CN107058735A - It is a kind of extract lithium continuous ion exchange unit and put forward lithium technique - Google Patents
It is a kind of extract lithium continuous ion exchange unit and put forward lithium technique Download PDFInfo
- Publication number
- CN107058735A CN107058735A CN201611155382.0A CN201611155382A CN107058735A CN 107058735 A CN107058735 A CN 107058735A CN 201611155382 A CN201611155382 A CN 201611155382A CN 107058735 A CN107058735 A CN 107058735A
- Authority
- CN
- China
- Prior art keywords
- area
- adsorption
- desorption
- elution
- lithium
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 91
- 238000000034 method Methods 0.000 title claims abstract description 39
- 238000005342 ion exchange Methods 0.000 title claims abstract description 26
- 239000000284 extract Substances 0.000 title claims abstract description 7
- 238000001179 sorption measurement Methods 0.000 claims abstract description 258
- 238000003795 desorption Methods 0.000 claims abstract description 140
- 238000010828 elution Methods 0.000 claims abstract description 112
- NJPPVKZQTLUDBO-UHFFFAOYSA-N novaluron Chemical compound C1=C(Cl)C(OC(F)(F)C(OC(F)(F)F)F)=CC=C1NC(=O)NC(=O)C1=C(F)C=CC=C1F NJPPVKZQTLUDBO-UHFFFAOYSA-N 0.000 claims abstract description 53
- 238000000605 extraction Methods 0.000 claims abstract description 15
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 70
- 239000000463 material Substances 0.000 claims description 36
- 239000003463 adsorbent Substances 0.000 claims description 24
- 238000010521 absorption reaction Methods 0.000 claims description 22
- 238000009826 distribution Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 9
- 241001131796 Botaurus stellaris Species 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 239000012267 brine Substances 0.000 description 4
- 238000011068 loading method Methods 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 4
- -1 adsorption zone Chemical compound 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- 239000004411 aluminium Substances 0.000 description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000011010 flushing procedure Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000013535 sea water Substances 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 238000012432 intermediate storage Methods 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000006210 lotion Substances 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004080 punching Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/42—Treatment or purification of solutions, e.g. obtained by leaching by ion-exchange extraction
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B26/00—Obtaining alkali, alkaline earth metals or magnesium
- C22B26/10—Obtaining alkali metals
- C22B26/12—Obtaining lithium
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Manufacturing & Machinery (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Treatment Of Liquids With Adsorbents In General (AREA)
Abstract
The invention discloses it is a kind of extract lithium continuous ion exchange unit and put forward lithium technique, extracting the continuous ion exchange unit of lithium includes operation pedestal and multiple adsorption columns, running pedestal includes adsorption zone, elute area and desorption area, multiple adsorption columns are arranged on operation pedestal, and it is distributed in adsorption zone, elute and set in area and desorption area, adsorption column in adsorption zone is connected with raw material feed tube, adsorption column in elution area is connected with elution feed tube, adsorption column in desorption area is connected with desorption feed tube, run the adsorption zone on pedestal, the position in elution area and desorption area substitutes successively.Lithium technique is put forward using above-mentioned continuous ion exchange unit, over time with the operating of operation pedestal, adsorption zone, elution area and desorption area on operation pedestal carry out adsorption operations, elution operation and desorption manipulation respectively, and each region is converted in consecutive intervals, so that the operation for entirely extracting lithium is in extremely rapid succession carried out, the benefit that the extraction efficiency and resource synthetic development of lithium are utilized is improved.
Description
Technical field
The present invention relates to salt solution (containing bittern) or the technical field of Extracting Lithium from Seawater technique, and in particular to a kind of company of extraction lithium
Continue ion interchange unit and put forward lithium technique.
Background technology
Lithium is a kind of argenteous metallic element, and it is widely used in rechargeable battery, glass, ceramics, alloy, lubrication
Agent, medicine and other fields, especially chargeable lithium cell are in recent years as hybrid vehicle and the main power source of electric automobile
And widely paid close attention to.In addition, lithium is used for into the existing compact batteries such as mobile phone, notebook computer, there is also huge city
.Therefore, home and overseas is all very big to the demand of lithium in whole industrial circle.
Salt lake bittern type lithium deposite accounts for the 66% of world's lithium resource, and the existing method that lithium is extracted from salt lake bittern includes
The precipitation method, calcining lixiviation process, solvent extraction, membrane separation process, absorption method etc., wherein absorption method have that technique is simple, the rate of recovery
High, environment-friendly the features such as, be the method for most application prospect.But existing absorption method is generally that interval puies forward lithium technique, it is impossible to realized
The quick of lithium technique is carried to be carried out continuously, and exist many required production equipments, complex operation, time-consuming, cost of investment height,
The problems such as recovery rate of lithium is not high.Therefore, realize that the operation for carrying lithium is unfavorable for the demand of industry development using traditional technique, no
Beneficial to the development of salt lake resources comprehensive development and utilization.
The content of the invention
It is existing for solving it is an object of the invention to provide a kind of continuous ion exchange unit and method for extracting lithium
Putting forward lithium technique can not in extremely rapid succession be carried out, and the production equipment needed for the method for traditional extraction lithium is more, technological operation is multiple
It is miscellaneous, the problem of time-consuming, cost of investment is high, the recovery rate of lithium is low.
To achieve these goals, the first technical scheme of the invention is a kind of continuous ion exchange unit for extracting lithium,
Characterized in that, the continuous ion exchange unit for extracting lithium includes operation pedestal and multiple adsorption columns, the operation pedestal
Including adsorption zone, elution area and desorption area, multiple adsorption columns are arranged on the operation pedestal, and are distributed in the absorption
Set in area, the elution area and the desorption area,
Adsorption column in the adsorption zone is connected with raw material feed tube, the adsorption column in the elution area and elution feed tube
Adsorption column in connection, the desorption area is connected with desorption feed tube,
The position of adsorption zone, elution area and desorption area on the operation pedestal substitutes successively.
