction from the adsorption brine.
Example 2
As shown in fig. 2, in this embodiment, the main structure of the salt-lithium separation device applied to the brine lithium extraction process is the same as that of embodiment 1, except that: the salt-washing liquid conveying mechanism 6 of the salt-washing area 200 has at least two liquid outlet ends (three are provided in the embodiment), and all the liquid outlet ends are uniformly arranged along the advancing direction of the filter cloth 2.
The specific mode of arranging the three liquid outlet ends can be as follows: three salt washing liquid conveying pipes 61 are arranged, the three salt washing liquid conveying pipes 61 are connected with a salt washing liquid storage tank through a four-way valve, a water distribution disc is mounted at the liquid outlet end of each salt washing liquid conveying pipe 61, the water distribution diameter of each water distribution disc is equivalent to the width of a filter cake, and the salt washing effect is ensured.
When the salt washing liquid is conveyed, one salt washing liquid conveying pump is adopted to provide power for three salt washing liquid conveying pipes 61 at the same time, or one salt washing liquid conveying pump is arranged on each salt washing liquid conveying pipe 61, and the method and the device can be implemented.
Similarly, the outlet ends of the salt-washing liquid conveying mechanism 6 are uniformly arranged with the starting end of the salt-washing area 200 as the starting point, and ensure that the outlet end at the tail end of the queue is slightly far away from the tail end of the salt-washing area 200, so as to reserve a certain time for the salt-washing liquid filtering cake and ensure that the salt eluent does not enter the desorption area 300.
Compared with the embodiment 1 with only one liquid outlet end, the total amount of the salt washing liquid used by a plurality of liquid outlet ends is unchanged, but the salt washing efficiency is higher because the salt washing is realized by 'washing for a plurality of times with small dosage'.
Example 3
As shown in fig. 2, in this embodiment, the main structure of the salt-lithium separation device applied to the brine lithium extraction process is the same as that in embodiment 1 or embodiment 2, except that: the desorption liquid conveying mechanism 7 of the desorption zone 300 has at least two liquid outlet ends (three are provided in this embodiment), and all the liquid outlet ends are uniformly arranged along the advancing direction of the filter cloth 2.
The desorption liquid conveying mechanism 7 with a plurality of liquid outlet ends can be arranged in the same way as the salt washing liquid conveying mechanism 6 in the embodiment 3, and a plurality of desorption liquid conveying pipes 71 are also arranged.
Compared with the case of only one liquid outlet end in the embodiment 1, the total amount of the desorption liquid used by a plurality of liquid outlet ends is unchanged, but the desorption efficiency is higher because the small-dose multiple washing is realized during desorption, and the lithium recovery rate can be further improved.
Example 4
As shown in fig. 3, in this embodiment, the main structure of the salt-lithium separation device applied to the brine lithium extraction process is the same as that in embodiment 1 or 3, except that: the salt washing liquid conveying mechanism 6 of the salt washing area 200 is provided with at least two liquid outlet ends (three are provided in the embodiment), and all the liquid outlet ends are uniformly arranged along the advancing direction of the filter cloth 2; in addition, the salt concentration of the salt washing solution conveyed by each liquid outlet end is gradually increased along the direction opposite to the advancing direction of the filter cloth 2.
The specific setting mode of the salt washing liquid conveying mechanism 6 can be as follows: the salt washing liquid conveying mechanism 6 comprises two salt washing liquid primary supply assemblies 62 and at least one salt washing liquid circulating assembly 63, and the salt washing liquid primary supply assemblies 62 and the salt washing liquid circulating assemblies 63 are sequentially connected in series along the opposite direction of the advancing direction of the filter cloth 2.
In this embodiment, the structures of the salt-washing liquid primary supply assembly 62 and the salt-washing liquid circulation assembly 63 are the same, and the structures of the salt-washing liquid primary supply assembly 62 and the salt-washing liquid circulation assembly 63 may be the same as those of the salt-washing liquid conveying mechanism 6 in embodiment 1, the liquid outlet ends of the salt-washing liquid primary supply assembly 62 and the salt-washing liquid circulation assembly 63 are both located above the salt-washing area 200, and the salt-washing liquid suction-filtration barrels 46 corresponding to the liquid outlet ends are arranged below the salt-washing area 200; however, the positions of the liquid inlet ends of the salt washing liquid primary supply assembly 62 and the salt washing liquid circulation assembly 63 are connected correspondingly are different, wherein the liquid inlet end of the salt washing liquid primary supply assembly 62 is connected with the salt washing liquid storage tank, and the liquid inlet end of the salt washing liquid circulation assembly 63 is connected with the salt eluent suction-filtration barrel 46 corresponding to the salt washing liquid primary supply assembly 62, or is connected with the salt eluent suction-filtration barrel 46 corresponding to the last salt washing liquid circulation assembly 63.
The supply of the salt washing liquid is carried out along the reverse direction of the advancing direction of the filter cloth 2, the salt washing liquid of the salt washing liquid circulating assembly 63 is collected from the salt washing liquid suction and filtration barrel 46 of the salt washing liquid primary supply assembly 62 or the previous salt washing liquid circulating assembly 63, and the salt washing liquid passes through at least one time, so the salt concentration of the salt washing liquid at the liquid outlet end of the salt washing liquid circulating assembly 63 is always higher than that of the salt washing liquid primary supply assembly 62 or the previous salt washing liquid circulating assembly 63, and the concentration gradient reverse elution of the salt washing liquid is realized.
The applicant researches and discovers that the adsorbent trapping lithium ions still has lithium ion loss in the salt washing process, but the higher the salt concentration of the salt washing solution, the lower the lithium ion loss rate. Therefore, the present embodiment provides the above-mentioned reverse elution manner with a concentration gradient of the salt-washing solution, so as to reduce the loss of lithium ions on the adsorbent during the salt-washing process as much as possible.
Similarly, in this embodiment, the outlet ends of the salt-washing liquid conveying mechanism 6 are uniformly arranged with the starting end of the salt-washing area 200 as the starting point, so as to ensure that the last outlet end is slightly far away from the tail end of the salt-washing area 200, so as to reserve a certain time for the salt-washing liquid filtering cake, and ensure that the salt eluent does not enter the desorption area 300.
Example 5
As shown in fig. 3, in this embodiment, the main structure of the salt-lithium separation device applied to the brine lithium extraction process is the same as that in embodiment 1, embodiment 2 or embodiment 4, except that: the desorption liquid conveying mechanism 7 of the desorption area 300 is provided with at least two liquid outlet ends (three liquid outlet ends are provided in the embodiment), and all the liquid outlet ends are uniformly arranged along the advancing direction of the filter cloth 2; the desorption liquid conveying mechanism 7 comprises a desorption liquid initial supply component 72 and at least one desorption liquid circulation component 73, wherein the desorption liquid initial supply component 72 and the desorption liquid circulation component 73 are sequentially connected in series along the direction opposite to the advancing direction of the filter cloth 2.
In this embodiment, the structure of the desorption liquid conveying mechanism 7 is the same as that of the wash salt liquid conveying mechanism 6 in embodiment 5.
Claims (10)
1. The utility model provides a be applied to brine and carry lithium process's salt lithium separator, its characterized in that, includes frame (1), frame (1) on be equipped with reciprocal rotary motion's filter cloth (2), be equipped with in proper order along filter cloth (2) advancing direction:
a salt washing liquid conveying mechanism (6) for conveying the salt washing liquid to the salt washing area (200) is distributed above the filter cloth (2);
the device comprises a desorption area (300), wherein a desorption liquid conveying mechanism (7) for conveying desorption liquid to the desorption area (300) is distributed above the filter cloth (2), and a lithium eluent collecting port (47) is arranged below the desorption area (300).
2. The device for separating the salt and the lithium applied to the brine lithium extraction process in claim 1, wherein the washing salt solution conveying mechanism (6) is provided with at least two liquid outlet ends arranged along the advancing direction of the filter cloth (2).
3. The apparatus of claim 2, wherein all the outlet ends are uniformly arranged along the advancing direction of the filter cloth (2) with the beginning of the salt-washing area (200) as the starting point, and the outlet end at the tail end of the queue is located at the upstream of the end of the salt-washing area (200).