Preferably, the continuous ion exchange unit for extracting lithium also includes distributing valve, and the distributing valve includes round end
And fixing end, the fixing end and round end of the distributing valve offer the notch of identical quantity,
Each notch of the round end is connected with corresponding each adsorption column,
Multiple notches of the fixing end are divided into adsorption zone, elution area and desorption area, are distributed in the notch of the adsorption zone
Connected with raw material feed tube, the notch for being distributed in the elution area is connected with elution feed tube, is distributed in the groove in the desorption area
Mouth is connected with desorption feed tube.
Preferably, the operation pedestal includes rotating disk and promotes the driver of turntable rotation, and multiple adsorption columns are in ring
Shape is arranged on the rotating disk.
Preferably, top layer distributor and bottom distributor, the top layer distributor are provided with each adsorption column
Aperture with the bottom distributor is 2~6mm.
Compared to prior art, the first technical scheme of the present invention extract lithium continuous ion exchange unit have with
Lower advantage：The present invention extract lithium continuous ion exchange unit may be such that each adsorption column absorption, elute desorption manipulation between according to
Secondary continuous switching, forms the continuous process that lithium is extracted, effectively improves the extraction rate of lithium, improves ion exchange effect
Rate, reduces supplement quantity of sorbent, the benefit of salt lake resources comprehensive development and utilization is improved, the need for meeting industry development.This
Outside, the continuous ion exchange unit of the present invention for extracting lithium can be realized by the equipment of automation, therefore shorten process
Operating time, operation operating process more facilitates, and cost is relatively low.
The second technical scheme of the present invention exchanges dress for a kind of continuous ionic of the extraction lithium using in the first technical scheme
That puts puies forward lithium technique, it is characterised in that comprise the following steps：
S1：Period 1：The adsorption column that operation pedestal is divided into adsorption zone, elution area and desorption area, the adsorption zone enters
Material liquid is transported in the adsorption column in adsorption zone by row adsorption operations, is entered after the adsorbent adsorption saturation in area to be adsorbed
Second round；
S2：Second round：Run pedestal operating once, the adsorption zone in step S1 substitutes to elute in area, step S1
It is that the adsorption column in adsorption zone, adsorption zone carries out adsorption operations to elute area to substitute the desorption area replacement for being to be desorbed in area, step S1
Material liquid is transported in the adsorption column after substituting in adsorption zone, meanwhile, the adsorption column in elution area carries out elution operation and is
Leacheate is transported in the adsorption column after substituting in elution area；
S3：Period 3：Operation pedestal is operated again, and the elution area in step S2 substitutes to be desorbed in area, step S2
It is that the adsorption zone in adsorption zone, step S2 substitutes for elution area to be desorbed area's replacement, and the adsorption column being desorbed in area carries out desorption manipulation
Desorption liquid is transported in the adsorption column after substituting in desorption area, meanwhile, the adsorption column in elution area carries out elution operation and is
Leacheate is transported in the adsorption column after substituting in elution area, the adsorption column in adsorption zone carries out adsorption operations i.e. by material liquid
It is transported in the adsorption column after substituting in adsorption zone；
S4：Period 4：Operation pedestal is operated again, and desorption area in step S3, which substitutes, is adsorption zone, step S3
Adsorption zone replacement is that the elution area in elution area, step S3 substitutes to be desorbed area, adsorption zone, elution area and desorption area after replacement
Interior adsorption column carries out adsorption operations, elution operation and desorption manipulation simultaneously respectively；
S5：At interval of a period run once, adsorption zone, elution area and desorption area substitute operation pedestal successively, also, institute
Adsorption zone, the elution area and the desorption area are stated respectively while carrying out adsorption operations, elution operation and desorption manipulation.
Preferably, the time in each cycle is 0.5~3h.
Preferably, the temperature of the desorption liquid is 20~60 DEG C.
Preferably, the feed rate of the material liquid is 5~20BV/h；The feed rate of the leacheate is 2~10BV/
h；The discharging flow of the desorption liquid is 5~15BV/h.
Preferably, the material liquid is from the bottom feed of the adsorption column, and the leacheate and the desorption liquid are from suction
Its top feed of attached column.
Compared to prior art, the second technical scheme of the present invention puies forward lithium technique and had the advantage that：Using this hair
It is bright it is described carry lithium technique can by adsorption column in absorption, elute and be switched between desorption manipulation, so as to complete the extraction of lithium
Operation, and multiple adsorption columns can be operated simultaneously, effectively increase the extraction efficiency of lithium.It is of the present invention to put forward lithium technique
Process is simple, and easy to operate, the usage amount of lithium adsorbent is also little, and cost is significantly reduced, and production efficiency is improved, with significant
Economic benefit.
Brief description of the drawings
By reading the detailed description of hereafter preferred embodiment, various other advantages and benefit is common for this area
Technical staff will be clear understanding.Accompanying drawing is only used for showing the purpose of preferred embodiment, and is not considered as to the present invention
Limitation.In the accompanying drawings：
Fig. 1 shows a kind of structural representation for the continuous ion exchange unit for extracting lithium of the present invention.
Label declaration
10- operation pedestals, 20- adsorption columns,
21- top layer distributors, 22- bottom distributors,
30- adsorption zones, 40- elution area,
50- desorptions area, 60- distributing valves,
61- fixing ends, 62- round ends,
63- notches, 70- raw material feed tubes,
80- elutes feed tube, 90- desorption feed tubes.
Embodiment
The invention provides many applicable creative concepts, the creative concept can be reflected in a large number of on specific
Hereinafter.Specific embodiment described in following embodiments of the present invention is only as embodiment of the invention
Exemplary illustration, and be not meant to limit the scope of the invention.
The invention will be further described with specific embodiment below in conjunction with the accompanying drawings.