4. The device for separating the salt and the lithium applied to the process of extracting the lithium from the brine as claimed in claim 2 or 3, wherein the salt concentration of the salt washing solution conveyed from the liquid outlet end is gradually higher along the direction opposite to the advancing direction of the filter cloth (2).
5. The device for separating the salt and the lithium, which is applied to the process of extracting the lithium from the brine, according to claim 4, is characterized in that the salt washing liquid conveying mechanism (6) comprises a salt washing liquid primary supply assembly (62) and at least one salt washing liquid circulating assembly (63), and the salt washing liquid primary supply assembly (62) and the salt washing liquid circulating assembly (63) are sequentially connected in series along the direction opposite to the advancing direction of the filter cloth (2).
6. The salt-lithium separation device applied to the process of extracting lithium from brine according to claim 5, wherein the outlet ends of the primary salt-washing liquid supply assembly (62) and the salt-washing liquid circulation assembly (63) are both positioned above the salt-washing area (200), a salt eluent collection port (45) corresponding to each outlet end is arranged below the salt-washing area (200), the inlet end of the primary salt-washing liquid supply assembly (62) is connected with a salt-washing liquid storage tank, and the inlet end of the salt-washing liquid circulation assembly (63) is connected with a salt eluent collection port (45) corresponding to the primary salt-washing liquid supply assembly (62) or the previous salt-washing liquid circulation assembly (63).
7. The device for separating the salt and the lithium, applied to the process of extracting the lithium from the brine, according to claim 6, is characterized in that a vacuum-pumping mechanism is arranged at the salt eluent collecting port (45).
8. The apparatus for separating lithium salt from brine for use in lithium extraction according to any of claims 1-3 and 5-7, wherein the desorption liquid conveying mechanism (7) has at least two liquid outlet ends arranged along the advancing direction of the filter cloth (2).
9. The device for separating the salt and the lithium applied to the brine lithium extraction process according to claim 8, wherein the desorption liquid conveying mechanism (7) comprises a desorption liquid initial supply component (72) and at least one desorption liquid circulation component (73), and the desorption liquid initial supply component (72) and the desorption liquid circulation component (73) are sequentially connected in series along the direction opposite to the advancing direction of the filter cloth (2).
10. The device for separating salt and lithium applied to the process of extracting lithium from brine according to claim 9, wherein the desorption liquid initial supply assembly (72) and the liquid outlet ends of the desorption liquid circulation assembly (73) are both positioned above the desorption area (300), lithium eluent collecting ports (47) corresponding to the liquid outlet ends are arranged below the desorption area (300), the liquid inlet end of the desorption liquid initial supply assembly (72) is connected with a desorption liquid storage tank, and the liquid inlet end of the desorption liquid circulation assembly (73) is connected with the lithium eluent collecting port (47) corresponding to the desorption liquid initial supply assembly (72) or the previous desorption liquid circulation assembly (73).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021316798.8U CN213221252U (en) | 2020-07-07 | 2020-07-07 | Salt lithium separation device applied to brine lithium extraction process |
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| CN202021316798.8U CN213221252U (en) | 2020-07-07 | 2020-07-07 | Salt lithium separation device applied to brine lithium extraction process |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022007662A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Band filter and application thereof in extraction of lithium from brine using adsorption method |
| WO2022007811A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Device for extracting lithium from brine by using adsorption method |
| WO2022007660A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdered adsorbent |
-
2020
- 2020-07-07 CN CN202021316798.8U patent/CN213221252U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022007662A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Band filter and application thereof in extraction of lithium from brine using adsorption method |
| WO2022007811A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Device for extracting lithium from brine by using adsorption method |
| WO2022007660A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdered adsorbent |
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Address after: Room 101, No. 15 Chuncheng Road, Quzhou City, Zhejiang Province, 324012 Patentee after: Quzhou Yongzheng Lithium Industry Technology Co.,Ltd. Address before: 810000 room 1013, building 1, No. 457, Qiyi Road, Chengzhong District, Xining City, Qinghai Province Patentee before: Xining Yongzheng Lithium Industry Co.,Ltd. |