Fig. 1 is a kind of structural representation for the continuous ion exchange unit for extracting lithium of the present invention.As shown in figure 1, extracting lithium
Continuous ion exchange unit include operation pedestal 10 and multiple adsorption columns 20, operation pedestal 10 includes adsorption zone 30, elution
Area 40 and desorption area 50, multiple adsorption columns 20 are arranged on operation pedestal 10, and distribution is arranged on adsorption zone 30, elution area 40
In desorption area 50, the adsorption column 20 in adsorption zone 30 is connected with raw material feed tube 70, and the adsorption column 20 in elution area 40 is with drenching
Feed tube 80 is washed to connect, desorption area 50 in adsorption column 20 with desorption feed tube 90 connect, run pedestal 10 on adsorption zone 30,
The position in elution area 40 and desorption area 50 substitutes successively.
Material liquid is transported in the adsorption column 20 of adsorption zone 30 by raw material feed tube 70, the material liquid be containing
There is the liquid of lithium, such as salt lake bittern, seawater.Lithium adsorbent is filled with adsorption column 20, lithium adsorbent is that one kind can be to gas
Lithium in body or liquid material has the solid matter of adsorption function, mainly includes manganese systems adsorbent, aluminium system adsorbent, the suction of titanium system
Attached dose and compound stibate adsorbent.Lithium adsorbent in the present embodiment uses aluminium system adsorbent.Material liquid flows through absorption
Post 20 be mobile phase, using lithium adsorbent in adsorption column 20 to the absorption affinity size of various different components in material liquid so that
Each component is separated, and lithium is attracted to absorbent interior.After adsorbent adsorption saturation in post 20 to be adsorbed, by running pedestal 10
Operating so that adsorption zone 30 reach elution area 40 position, elution area 40 reach desorption area 50 position, desorption area 50 reach
The position of adsorption zone 30.In elution area 40, leacheate is transported to positioned at the absorption for eluting area 40 by eluting feed tube 80
In post 20 so that under the flushing of leacheate, substantial amounts of material liquid in adsorption column 20 is got rid of, it is miscellaneous in final product to reduce
Leacheate in matter composition, the present embodiment is normal temperature light salt brine.After elution operation, operation pedestal 10 is operated again so that drenched
The position that area 40 reaches desorption area 50 is washed, desorption area 50 reaches the position of adsorption zone 30, and adsorption zone 30 reaches the position in elution area 40
Put.In desorption area 50, desorption liquid is transported in the adsorption column 20 in desorption area 50 by being desorbed feed tube 90 so that
In the presence of desorption liquid, lithium is desorbed from lithium adsorbent and come out, the desorption liquid exported from adsorption column 20 is reclaimed, then
Via the operation such as evaporation, the lithium in desorption liquid is extracted.This is absorption, elution and the desorption in lithium extraction process,
In the present invention, due to being provided with operation pedestal 10, adsorption zone 30, elution area 40 and desorption area 50 can be caused to substitute successively, therefore
In the present invention, each adsorption column 20 in adsorption zone 30, elution area 40 and desorption area 50 can be in working condition simultaneously, so that
Form the continuous extraction effect of lithium.
Absorption feed tube can be passed directly into the water source of salt lake bittern, and salt lake bittern is conveyed, and elute feed tube 80
Directly it can be connected with light salt brine or running water water source, to realize that current are conveyed, by the material liquid (salt lake bittern) of adsorption column 20
Or leacheate can be directly discharged in the water source of salt lake bittern, if the present apparatus is distant with water source, all kinds of storages also can be set
Tank is stored to material liquid, leacheate etc..
It can quickly and efficiently switch its to any one or one group of adsorption column 20 by being provided with operation pedestal 10 to run
Pattern so that lithium can be carried out efficiently and rapidly during extraction, is located at adsorption zone 30, elution area while running on pedestal 10
40 can be operated accordingly simultaneously with the adsorption column 20 in desorption area 50.The present embodiment effectively increases the speed of lithium extraction
Rate, improves ion-exchanging efficiency, reduces supplement quantity of sorbent, improves the benefit of salt lake resources comprehensive development and utilization, full
The need for sufficient industry development.
Positioned at adsorption zone 30, elute the quantity and each adsorption column 20 of adsorption column 20 in area 40 and desorption area 50 each other
Relation, need to according to the uninterrupted of raw material feed tube 70, elute the uninterrupted of feed tube 80, be desorbed the flow of feed tube 90
Size and absorption, elution and time needed for desorption determine so that in a cycle, the adsorption column 20 in adsorption zone 30
The adsorption column 20 completed in the completion elution operation of adsorption column 20 in adsorption operations, elution area 40, desorption area 50 completes to be desorbed behaviour
Make.Relation between each adsorption column 20 includes independent, series connection and in parallel.
Further, in order to improve automaticity of the invention, the present embodiment extracts the continuous ion exchange unit of lithium also
Including distributing valve 60, the distributing valve 60 includes round end 62 and fixing end 61, the fixing end 61 and round end 62 of distributing valve 60
The notch 63 of identical quantity is offered, wherein, each notch 63 of round end 62 is connected with corresponding each adsorption column 20, Gu
63 points of multiple notches of fixed end 61 are adsorption zone 30, elution area 40 and desorption area 50, are distributed in the notch 63 and original of adsorption zone 30
Material feed tube 70 is connected, and the notch 63 for being distributed in elution area 40 is connected with elution feed tube 80, is distributed in the notch in desorption area 50
63 connect with desorption feed tube 90.
Material liquid, leacheate and desorption liquid are respectively by fixing end 61 in adsorption zone 30, elution area 40 and desorption area 50
Notch 63 input, then via round end 62 corresponding with the notch 63 in each fixing end 61 notch 63 into adsorption column 20
Conveying.Round end 62 can be moved with the movement of corresponding adsorption column 20, i.e., in initial position, the suction in adsorption zone 30
The absorption notch 63 of round end 62 and the notch 63 in fixing end 61 positioned at adsorption zone 30 that attached column 20 is connected are correspondingly arranged so that former
Feed liquid is input to suction via the absorption notch 63 in fixing end 61 on the notch 63 and corresponding round end 62 of adsorption zone 30
In attached column 20, the elution notch 63 of round end 62 that the adsorption column 20 in elution area 40 is connected is with being located at elution area 40 in fixing end 61
Notch 63 be correspondingly arranged so that leacheate via in fixing end 61 elute area 40 notch 63 and corresponding round end 62
On elution notch 63 be input in adsorption column 20, desorption area 50 in adsorption column 20 connect round end 62 desorption notch 63 with
The notch 63 for being located at desorption area 50 in fixing end 61 is correspondingly arranged so that desorption liquid is via the desorption area 50 in fixing end 61
Desorption notch 63 on notch 63 and corresponding round end 62 is input in adsorption column 20.When the adsorption column 20 positioned at adsorption zone 30
Adsorption saturation, the adsorption column 20 positioned at elution area 40 complete elution operation, and the adsorption column 20 positioned at desorption area 50 completes desorption behaviour
After work, operation pedestal 10 is once operated so that the adsorption column 20 in adsorption zone 30 reaches the absorption in elution area 40, elution area 40
The adsorption column 20 that post 20 is reached in desorption area 50, desorption area 50 reaches adsorption zone 30, and accordingly, round end 62 is also operated,
The absorption notch 63 connected with adsorption column 20 in the adsorption zone 30 before operating also correspondingly turns with the position conversion of adsorption column 20
Move on to elution area 40 and switch to elution notch 63, and it is corresponding with the notch 63 for being located at elution area 40 in fixing end 61 so that drench
Washing lotion elution notch 63 corresponding after being operated by the notch 63 and round end 62 in fixing end 61 positioned at elution area 40 is exported,
The elution notch 63 connected with the adsorption column 20 in the elution area 40 before operating is changed also correspondingly with the position of adsorption column 20
It is transferred to desorption area 50 and switches to desorption notch 63, and it is corresponding with the notch 63 for being located at desorption area 50 in fixing end 61 so that
Desorption liquid is defeated by being located at the desorption notch 63 corresponding to being desorbed after the notch 63 in area 50 and the operating of round end 62 in fixing end 61
Go out, the desorption notch 63 connected with adsorption column 20 in the desorption area 50 before operating is changed also correspondingly with the position of adsorption column 20
It is transferred to adsorption zone 30 and switches to absorption notch 63, and it is corresponding with the notch 63 in fixing end 61 positioned at adsorption zone 30 so that
The absorption notch 63 that adsorption liquid is answered after being operated by the notch 63 and round end 62 in fixing end 61 positioned at adsorption zone 30 is exported,
Carry out absorption, elution and the desorption manipulation of second round.Round end 62 is during operating, the He of notch 63 on round end 62
Notch 63 in fixing end 61 is in shifting to install, now, the outlet of the notch 63 in the clogging fixing end 61 of round end 62, because
This, during switching in the position of adsorption column 20, material liquid, leacheate and desorption liquid will not be from the notches 63 in fixing end 61
Overflow.After second round terminates, operation pedestal 10, round end 62 are run to up to corresponding position again, into the period 3,
Over time, pedestal 10 is run, each periodic duty once, is formd and continuously carried round end 62 as procedure described above
Lithium technique.
Certainly, can be set in the present embodiment has controller, to control the operating for running pedestal 10 and rotary valve.
The present embodiment includes round end 62 and the distributing valve 60 of fixing end 61 by setting so that whole to put forward lithium technique reality
The operation of continuous and automatic is showed, material liquid, leacheate and the desorption liquid conveyed in each cycle into different adsorption columns 20
It can automatically switch, substantially increase the extraction efficiency of lithium, reduce the input of manpower, operator scheme is convenient and swift, reduces
Production cost, is used beneficial to being widely popularized.
In addition, the operation pedestal 10 in the present embodiment includes rotating disk and promotes the driver of turntable rotation (not show in accompanying drawing
Go out), multiple adsorption columns 20 are arranged on rotating disk in a ring.
Adsorption column 20 is set along disk peripheral, around the rotating disk center of circle in 360 ° of distributions, and every three cycles are one cycle, are turned
Disk completes 360 ° of cycle operation successively, returns to home position.The adsorption column 20 being located in each cycle in adsorption zone 30 is passed through
Elution area 40 and desorption area 50 are crossed, adsorption zone 30 is returned to, completes once to adsorb, elute and desorption manipulation.The operating in each cycle
Driven by driver so that rotating disk operates corresponding angle according to the setting in driver, realize adsorption zone 30, elution
Area 40 and the replacement in desorption area 50.
The setting of the present embodiment turntable is more conducive to the switching to being operated in adsorption column 20, and adsorption column 20 is arranged neatly, cut
Change processing efficient quick, further improve the automaticity and operational efficiency of the present embodiment.
It should be noted that being provided with top layer distributor 21 and bottom distributor in each adsorption column 20 in the present embodiment
22, the aperture of distributor is 2~6mm.
Distributor can be such that liquid is uniformly distributed on tower cross section, so as to ensure expeditiously to operate in tower.The present embodiment
In top layer distributor 21 and bottom distributor 22 be close to respectively adsorption column 20 top and bottom set, in top layer distributor 21
Loading area is formed between bottom distributor 22, is aoxidized in a diameter of 3~6mm stones of the underfill of loading area or inertia
Other wear-resistant materials covering bottom such as aluminium ball distributor 22, a diameter of 2~6mm polypropylene pellets are filled at the top of loading area
Or the less material covering top layer distributor 21 of color density, loading area central filler has lithium adsorbent.By its top feed side
Formula and fluid distribution requirements, the aperture of distributor are set as 2~6mm.
Be provided with top layer distributor 21 and bottom distributor 22 in the present embodiment, each adsorption column 20, beneficial to material liquid,
The transmission of leacheate and desorption liquid in adsorption column 20, improves adsorption efficiency, elution efficiency and desorption efficiency.
Lithium technique is put forward present invention also offers one kind, to put forward lithium work using the continuous ion exchange unit of said extracted lithium
Skill, is carried out in accordance with the following steps, after the continuous ion exchange unit for extracting lithium starts, into the operation of period 1, that is, is walked
Rapid S1.In the period 1 so that the adsorption column 20 in adsorption zone 30 carries out adsorption operations, i.e., material liquid is transported into adsorption zone
In adsorption column 20 in 30, the operation of second round is entered after to be adsorbed dose of adsorption saturation.Wherein, the raw material of transferring raw material liquid enters
The road one end of liquid pipe 70 is directly protruding into salt lake or is connected with raw material storage tank, and the material liquid conveyed into adsorption zone 30 is by filtering off
Except the salt lake bittern after silt, it is to avoid infringement of the silt to lithium adsorbent in adsorption column 20.The feed rate of material liquid passes through
The flowmeter control being arranged on feed pipe is 5~20BV/h, and material liquid uses the bottom input from adsorption column 20,
The mode flowed to the top of adsorption column 20, more conducively material liquid connect in adsorption column 20 with adsorbent inside adsorption column 20
Touch, so that adsorption efficiency is improved, while material liquid washes away to adsorbent when can also reduce the bias current and charging in adsorption tower, drop
The breakage of low adsorbent.After adsorption column 20, most of lithium in material liquid is adsorbed post 20 and adsorbed, the original after adsorption treatment
Feed liquid is exported from the top of adsorption column 20, is discharged, can be directly discharged in salt lake.
Operation after the adsorption saturation of adsorption column 20 in period 1, area 30 to be adsorbed into second round is step S2.
Operation pedestal 10 is operated once, and the adsorption zone 30 in step S1, which substitutes to substitute for the elution area 40 eluted in area 40, step S1, is
It is adsorption zone 30 that the desorption area 50 being desorbed in area 50, step S1, which substitutes, and the adsorption column 20 in adsorption zone 30 after replacement is inhaled
Material liquid, i.e., be transported in the adsorption column 20 in the adsorption zone 30 after substituting by attached operation, the suction in elution area 40 after replacement
Attached column 20 carries out elution operation, i.e., material liquid is transported in the adsorption column 20 in the elution area 40 after substituting, to completing to adsorb
The adsorption column 20 of operation carries out elution processing so that remains in the material liquid in adsorption column 20 and is discharged under the flushing of leacheate,
So that the impurity reduced in the final liquid being desorbed out reduces the impurity in the lithium finally extracted, what the leacheate was used
It is that, in order to reduce cost, can be entered for the leacheate used first using intermediate storage tank in light salt brine or running water, the present embodiment
Row is reclaimed, and is again acted as leacheate, is discharged again through the secondary leacheate used, can be directly discharged to salt lake.Above-mentioned elution
Liquid uses the mode that bottom discharge is inputted from the top of adsorption column 20, improves flushing effect of the leacheate in adsorption column 20
Really, the feed rate of leacheate is 2~10BV/h by eluting the control of the flowmeter on feed pipe.
In the second cycle, the elution operation in elution area 40 is completed, and completes the adsorption operations of adsorption zone 30 simultaneously, afterwards
Operation into the period 3 is step S3.Operation pedestal 10 is operated again, then the elution area 40 in step S2 substitutes for desorption
The replacement of desorption area 50 in area 50, step S2 is that the adsorption zone 30 in adsorption zone 30, step S2 substitutes to elute area 40, after replacement
Desorption area 50 in adsorption column 20 carry out desorption manipulation, i.e., by desorption liquid be transported to substitute after be desorbed area 50 in adsorption column
In 20, desorption manipulation refers to the devolatilization that will be adsorbed in adsorbent, to make it into the operation of desorption liquid.In the present embodiment
Desorption liquid use the light salt brine of warm or the running water of warm, the temperature of used desorption liquid is 20~60 DEG C, temperature
The desorption liquid energy of heat accelerates lithium from the desorption on adsorbent, and what above-mentioned desorption liquid was used is also to input bottom from the top of adsorption column 20
The mode of portion's discharge, because adsorbent can shrink in desorption, can be reached to the more preferable punching of adsorbent by way of upper feeding
Brush is acted on, meanwhile, desorption manipulation is by the way of upper feeding, and adsorption operations are by the way of lower charging so that in adsorption tower
Adsorbent keeps certain loosening degree, is conducive to the raising of the adsorption efficiency of adsorption column 20.The desorption liquid of output is integrally carried out
All reclaim, to improve the ultimate output of lithium, then via the operation such as evaporation so that the lithium in desorption liquid is separated out, in order to ensure desorption
Efficiency, the discharging flow for controlling the desorption liquid is 5~15BV/h.The adsorption column 20 in elution area 40 after replacement is eluted
Leacheate, i.e., be transported in the adsorption column 20 in the elution area 40 after substituting, the absorption in adsorption zone 30 after replacement by operation
Post 20 carries out adsorption operations, i.e., be transported to material liquid in the adsorption column 20 in the adsorption zone 30 after substituting.
In the period 3, in the elution operation and desorption area 50 in adsorption operations, elution area 40 in adsorption zone 30
Desorption manipulation is carries out simultaneously, when operations are completed, then the operation for entering the period 4 is step S4.Run pedestal 10
Operate again, the replacement of desorption area 50 in step S3 is that the adsorption zone 30 in adsorption zone 30, step S3 substitutes to elute area 40, is walked
Elution area 40 in rapid S3 substitutes for desorption area 50, same respectively in the adsorption zone 30, elution area 40 and desorption area 50 after replacement
Shi Jinhang adsorption operations, elution operation and desorption manipulation, the adsorption operations, elution operation and desorption manipulation are with step S1, S2
With the adsorption operations in S3, elution operation and desorption manipulation.
Over time, step into the period 5, the period 6, the 7th cycle ... operation pedestal 10 at interval of
A cycle is operated once, and adsorption zone 30, elution area 40 and desorption area 50 accordingly substitute successively, in each cycle, adsorption zone
30th, elution area 40 and desorption area 50 carry out adsorption operations, elution operation and desorption manipulation simultaneously respectively.Between the time in each cycle
Every being set as 5~3h, according to material liquid enter flow quantity, the factors such as flow quantity of entering for entering flow quantity and desorption liquid of leacheate exist
Determined in specific production process.
Lithium technical process is simple for carrying described in the present embodiment, and easy to operate, the usage amount of lithium adsorbent is little, compared to biography
The technique that the lithium of system is extracted significantly reduces production cost, and improves production efficiency, and whole operation process is environment friendly and pollution-free,
It is applied widely, with significant economic benefit.
It should be noted that the present invention will be described rather than limits the invention for above-described embodiment, and this
Art personnel can design alternative embodiment without departing from the scope of the appended claims.In claim
In, any reference symbol between bracket should not be configured to limitations on claims.Word "comprising" is not excluded for depositing
In element or step not listed in the claims.
Claims (9)
1. a kind of continuous ion exchange unit for extracting lithium, it is characterised in that the continuous ion exchange unit bag of the extraction lithium
Operation pedestal (10) and multiple adsorption columns (20) are included, the operation pedestal (10) includes adsorption zone (30), elution area (40) and taken off
Attached area (50), multiple adsorption columns (20) are arranged on the operation pedestal (10), and are distributed in the adsorption zone (30), institute
State in elution area (40) and the desorption area (50) and set,
Adsorption column (20) in the adsorption zone (30) is connected with raw material feed tube (70), the adsorption column in the elution area (40)
(20) connected with elution feed tube (80), the adsorption column (20) in the desorption area (50) is connected with desorption feed tube (90),
The position of adsorption zone (30), elution area (40) and desorption area (50) on the operation pedestal (10) substitutes successively.
2. it is according to claim 1 extract lithium continuous ion exchange unit, it is characterised in that the extraction lithium it is continuous
Ion interchange unit also includes distributing valve (60), and the distributing valve (60) includes round end (62) and fixing end (61), described point
Fixing end (61) and round end (62) with valve (60) offer the notch (63) of identical quantity,
Each notch (63) of the round end (62) is connected with corresponding each adsorption column (20),
Multiple notches (63) of the fixing end (61) are divided into adsorption zone (30), elution area (40) and desorption area (50), are distributed in
The notch (63) of the adsorption zone (30) is connected with raw material feed tube (70), be distributed in the notch (63) of the elution area (40) with
Feed tube (80) connection is eluted, the notch (63) for being distributed in the desorption area (50) is connected with desorption feed tube (90).
3. the continuous ion exchange unit according to claim 1 for extracting lithium, it is characterised in that the operation pedestal (10)
Driver including rotating disk and promotion turntable rotation, multiple adsorption columns (20) are arranged on the rotating disk in a ring.
4. the continuous ion exchange unit according to claim 1 for extracting lithium, it is characterised in that each adsorption column
(20) top layer distributor (21) and bottom distributor (22), the top layer distributor (21) and bottom distribution are provided with
The aperture of device (22) is 2~6mm.
5. the continuous ion exchange unit of the extraction lithium in use Claims 1 to 4 described in any one a kind of puies forward lithium technique,
It is characterised in that it includes following steps：
S1：Period 1：Operation pedestal (10) is divided into adsorption zone (30), elution area (40) and desorption area (50), the adsorption zone
(30) adsorption column (20) in carries out adsorption operations and material liquid is transported to the adsorption column (20) in adsorption zone (30) Nei, waits to inhale
Enter second round after adsorbent adsorption saturation in attached area (30)；
S2：Second round：Run pedestal (10) operating once, the adsorption zone (30) in step S1 substitutes for elution area (40), step
Elution area (40) in rapid S1 substitutes to be desorbed area (50), and it is adsorption zone (30), absorption that the desorption area (50) in step S1, which substitutes,
It is that material liquid is transported to the adsorption column after replacement in adsorption zone (30) that adsorption column (20) in area (30), which carries out adsorption operations,
(20) in, meanwhile, the adsorption column (20) in elution area (40) carries out eluting area after leacheate is transported to replacement by elution operation
(40) in the adsorption column (20) in；
S3：Period 3：Operation pedestal (10) is operated again, and the elution area (40) in step S2 substitutes for desorption area (50), step
Desorption area (50) replacement in rapid S2 is that adsorption zone (30) replacement in adsorption zone (30), step S2 is elution area (40), is desorbed
It is that desorption liquid is transported to the adsorption column after replacement in desorption area (50) that adsorption column (20) in area (50), which carries out desorption manipulation,
(20) in, meanwhile, the adsorption column (20) in elution area (40) carries out eluting area after leacheate is transported to replacement by elution operation
(40) in the adsorption column (20) in, the adsorption column (20) in adsorption zone (30) carries out adsorption operations and material liquid is transported into replacement
In adsorption column (20) afterwards in adsorption zone (30)；
S4：Period 4：Operation pedestal (10) is operated again, and it is adsorption zone (30), step that the desorption area (50) in step S3, which substitutes,
Adsorption zone (30) in rapid S3 substitutes to elute area (40), and elution area (40) replacement in step S3 is desorption area (50), is substituted
Adsorption zone (30), elution area (40) and desorption area (50) interior adsorption column (20) afterwards carries out adsorption operations, elution behaviour simultaneously respectively
Make and desorption manipulation；
S5：At interval of a period run once, adsorption zone (30), elution area (40) and desorption area (50) are successively for operation pedestal (10)
Substitute, also, the adsorption zone (30), the elution area (40) and the desorption area (50) respectively carry out absorption behaviour simultaneously
Make, elution is operated and desorption manipulation.
6. according to claim 5 put forward lithium technique, it is characterised in that the duration in each cycle is 0.5~3h.
7. according to claim 5 put forward lithium technique, it is characterised in that the temperature of the desorption liquid is 20~60 DEG C.
8. according to claim 5 put forward lithium technique, it is characterised in that the feed rate of the material liquid is 5~20BV/h；
The feed rate of the leacheate is 2~10BV/h；The discharging flow of the desorption liquid is 5~15BV/h.
9. according to claim 5 put forward lithium technique, it is characterised in that bottom of the material liquid from the adsorption column (20)
Charging, the leacheate and the desorption liquid are from its top feed of adsorption column (20).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611155382.0A CN107058735B (en) | 2016-12-14 | 2016-12-14 | It is a kind of extract lithium continuous ion exchange unit and propose lithium technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611155382.0A CN107058735B (en) | 2016-12-14 | 2016-12-14 | It is a kind of extract lithium continuous ion exchange unit and propose lithium technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107058735A true CN107058735A (en) | 2017-08-18 |
| CN107058735B CN107058735B (en) | 2019-01-18 |
Family
ID=59619795
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611155382.0A Active CN107058735B (en) | 2016-12-14 | 2016-12-14 | It is a kind of extract lithium continuous ion exchange unit and propose lithium technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107058735B (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109761249A (en) * | 2018-12-07 | 2019-05-17 | 三门峡联利新材料有限公司 | Parse the method and system of lithium in aluminium oxide factory richness lithium adsorbent |
| CN111041201A (en) * | 2019-12-30 | 2020-04-21 | 西安蓝晓科技新材料股份有限公司 | A new method for extracting lithium from salt lake brine |
| CN111197123A (en) * | 2020-01-15 | 2020-05-26 | 西安蓝晓科技新材料股份有限公司 | Novel method for separating lithium and sodium |
| CN112501455A (en) * | 2020-11-30 | 2021-03-16 | 五矿盐湖有限公司 | Method for separating lithium from salt lake raw brine |
| WO2021147573A1 (en) * | 2020-01-23 | 2021-07-29 | 西安蓝晓科技新材料股份有限公司 | New method for extracting metal nickel from laterite nickel ore leaching liquor |
| CN115418479A (en) * | 2022-08-16 | 2022-12-02 | 北京万邦达环保技术股份有限公司 | Novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio |
| CN115433839A (en) * | 2022-10-12 | 2022-12-06 | 广东邦普循环科技有限公司 | Lithium extraction device capable of automatically running in salt lake |
| CN116037222A (en) * | 2023-01-13 | 2023-05-02 | 格尔木藏格锂业有限公司 | Method for extracting lithium by efficient continuous ion exchange |
| CN116474417A (en) * | 2022-09-08 | 2023-07-25 | 礼思(上海)材料科技有限公司 | An experimental device and method for extracting lithium from brine |
| CN118222825A (en) * | 2023-09-28 | 2024-06-21 | 比亚迪股份有限公司 | Lithium extraction system and method |
| WO2025135710A1 (en) * | 2023-12-18 | 2025-06-26 | 포스코홀딩스 주식회사 | Lithium recovery system for recovering lithium from lithium-containing solution |
| WO2025135047A1 (en) * | 2023-12-19 | 2025-06-26 | 国立研究開発法人産業技術総合研究所 | Soluble-ion separation/recovery device and separation/recovery method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101928828A (en) * | 2010-09-25 | 2010-12-29 | 西安蓝晓科技有限公司 | Method for extracting lithium from salt lake brine by adsorption method |
| CN102031368A (en) * | 2010-10-29 | 2011-04-27 | 西安蓝晓科技有限公司 | Continuous ion exchange device and method for extracting lithium from salt lake brine |
| CN201825992U (en) * | 2010-10-29 | 2011-05-11 | 西安蓝晓科技有限公司 | Continuous ion exchange device extracting lithium from salt lake brine |
| CN104310446A (en) * | 2014-10-17 | 2015-01-28 | 江苏久吾高科技股份有限公司 | Process and device for extracting battery grade lithium from brine |
| CN104843819A (en) * | 2015-05-26 | 2015-08-19 | 陕西厚亿节能环保新材料科技有限公司 | Method for continuously treating heavy metal liquid |
| US9222148B2 (en) * | 2010-10-29 | 2015-12-29 | Ceramatec, Inc. | Device and method for recovery or extraction of lithium |
| CN105251436A (en) * | 2015-11-27 | 2016-01-20 | 上海空间电源研究所 | Assembly line system in which service life of lithium ion sieve adsorbents is prolonged and operating method thereof |
-
2016
- 2016-12-14 CN CN201611155382.0A patent/CN107058735B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101928828A (en) * | 2010-09-25 | 2010-12-29 | 西安蓝晓科技有限公司 | Method for extracting lithium from salt lake brine by adsorption method |
| CN102031368A (en) * | 2010-10-29 | 2011-04-27 | 西安蓝晓科技有限公司 | Continuous ion exchange device and method for extracting lithium from salt lake brine |
| CN201825992U (en) * | 2010-10-29 | 2011-05-11 | 西安蓝晓科技有限公司 | Continuous ion exchange device extracting lithium from salt lake brine |
| US9222148B2 (en) * | 2010-10-29 | 2015-12-29 | Ceramatec, Inc. | Device and method for recovery or extraction of lithium |
| CN104310446A (en) * | 2014-10-17 | 2015-01-28 | 江苏久吾高科技股份有限公司 | Process and device for extracting battery grade lithium from brine |
| CN104843819A (en) * | 2015-05-26 | 2015-08-19 | 陕西厚亿节能环保新材料科技有限公司 | Method for continuously treating heavy metal liquid |
| CN105251436A (en) * | 2015-11-27 | 2016-01-20 | 上海空间电源研究所 | Assembly line system in which service life of lithium ion sieve adsorbents is prolonged and operating method thereof |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109761249A (en) * | 2018-12-07 | 2019-05-17 | 三门峡联利新材料有限公司 | Parse the method and system of lithium in aluminium oxide factory richness lithium adsorbent |
| CN109761249B (en) * | 2018-12-07 | 2021-07-27 | 开曼铝业（三门峡）有限公司 | Method and system for resolving lithium in lithium-rich adsorbent of alumina plant |
| CN111041201A (en) * | 2019-12-30 | 2020-04-21 | 西安蓝晓科技新材料股份有限公司 | A new method for extracting lithium from salt lake brine |
| WO2021135946A1 (en) * | 2019-12-30 | 2021-07-08 | 西安蓝晓科技新材料股份有限公司 | New method for extracting lithium from salt lake brine |
| CN111197123A (en) * | 2020-01-15 | 2020-05-26 | 西安蓝晓科技新材料股份有限公司 | Novel method for separating lithium and sodium |
| WO2021147573A1 (en) * | 2020-01-23 | 2021-07-29 | 西安蓝晓科技新材料股份有限公司 | New method for extracting metal nickel from laterite nickel ore leaching liquor |
| CN112501455A (en) * | 2020-11-30 | 2021-03-16 | 五矿盐湖有限公司 | Method for separating lithium from salt lake raw brine |
| CN115418479B (en) * | 2022-08-16 | 2023-11-10 | 北京万邦达环保技术股份有限公司 | Novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio |
| CN115418479A (en) * | 2022-08-16 | 2022-12-02 | 北京万邦达环保技术股份有限公司 | Novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio |
| CN116474417A (en) * | 2022-09-08 | 2023-07-25 | 礼思(上海)材料科技有限公司 | An experimental device and method for extracting lithium from brine |
| CN115433839A (en) * | 2022-10-12 | 2022-12-06 | 广东邦普循环科技有限公司 | Lithium extraction device capable of automatically running in salt lake |
| CN115433839B (en) * | 2022-10-12 | 2023-11-03 | 广东邦普循环科技有限公司 | Lithium extraction device for self-running salt lake |
| CN116037222A (en) * | 2023-01-13 | 2023-05-02 | 格尔木藏格锂业有限公司 | Method for extracting lithium by efficient continuous ion exchange |
| CN118222825A (en) * | 2023-09-28 | 2024-06-21 | 比亚迪股份有限公司 | Lithium extraction system and method |
| WO2025066818A1 (en) * | 2023-09-28 | 2025-04-03 | 比亚迪股份有限公司 | Lithium extraction system and lithium extraction method |
| CN118222825B (en) * | 2023-09-28 | 2025-04-08 | 比亚迪股份有限公司 | Lithium extraction system and method |
| WO2025135710A1 (en) * | 2023-12-18 | 2025-06-26 | 포스코홀딩스 주식회사 | Lithium recovery system for recovering lithium from lithium-containing solution |
| WO2025135047A1 (en) * | 2023-12-19 | 2025-06-26 | 国立研究開発法人産業技術総合研究所 | Soluble-ion separation/recovery device and separation/recovery method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107058735B (en) | 2019-01-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107058735A (en) | It is a kind of extract lithium continuous ion exchange unit and put forward lithium technique | |
| WO2021135946A1 (en) | New method for extracting lithium from salt lake brine | |
| CN111729350B (en) | Equipment for extracting lithium from brine by adsorption method | |
| US20230017362A1 (en) | New lithium-sodium separation method | |
| CN101870506B (en) | Process for recovering rare earth from rare earth mining wastewater by resin adsorption method | |
| CN102031368A (en) | Continuous ion exchange device and method for extracting lithium from salt lake brine | |
| CN105251436A (en) | Assembly line system in which service life of lithium ion sieve adsorbents is prolonged and operating method thereof | |
| CN111825152B (en) | Belt filter and application thereof in adsorption method brine lithium extraction | |
| CN201825992U (en) | Continuous ion exchange device extracting lithium from salt lake brine | |
| CN105797428A (en) | Device and method for removing impurities in high-lithium solution | |
| CN101962713A (en) | Continuous ion exchange device and method for extracting gallium from Bayer mother solution | |
| CN104843819B (en) | A kind of method of continuous processing heavy metal liquid | |
| WO2025066818A1 (en) | Lithium extraction system and lithium extraction method | |
| CN101811688A (en) | Device and process method for recovering phosphorus from waste water by struvite precipitation method | |
| CN103482656A (en) | Method for beneficiation of potassium from salt lake brine | |
| CN102863054B (en) | Device for classification recycling of ion exchange resins and process thereof | |
| CN213739613U (en) | W-shaped fixed bed leaching device | |
| CN114752785B (en) | Application of inorganic adsorbent and continuous fluid separation combined process in brine lithium extraction | |
| CN105836766A (en) | Method for removing boron ions in high lithium solution | |
| CN201825993U (en) | Continuous ion exchange device for extracting gallium in Bayer mother liquid | |
| CN213357700U (en) | Continuous ion exchange device for chromatographic separation and gallium extraction of aluminum chloride solution | |
| CN204690088U (en) | Granular lithium ion sieve adsorbant carries the device of lithium | |
| CN203508043U (en) | Ion exchange unit | |
| CN208213199U (en) | A kind of multicolumn series connection automatic control ion interchange unit | |
| CN105461542A (en) | Technology for producing nickel acetate through ion exchange method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |