CN106276987A - The method for concentration of lithium leachate - Google Patents
The method for concentration of lithium leachate Download PDFInfo
- Publication number
- CN106276987A CN106276987A CN201610634839.XA CN201610634839A CN106276987A CN 106276987 A CN106276987 A CN 106276987A CN 201610634839 A CN201610634839 A CN 201610634839A CN 106276987 A CN106276987 A CN 106276987A
- Authority
- CN
- China
- Prior art keywords
- filter
- concentration
- lithium leachate
- filter plant
- 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
- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 152
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 151
- 238000000034 method Methods 0.000 title claims abstract description 81
- 238000001914 filtration Methods 0.000 claims abstract description 74
- 239000007788 liquid Substances 0.000 claims abstract description 49
- 239000000463 material Substances 0.000 claims abstract description 30
- 239000012141 concentrate Substances 0.000 claims abstract description 27
- 238000001556 precipitation Methods 0.000 claims abstract description 12
- 239000000126 substance Substances 0.000 claims abstract description 10
- 239000000203 mixture Substances 0.000 claims abstract description 7
- 239000000706 filtrate Substances 0.000 claims description 78
- 239000003513 alkali Substances 0.000 claims description 48
- 239000002245 particle Substances 0.000 claims description 16
- 238000010992 reflux Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 10
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000012535 impurity Substances 0.000 abstract description 29
- 239000000047 product Substances 0.000 abstract description 20
- 239000012467 final product Substances 0.000 abstract 1
- 239000012528 membrane Substances 0.000 description 22
- 230000000694 effects Effects 0.000 description 14
- 238000001471 micro-filtration Methods 0.000 description 12
- 229910003002 lithium salt Inorganic materials 0.000 description 11
- 159000000002 lithium salts Chemical group 0.000 description 11
- 238000004519 manufacturing process Methods 0.000 description 11
- 230000015572 biosynthetic process Effects 0.000 description 8
- 238000001816 cooling Methods 0.000 description 8
- 239000007787 solid Substances 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 description 5
- 229910052808 lithium carbonate Inorganic materials 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 230000004907 flux Effects 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 229910021642 ultra pure water Inorganic materials 0.000 description 4
- 239000012498 ultrapure water Substances 0.000 description 4
- 239000012530 fluid Substances 0.000 description 3
- 230000008719 thickening Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- 241001131796 Botaurus stellaris Species 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- YZSKZXUDGLALTQ-UHFFFAOYSA-N [Li][C] Chemical group [Li][C] YZSKZXUDGLALTQ-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 230000001052 transient effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D15/00—Lithium compounds
- C01D15/08—Carbonates; Bicarbonates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
-
- 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
-
- 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
- C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
-
- 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
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
-
- 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
Abstract
The invention discloses the method for concentration of a kind of lithium leachate, described lithium leachate refers to that the weight/mass percentage composition of soluble-salt therein content >=60000mg/L and water-insoluble is not less than the liquid of 0.1%, the method step includes: 1) concentration process: filter described lithium leachate, obtains concentrating lithium leachate；The described soluble-salt content >=130000mg/L concentrated in lithium leachate；2) dedoping step: make Si, Al, the Ca in described concentration lithium leachate by chemical method2+、Mg2+It is converted into precipitation, after filtering out described precipitation, i.e. obtains the first concentrated solution.Traditional technique be first carry out remove impurity after concentrate again, but impurity content in final product is high, and product quality is low.The application uses the technique of remove impurity after first the concentrating of novelty, first stop some precipitation and the colloidal substances removed in lithium leachate before remove impurity in concentration process, it is to avoid these materials affects dedoping step, make remove impurity more thoroughly, and the quality of product is higher.
Description
Technical field
The present invention relates to lithium production field, be specifically related to the method for concentration of a kind of lithium leachate.
Background technology
Lithium is a kind of important strategic resources material, is the indispensable important source material of modern high technology product.Carbonic acid
Lithium is to produce secondary lithium salts and the basic material of lithium metal goods, thus becomes the lithium product that in lithium industry, consumption is maximum, its
His lithium product is all the downstream product of lithium carbonate on it.The production technology of lithium carbonate can be divided into according to the difference of raw material sources
Salt lake bittern extracts and Ore extracts.Extracting the with a long history of lithium resource from Ore, technology is the most ripe, main production
Having lime sinter process and sulfuric acid process, wherein sulfuric acid process is currently used topmost method.Current sulfuric acid process step
As follows: the fine grinding of lithium Ore, roasting, acidleach, remove impurity, filtration, evaporation and concentration, sinker, separating, washing, be dried.The applicant grinds
Study carefully discovery, above-mentioned technique have the disadvantage in that one be due to remove impurity after system temperature higher, this make in filter process filter
The service life of medium is shorter；Two be filter link filtering accuracy relatively low, after filtration, in lithium leachate, impurity content is higher,
Cause subsequent product quality relatively low；Three be at evaporation and concentration link duration, thickening efficiency is low, power consumption is high, cause producing lithium
Cost is greatly increased.
Summary of the invention
The technical problem to be solved is to provide the method for concentration of the excellent lithium leachate of a kind of concentrated effect.
In order to solve above-mentioned problem of the prior art, the present invention realizes by the following technical solutions:
The method for concentration of the first lithium leachate of the present invention, described lithium leachate refer to soluble-salt content therein >=
The weight/mass percentage composition of 60000mg/L and water-insoluble is not less than the liquid of 0.1%, and the method step includes: 1) dedoping step:
Si, Al, the Ca in described lithium leachate is made by chemical method2+、Mg2+It is converted into precipitation, i.e. obtains after filtering out described precipitation
First concentrated solution；2) temperature-fall period: the temperature of described first concentrated solution is down to 25-40 DEG C；3) concentration process: after cooling
First concentrated solution filters, and obtains concentrating lithium leachate；The described soluble-salt content concentrated in lithium leachate >=
130000mg/L.Traditional technique be by remove impurity after lithium leachate be passed directly into follow-up filter plant, long-time with higher
The life-span of filter medium can be significantly shortened in the lithium leachate contact of temperature, causes frequently stopping to change filter medium, therefore,
Dedoping step and concentration process increase temperature-fall period, the service life of the filter medium of subsequent filter equipment can be extended, carry
Rise production efficiency, energy-conserving and environment-protective.
Further, described temperature-fall period uses heat exchanger.Heat exchanger can use dividing wall type heat exchanger of the prior art
Or the heat exchanger of other structures.Described dividing wall type heat exchanger is that two kinds of fluids that temperature is different flow in by the separate space of wall
Dynamic, heat conduction and fluid by wall carry out heat exchange between wall surface convection current, two kinds of fluids.Dividing wall type heat exchanger has shell
The heat exchanger of formula, bushing type and other patterns.Further, the type of cooling of described temperature-fall period is water-cooled, air-cooled or vaporize cold
But.Concrete which kind of type of cooling of employing, can select according to the particularity of enterprise, such as, when selecting water-cooled, cooling is situated between
Matter is water and can be recycled.
Further, it is provided with the 4th valve at the first concentrated solution liquid outlet liquid outlet of described heat exchanger.When cooling being detected
After the temperature of the first concentrated solution not in 25-40 DEG C time, then close valve, in time being down within 25-40 DEG C, be then turned on the 4th
Valve.
Further, described dedoping step comprises the following steps: the pH value 1) regulating described lithium leachate is 9-10, obtains
One alkali liquor；2) described first alkali liquor is filtered, obtain the second alkali liquor；3) it is 12-13 by the pH regulator of described second alkali liquor,
It is subsequently adding sodium carbonate, obtains the 3rd alkali liquor；4) described 3rd alkali liquor is filtered, obtain the first concentrated solution.Described step
1) and 2) Si and Al in lithium leachate can be removed, described step 3) and 4) Ca in lithium leachate can be removed2+And Mg2+。
After remove impurity, in gained the first concentrated solution, not only impurity content substantially reduces, and the hardness of concentrated solution significantly reduces, permissible
Slow down formation incrustation scale in follow-up pipeline and equipment, thus reduce pipeline and plant maintenance cycle, increase the service life, promote
Production efficiency.
Further, described dedoping step is carried out in the range of the system temperature of 80-95 DEG C.Si, Al, Ca under the conditions of this2+、
Mg2+The conversion ratio being converted into precipitation is high, can remove the impurity in lithium leachate, the quality of improving product more up hill and dale.
Further, the described filtration being carried out the first alkali liquor includes that making the first alkali liquor pass sequentially through filtration particle diameter is 0.1-
5th filter plant of 100 μm and the 6th filter plant of interception rate >=95% to molecular weight >=1000 material；Described to
The filtration that three alkali liquor are carried out includes making the 3rd alkali liquor by filtering the 7th filter plant that particle diameter is 0.1-100 μm.By
Filtering and the molecular weight screening of the second filter plant of one filter plant, is possible not only to remove Si and Al, it is also possible to remove
Deposit and colloidal substance, make Ca in follow-up remove impurity operation2+And Mg2+The conversion ratio being converted into deposit is higher.
Further, described concentration process comprises the following steps: 1) by the first concentrated solution after described cooling by filtering grain
Footpath is the first filter plant of 0.1-50 μm, and wherein, the first concentrated solution after described cooling is through the filtration of the first filter plant
The first filtrate is formed after medium；2) by first filtrate the second mistake by interception rate >=99.5% to molecular weight >=1000 material
Filter equipment, wherein, described first filtrate forms the second filtrate after the filter medium of the second filter plant；3) by the second filtrate
By the 3rd filter plant to interception rate >=90% that molecular weight is 100-1000 material, wherein, described second filtrate is by
The filter medium of three filter plants is formed after stopping and concentrates lithium leachate, forms the after the filter medium of the 3rd filter plant
Three filtrates, the output of the 3rd filtrate keeps being not less than 8L/ (m2·h).First under the filtration of the first filter plant, grain is removed
Footpath more than the solid matter of the larger particles of 0.1-50 μm, such as some deposits.Increased before the first filter plant filters
Add coarse filtration operating unit, filter out the large-sized solid particulate matter in liquid, it is to avoid these solid particulate matters confrontation the first filtration
In equipment, filter medium causes mechanical damage.Screened the material of molecular weight >=1000 by the molecular weight of the second filter plant
(such as some colloidal substances) remove and obtain the solution that purity is higher.Second filtrate is energy under the operation condition of the 3rd filter plant
Enough realization salt content is that 60000mg/L is concentrated into 130000mg/L and can also concentrate further, finally gives concentration lithium and leaches
Liquid, does not haves in concentration process and concentrates situation about stagnating.
Further, described concentration process also includes step 4): the 3rd filtrate is passed through the interception to molecular weight≤100 material
4th filter plant of rate >=99.99%, wherein, described 3rd filtrate is formed after being stopped by the filter medium of the 4th filter plant
Second concentrated solution, forms the 4th filtrate after the filter medium of the 4th filter plant, and the 4th concentrated solution is back to the 3rd filtration
Device repeats steps 3).4th filtrate is the pure water that purity is higher, typically up to the purity of ultra-pure water.4th concentrated solution backflow
Step 3 is repeated to the 3rd filter plant) lithium in the second concentrated solution can be reclaimed further, it is to avoid the loss of lithium resource.
Further, described 3rd filter plant includes the defecator that at least two is sequentially connected, and each defecator is to dividing
Son amount is interception rate >=90% of 100-1000 material and keeps the output of the 3rd filtrate to be not less than 8L/ (m2·h).Upper
Under the conditions of stating, two defecators are incremented by the most successively through the soluble-salt content of the concentrated solution of filter medium obstruction formation,
And keep the output of the 3rd filtrate, thereby guarantee that concentrated effect.The defecator quantity increasing by the 3rd filter plant is permissible
Effectively realize the renewal of filtration flux, be more favorable for the concentration of the second filtrate, it is achieved high salinity is contained the multistage concentration of mixture solution,
Here multistage concentration can be able to be open, semi open model to use multiple combination mode.
Further, described 3rd filter plant is made up of two defecators being sequentially connected, and two defecators are stopped
The soluble-salt content concentrating lithium leachate of rear formation is followed successively by 130000mg/L, 180000mg/L.With this understanding, remove impurity
After lithium leachate concentrated effect best, products obtained therefrom performance optimal.
Further, the filtration temperature of described concentration process remains between 5 DEG C-40 DEG C.Under this temperature conditions, more
Add the filtration of applicable lithium leachate, concentration.
Further, described 3rd filter plant includes first level filtering device, the two-stage filter being sequentially connected, described two
Level defecator is provided with the concentrated solution outlet discharged for concentrated solution, and therefore in the 3rd filter plant, two-stage filter concentrates resistance
Cut the concentrated solution formed to flow directly out.
Further, described 3rd filter plant includes first level filtering device, the two-stage filter being sequentially connected, described two
Level defecator is provided with the concentrated solution liquid outlet for concentrating the discharge of lithium leachate and is back to one-level for concentrating lithium leachate
The concentrated solution refluxing opening of defecator, described concentrated solution refluxing opening is connected with the inlet of first level filtering device, and cascade filtration fills
The concentrated solution refluxing opening put is provided with the first valve, and the concentrated solution liquid outlet of two-stage filter is provided with the second valve.3rd filters
Two-stage filter in equipment concentrates the concentration lithium leachate of obstruction formation and returns to its inlet and a upper defecator outflow
Concentrated solution converge and be again introduced into last defecator, be then exhausted from after reaching to concentrate salt content, thus improve lithium leachate
Thickening efficiency.
Further, the 3rd filtrate liquid outlet of described 3rd filter plant is provided with the 3rd valve, described 4th filter plant
Concentrated solution liquid outlet and the inlet of the 3rd filter plant between be provided with for second concentrated solution store pans.These pans
The second concentrated solution can be stored, stablize the second concentrated solution pressure and the second concentrated solution is diverted to other operation link.
The method for concentration of the second lithium leachate of the present invention, described lithium leachate refer to soluble-salt content therein >=
The weight/mass percentage composition of 60000mg/L and water-insoluble is not less than the liquid of 0.1%, and the method step includes: 1) concentration process:
Described lithium leachate is filtered, obtains concentrating lithium leachate；The described soluble-salt content concentrated in lithium leachate >=
130000mg/L；2) dedoping step: make Si, Al, the Ca in described concentration lithium leachate by chemical method2+、Mg2+It is converted into
Precipitation, i.e. obtains the first concentrated solution after filtering out described precipitation.Traditional technique be first carry out remove impurity after concentrate again, but
The final impurity in product is (such as Si, Al, Ca2+、Mg2+) content height, product quality is low.The application uses the elder generation of novelty dense
The technique of remove impurity after contracting, first stopped some precipitation and the colloid substances removed in lithium leachate before remove impurity in concentration process
Matter, it is to avoid these materials affect dedoping step, makes remove impurity more thorough, and the quality of product is higher.
Further, described dedoping step comprises the following steps: the pH value 1) regulating described concentration lithium leachate is 9-10,
To the first alkali liquor；2) described first alkali liquor is filtered, obtain the second alkali liquor；3) by the pH regulator of described second alkali liquor it is
12-13, is subsequently adding sodium carbonate, obtains the 3rd alkali liquor；4) described 3rd alkali liquor is filtered, obtain the first concentrated solution.Institute
State step 1) and 2) Si and Al concentrated in lithium leachate, described step 3 can be removed) and 4) concentration lithium leachate can be removed
In Ca2+And Mg2+.After remove impurity, in gained the first concentrated solution, not only impurity content substantially reduces, and the hardness of concentrated solution
Significantly reduce, formation incrustation scale in follow-up pipeline and equipment can be slowed down, thus reduce pipeline and plant maintenance cycle, extend
Service life, improving production efficiency.
Further, described dedoping step is carried out in the range of the system temperature of 80-95 DEG C.Si, Al, Ca under the conditions of this2+、
Mg2+The conversion ratio being converted into precipitation is high, can remove the impurity in lithium leachate, the quality of improving product more up hill and dale.
Further, the described filtration being carried out the first alkali liquor includes that making the first alkali liquor pass sequentially through filtration particle diameter is 0.1-
5th filter plant of 100 μm and the 6th filter plant of interception rate >=95% to molecular weight >=1000 material；Described to
The filtration that three alkali liquor are carried out includes making the 3rd alkali liquor by filtering the 7th filter plant that particle diameter is 0.1-100 μm；7th mistake
It is provided with the 6th valve at first concentrated solution liquid outlet of filter equipment.Filtering and the second filter plant by the first filter plant
Molecular weight screens, and is possible not only to remove Si and Al, it is also possible to remove some deposits and colloidal substance, make follow-up remove impurity operate
Middle Ca2+And Mg2+The conversion ratio being converted into deposit is higher.
Further, the first concentrated solution liquid outlet and second collection device of described 7th filter plant is connected.Described second
Collection device is the first concentrated solution storage device or sinker device, and the first concentrated solution can temporarily store, it is also possible to directly
Flow to follow-up dedoping step.
Further, described concentration process comprises the following steps: 1) by described lithium leachate by filter particle diameter be 0.1-50 μ
First filter plant of m, wherein, described lithium leachate forms the first filtrate after the filter medium of the first filter plant；2)
By first filtrate the second filter plant by interception rate >=99.5% to molecular weight >=1000 material, wherein, described first
Filtrate forms the second filtrate after the filter medium of the second filter plant；3) by the second filtrate by being 100-to molecular weight
3rd filter plant of interception rate >=90% of 1000 materials, wherein, described second filtrate is situated between by the filtration of the 3rd filter plant
Matter is formed after stopping and concentrates lithium leachate, forms the 3rd filtrate after the filter medium of the 3rd filter plant, the 3rd filtrate
Output keeps being not less than 8L/ (m2·h).First under the filtration of the first filter plant, particle diameter is removed more than 0.1-50 μm relatively
Oarse-grained solid matter, such as some deposits.Before the first filter plant filters, increase coarse filtration operating unit, filter
Fall the large-sized solid particulate matter in liquid, it is to avoid these solid particulate matters filter medium in the first filter plant of verifying causes machine
Tool damages.Screened by the molecular weight of the second filter plant and the material (such as some colloidal substances) of molecular weight >=1000 is removed
Obtain the solution that purity is higher.Second filtrate is capable of under the operation condition of the 3rd filter plant
60000mg/L is concentrated into 130000mg/L and can also concentrate further, finally gives concentration lithium leachate, will not in concentration process
Occur concentrating situation about stagnating.
Further, described concentration process also includes step 4): the 3rd filtrate is passed through the interception to molecular weight≤100 material
4th filter plant of rate >=99.99%, wherein, described 3rd filtrate is formed after being stopped by the filter medium of the 4th filter plant
Second concentrated solution, forms the 4th filtrate after the filter medium of the 4th filter plant, and the 4th concentrated solution is back to the 3rd filtration
Device repeats steps 3).4th filtrate is the pure water that purity is higher, typically up to the purity of ultra-pure water.4th concentrated solution backflow
Step 3 is repeated to the 3rd filter plant) lithium in the second concentrated solution can be reclaimed further, it is to avoid the loss of lithium resource.
Further, described 3rd filter plant includes the defecator that at least two is sequentially connected, and each defecator is to dividing
Son amount is interception rate >=90% of 100-1000 material and keeps the output of the 3rd filtrate to be not less than 8L/ (m2·h).Upper
Under the conditions of stating, two defecators are incremented by the most successively through the soluble-salt content of the concentrated solution of filter medium obstruction formation,
And keep the output of the 3rd filtrate, thereby guarantee that concentrated effect.The defecator quantity increasing by the 3rd filter plant is permissible
Effectively realize the renewal of filtration flux, be more favorable for the concentration of the second filtrate, it is achieved high salinity is contained the multistage concentration of mixture solution,
Here multistage concentration can be able to be open, semi open model to use multiple combination mode.
Further, described 3rd filter plant is made up of two defecators being sequentially connected, and two defecators are stopped
The soluble-salt content concentrating lithium leachate of rear formation is followed successively by 130000mg/L, 180000mg/L.With this understanding, remove impurity
After lithium leachate concentrated effect best, products obtained therefrom performance optimal.
Further, the filtration temperature of described concentration process remains between 5 DEG C-40 DEG C.Under this temperature conditions, more
Add the filtration of applicable lithium leachate, concentration.
Further, described 3rd filter plant includes first level filtering device, the two-stage filter being sequentially connected, described two
Level defecator is provided with the concentrated solution outlet discharged for concentrated solution, and therefore in the 3rd filter plant, two-stage filter concentrates resistance
Cut the concentrated solution formed to flow directly out.
Further, described 3rd filter plant includes first level filtering device, the two-stage filter being sequentially connected, described two
Level defecator is provided with the concentrated solution liquid outlet for concentrating the discharge of lithium leachate and is back to one-level for concentrating lithium leachate
The concentrated solution refluxing opening of defecator, described concentrated solution refluxing opening is connected with the inlet of first level filtering device, and cascade filtration fills
The concentrated solution refluxing opening put is provided with the first valve, and the concentrated solution liquid outlet of two-stage filter is provided with the second valve.3rd filters
Two-stage filter in equipment concentrates the concentration lithium leachate of obstruction formation and returns to its inlet and a upper defecator outflow
Concentrated solution converge and be again introduced into last defecator, be then exhausted from after reaching to concentrate salt content, thus improve lithium leachate
Thickening efficiency.
Further, the 3rd filtrate liquid outlet of described 3rd filter plant is provided with the 3rd valve, described 4th filter plant
Concentrated solution liquid outlet and the inlet of the 3rd filter plant between be provided with for second concentrated solution store pans.These pans
The second concentrated solution can be stored, stablize the second concentrated solution pressure and the second concentrated solution is diverted to other operation link.
Further, the concentration lithium leachate liquid outlet of described 3rd filter plant is connected with the first collection device, and described first
The liquid outlet of collection device is provided with the 5th valve, and described first collection device is for concentrating lithium leachate storage device or sinker dress
Putting, concentrating lithium leachate can temporarily store, it is also possible to flow directly into follow-up dedoping step.
By said method, lithium leachate being carried out concentration, concentrated effect is excellent, it is possible to realizes high lithium salts and divides solution
Concentration, after concentration, the lithium leachate purity of gained is high, the highest for the lithium carbonate product quality of subsequent production gained,
Processing procedure can be run under relatively low energy consumption, and production cost is low, good in economic efficiency.
Below by way of accompanying drawing and detailed description of the invention, the invention will be further described.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 1.
Fig. 2 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 2.
Fig. 3 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 3.
Fig. 4 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 4.
Fig. 5 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 5.
Fig. 6 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 6.
Fig. 7 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 7.
Fig. 8 is the schematic flow sheet of the method for concentration of the lithium leachate of embodiment 8.
Detailed description of the invention
Below by way of the method for concentration of lithium leachate of the present invention, the invention will be further described, and described lithium leachate is carbon
Lithium leachate after finely ground, the roasting of lithium Ore, acidleach in acid lithium production process, the solubility lithium in described lithium leachate
The weight/mass percentage composition of salt content >=60000mg/L and water-insoluble is not less than 0.1%.
Embodiment 1
As it is shown in figure 1, the method for concentration of the lithium leachate of the present embodiment comprises the following steps:
Dedoping step: 1) under the effect of power set pump 110, make lithium leachate enter the first container 11, hold first
In device 11, described lithium leachate being warming up to 80-95 DEG C, then regulation pH is 9-10, is sufficiently stirred for i.e. obtaining the first alkali liquor；
2) make the first alkali liquor pass sequentially through filter particle diameter be 0.1-100 μm the 5th filter plant 5 and to molecular weight >=
6th filter plant 6 of interception rate >=95% of 1000 materials, the filter medium of the 5th filter plant 5 is micro-filtration membrane, the 6th mistake
The filter medium of filter equipment 6 is ultrafilter membrane, under twice interception function of described micro-filtration membrane and ultrafilter membrane, and the Si in the first alkali liquor
With Al by effectively catching, finally give the second alkali liquor；
3) in second container 22, pH regulator by described second alkali liquor is 12-13, is subsequently adding sodium carbonate, is sufficiently stirred for
I.e. obtain the 3rd alkali liquor；
4) make the 3rd alkali liquor by filtering the 7th filter plant 7 that particle diameter is 0.1-100 μm, the mistake of the 7th filter plant 7
Filter medium is micro-filtration membrane, the Ca in the 3rd alkali liquor2+、Mg2+Being retained by described micro-filtration membrane, the 3rd alkali liquor obtains through described micro-filtration membrane
To the first concentrated solution；
Whole dedoping step is carried out under the system temperature of 80-95 DEG C.
Temperature-fall period: utilize heat exchanger 8 that the temperature of the first concentrated solution is down to 25-40 DEG C, wherein, cooling medium is circulation
Water, is provided with the 4th valve 800 at the first concentrated solution liquid outlet of heat exchanger..
Concentration process: 1) the first concentrated solution after cooling first passes around plate-and-frame filtration device and carries out coarse filtration, filters out big
Grain solid impurity, then by the first concentrated solution after coarse filtration by filtering the first filter plant 1 that particle diameter is 0.1-50 μm, first
The filter medium that filter plant 1 uses is micro-filtration membrane；
2) the first filtrate formed through the first filter plant 1 after flow to the interception rate of molecular weight >=1000 material >=
Second filter plant 2 of 99.5%, the second filter plant 2 uses ultrafilter membrane as filter medium, and the first filtrate passes the second mistake
The filter medium of filter equipment 2 forms the second filtrate；
3) by the second filtrate by the 3rd filter plant 3 to interception rate >=90% that molecular weight is 100-1000 material,
Wherein, described second filtrate is formed after being stopped by the filter medium of the 3rd filter plant 3 and concentrates lithium leachate, filters through the 3rd
Forming the 3rd filtrate after the filter medium of equipment 3, wherein, the filter medium of the 3rd filter plant 3 is NF membrane, the 3rd filtrate
Output is maintained at and is not less than 8L/ (m2·h)；The concentration lithium leachate liquid outlet of described 3rd filter plant is connected with the first collection
Device 9, described first collection device 9 is for concentrating lithium leachate storage device or sinker device, and concentrating lithium leachate can be temporary transient
Store, it is also possible to flow directly into follow-up sinker device and carry out sinker operation.
Whole process temperature controls device and controls in first filter plant the 1, second filter plant the 2, the 3rd filter plant 3
Filtration temperature remain at 40 DEG C.First filter plant 1 and the second filter plant 2 use end-filtration mode or cross-flow
Filter mode.
You need to add is that, concentration process can periodically be turned off the 3rd filtrate liquid outlet of the 3rd filter plant 3
3rd valve 300, then inputs clear water in the 3rd filter plant 3, and clear water enters the 3rd filtration with the flow velocity of 1.5-3m/s and sets
Standby 3, it may be preferred to clear water flow velocity is 2.5-3m/s, is passed through 24-64h continuously, it is possible to play routine cleaning filter plant, protect
The effect of card filter plant filtration flux.
Embodiment 2
As in figure 2 it is shown, the method for concentration of the lithium leachate of the present embodiment is with the difference of embodiment 1: described dense
Compression process also includes step 4): the 3rd filtrate is passed through the 4th filtration of interception rate >=99.99% to molecular weight≤100 material
Equipment 4, wherein, described 3rd filtrate forms the second concentrated solution, through the 4th after being stopped by the filter medium of the 4th filter plant 4
Forming the 4th filtrate after the filter medium of filter plant 4, the 4th filter plant 4 is stopped the second concentrated solution formed and is back to the 3rd
Filter plant 3 repeats step 3), wherein, the filter medium of the 4th filter plant 4 is reverse osmosis membrane；4th filter plant 4 flows out
The 4th filtrate be ultra-pure water, be used directly for after collection produce other link.Described 3rd filtrate liquid outlet is provided with
3rd valve, is provided with between concentrated solution liquid outlet and the inlet of the 3rd filter plant 3 of described 4th filter plant 4 for concentrating
The pans 10 that lithium leachate stores.With this understanding, the lithium leachate concentrated effect after remove impurity is best, and products obtained therefrom quality is
Good.
Embodiment 3
As it is shown on figure 3, the method for concentration of the lithium leachate of the present embodiment is with the difference of embodiment 2: described
Three filter plants are made up of two defecators being sequentially connected, and what two defecators were formed after stopping concentrates lithium leachate
Soluble lithium salt content is followed successively by 130000mg/L, 180000mg/L.First level filtering device 31 and the of two-stage filter 32
Three filtrate liquid outlets converge and are connected with the inlet of the 4th filter plant 4.
Embodiment 4
As shown in Figure 4, the method for concentration of the lithium leachate of the present embodiment is with the difference of embodiment 2: this enforcement
The 3rd filter plant 3 in example is semi open model structure, and i.e. from the 3rd filter plant 3, two-stage filter 32 is isolated dense
Contracting lithium leachate returns to the inlet of first level filtering device 31 and again concentrates, and flows out after lithium salt content reaches 180000mg/L.
3rd filter plant includes first level filtering device 31 and the two-stage filter 32 being sequentially connected, and two-stage filter 32 is provided with
Concentrate lithium leachate liquid outlet and concentrate lithium salts leachate refluxing opening, concentrating lithium leachate refluxing opening and be provided with the first valve 321
And connect with the inlet of first level filtering device 31, concentrate lithium leachate liquid outlet and be provided with the second valve 322.Single filter fills
Put 31 converge with the 3rd filtrate liquid outlet of two-stage filter 32 and be connected with the inlet of the 4th filter plant 4.Two mistakes
The soluble lithium salt content concentrating lithium leachate that filter device is formed after stopping is followed successively by 130000mg/L, 180000mg/L.Tool
Gymnastics opens the first valve 321 as line, closes the second valve 322, and the lithium salt content of lithium leachate to be concentrated reaches
Close the first valve 321 after 180000mg/L, open the second valve 322 so that concentrate lithium leachate and discharge and collect, the 3rd
Filtrate enters the 4th filter plant.With this understanding, the present embodiment leaches compared to the lithium of embodiment 1, embodiment 2, embodiment 3
The concentrated effect of liquid is more preferable, and concentration process is more stable, the highest for the lithium carbonate product quality of subsequent production gained.
Embodiment 5
As it is shown in figure 5, the method for concentration of the lithium leachate of the present embodiment comprises the following steps:
Concentration process: 1) under the effect of power set pump 110, lithium leachate first passes around plate-and-frame filtration device to be carried out slightly
Filter, filters out bulky grain solid impurity, then by the lithium leachate after coarse filtration by filtering the first mistake that particle diameter is 0.1-50 μm
Filter equipment 1, the filter medium that the first filter plant 1 uses is micro-filtration membrane；
2) the first filtrate formed through the first filter plant 1 after flow to the interception rate of molecular weight >=1000 material >=
Second filter plant 2 of 99.5%, the second filter plant 2 uses ultrafilter membrane as filter medium, and the first filtrate passes the second mistake
The filter medium of filter equipment 2 forms the second filtrate；
3) by the second filtrate by the 3rd filter plant 3 to interception rate >=90% that molecular weight is 100-1000 material,
Wherein, described second filtrate is formed after being stopped by the filter medium of the 3rd filter plant 3 and concentrates lithium leachate, filters through the 3rd
Forming the 3rd filtrate after the filter medium of equipment 3, wherein, the filter medium of the 3rd filter plant 3 is NF membrane, the 3rd filtrate
Output is maintained at and is not less than 8L/ (m2·h)；The concentration lithium leachate liquid outlet of described 3rd filter plant 3 is connected with the first receipts
Acquisition means 9, the liquid outlet of described first collection device 9 is provided with the 5th valve 900, and described first collection device 9 is for concentrating lithium leaching
Going out liquid storage device or sinker device, concentrating lithium leachate can temporarily store, it is also possible to flow directly into follow-up remove impurity
Operation.
Dedoping step: 1) in the first container 11, described concentration lithium leachate is warming up to 80-95 DEG C, then regulation pH is
9-10, is sufficiently stirred for i.e. obtaining the first alkali liquor；
2) make the first alkali liquor pass sequentially through filter particle diameter be 0.1-100 μm the 5th filter plant 5 and to molecular weight >=
6th filter plant 6 of interception rate >=95% of 1000 materials, the filter medium of the 5th filter plant 5 is micro-filtration membrane, the 6th mistake
The filter medium of filter equipment 6 is ultrafilter membrane, under twice interception function of described micro-filtration membrane and ultrafilter membrane, and the Si in the first alkali liquor
With Al by effectively catching, finally give the second alkali liquor；
3) in second container 22, pH regulator by described second alkali liquor is 12-13, is subsequently adding sodium carbonate, is sufficiently stirred for
I.e. obtain the 3rd alkali liquor；
4) make the 3rd alkali liquor by filtering the 7th filter plant 7 that particle diameter is 0.1-100 μm, the mistake of the 7th filter plant 7
Filter medium is micro-filtration membrane, the Ca in the 3rd alkali liquor2+、Mg2+Being retained by described micro-filtration membrane, the 3rd alkali liquor obtains through described micro-filtration membrane
To the first concentrated solution；First concentrated solution liquid outlet of described 7th filter plant 7 connects the second collection device 11, and described second
Collection device 11 is storage device or the sinker device of the first concentrated solution, and the first concentrated solution can temporarily store, it is also possible to
Flow directly into follow-up operation.
Whole dedoping step is carried out under the system temperature of 80-95 DEG C.
Whole process temperature controls device and controls in first filter plant the 1, second filter plant the 2, the 3rd filter plant 3
Filtration temperature remain at 40 DEG C.First filter plant 1 and the second filter plant 2 use end-filtration mode or cross-flow
Filter mode.
You need to add is that, concentration process can periodically be turned off the 3rd filtrate liquid outlet of the 3rd filter plant 3
3rd valve 300, then inputs clear water in the 3rd filter plant 3, and clear water enters the 3rd filtration with the flow velocity of 1.5-3m/s and sets
Standby 3, it may be preferred to clear water flow velocity is 2.5-3m/s, is passed through 24-64h continuously, it is possible to play routine cleaning filter plant, protect
The effect of card filter plant filtration flux.
Embodiment 6
As shown in Figure 6, the method for concentration of the lithium leachate of the present embodiment is with the difference of embodiment 5: described dense
Compression process also includes step 4): the 3rd filtrate is passed through the 4th filtration of interception rate >=99.99% to molecular weight≤100 material
Equipment 4, wherein, described 3rd filtrate forms the second concentrated solution, through the 4th after being stopped by the filter medium of the 4th filter plant 4
Forming the 4th filtrate after the filter medium of filter plant 4, the 4th filter plant 4 is stopped the second concentrated solution formed and is back to the 3rd
Filter plant 3 repeats step 3), wherein, the filter medium of the 4th filter plant 4 is reverse osmosis membrane；4th filter plant 4 flows out
The 4th filtrate be ultra-pure water, be used directly for after collection produce other link.Described 3rd filtrate liquid outlet is provided with
3rd valve 300, is provided with confession between concentrated solution liquid outlet and the inlet of the 3rd filter plant 3 of described 4th filter plant 4
Concentrate the pans 10 that lithium leachate stores.With this understanding, the lithium leachate concentrated effect after remove impurity is best, products obtained therefrom product
Matter is optimal.
Embodiment 7
As it is shown in fig. 7, the method for concentration of the lithium leachate of the present embodiment is with the difference of embodiment 6: described
Three filter plants 3 are made up of two defecators being sequentially connected, the concentration lithium leachate that two defecators are formed after stopping
Soluble lithium salt content be followed successively by 130000mg/L, 180000mg/L.First level filtering device 31 and two-stage filter 32
3rd filtrate liquid outlet converges and is connected with the inlet of the 4th filter plant 4.
Embodiment 8
As shown in Figure 8, the method for concentration of the lithium leachate of the present embodiment is with the difference of embodiment 6: this enforcement
The 3rd filter plant 3 in example is semi open model structure, and i.e. from the 3rd filter plant 3, two-stage filter 32 is isolated dense
Contracting lithium leachate returns to the inlet of first level filtering device 31 and again concentrates, and flows out after lithium salt content reaches 180000mg/L.
3rd filter plant 3 includes first level filtering device 31 and the two-stage filter 32 being sequentially connected, and two-stage filter 32 sets
There is concentration lithium leachate liquid outlet and concentrate lithium leachate refluxing opening, concentrating lithium leachate refluxing opening and be provided with the first valve 321
And connect with the inlet of first level filtering device 31, concentrate lithium leachate liquid outlet and be provided with the second valve 322.Single filter fills
Put 31 converge with the 3rd filtrate liquid outlet of two-stage filter 32 and be connected with the inlet of the 4th filter plant 4.Two mistakes
The soluble lithium salt content concentrating lithium leachate that filter device is formed after stopping is followed successively by 130000mg/L, 180000mg/L.Tool
Gymnastics opens the first valve 321 as line, closes the second valve 322, and the lithium salt content of lithium leachate to be concentrated reaches
Close the first valve 321 after 180000mg/L, open the second valve 322 so that concentrate lithium leachate and discharge and collect, the 3rd
Filtrate enters the 4th filter plant 4.With this understanding, the present embodiment soaks compared to the lithium of embodiment 5, embodiment 6, embodiment 7
The concentrated effect going out liquid is more preferable, and concentration process is more stable, the highest for the lithium carbonate product quality of subsequent production gained.
Claims (10)
1. the method for concentration of lithium leachate, described lithium leachate refers to soluble-salt therein content >=60000mg/L and water not
The weight/mass percentage composition of molten thing is not less than the liquid of 0.1%, it is characterised in that the method step includes:
1) concentration process: filter described lithium leachate, obtains concentrating lithium leachate；
The described soluble-salt content >=130000mg/L concentrated in lithium leachate；
2) dedoping step: make Si, Al, the Ca in described concentration lithium leachate by chemical method2+、Mg2+It is converted into precipitation, filters
The first concentrated solution is i.e. obtained after falling described precipitation.
2. the method for concentration of lithium leachate as claimed in claim 1, it is characterised in that described concentration process includes following step
Rapid:
1) by described lithium leachate by filtering the first filter plant (1) that particle diameter is 0.1-50 μm, wherein, described lithium leachate
The first filtrate is formed after the filter medium of the first filter plant (1)；
2) by first filtrate the second filter plant (2) by interception rate >=99.5% to molecular weight >=1000 material, wherein,
Described first filtrate forms the second filtrate after the filter medium of the second filter plant (2)；
3) by the second filtrate by the 3rd filter plant (3) to interception rate >=90% that molecular weight is 100-1000 material, its
In, described second filtrate is formed after being stopped by the filter medium of the 3rd filter plant (3) and concentrates lithium leachate, filters through the 3rd
The 3rd filtrate is formed after the filter medium of equipment (3)；
The output of described 3rd filtrate keeps being not less than 8L/ (m2·h)。
3. the method for concentration of lithium leachate as claimed in claim 2, it is characterised in that described concentration process also includes step
4): the 3rd filtrate is passed through the 4th filter plant (4) of interception rate >=99.99% to molecular weight≤100 material, wherein, institute
State after the 3rd filtrate is stopped by the filter medium of the 4th filter plant (4) and form the second concentrated solution, through the 4th filter plant (4)
Filter medium after formed the 4th filtrate, the 4th concentrated solution be back to the 3rd filter plant (3) repeat step 4).
4. the method for concentration of lithium leachate as claimed in claim 2 or claim 3, it is characterised in that: described 3rd filter plant (3) bag
Including the defecator that at least two is sequentially connected, each defecator is to interception rate >=90% that molecular weight is 100-1000 material also
And keep the 3rd filtrate output be not less than 8L/ (m2·h)。
5. the method for concentration of lithium leachate as claimed in claim 4, it is characterised in that described 3rd filter plant (3) includes
The first level filtering device (31) that is sequentially connected, two-stage filter (32), described two-stage filter (32) is provided with for concentrating
The concentrated solution liquid outlet of lithium leachate discharge and confession concentration lithium leachate are back to the concentrated solution of first level filtering device (31) and return
Head piece, described concentrated solution refluxing opening is connected with the inlet of first level filtering device (31), the concentrated solution of two-stage filter (32)
Refluxing opening is provided with the first valve (321), and the concentrated solution liquid outlet of two-stage filter (32) is provided with the second valve (322).
6. the method for concentration of lithium leachate as claimed in claim 2 or claim 3, it is characterised in that: described 3rd filter plant (3)
Concentrated solution liquid outlet and the first collection device (9) are connected, and are provided with the 5th valve at the liquid outlet of described first collection device (9)
(900)。
7. the method for concentration of lithium leachate as claimed in claim 1, it is characterised in that described dedoping step includes following step
Rapid:
1) pH value regulating described concentration lithium leachate is 9-10, obtains the first alkali liquor；
2) described first alkali liquor is filtered, obtain the second alkali liquor；
3) pH regulator by described second alkali liquor is 12-13, is subsequently adding sodium carbonate, obtains the 3rd alkali liquor；
4) described 3rd alkali liquor is filtered, obtain the first concentrated solution.
8. the method for concentration of lithium leachate as claimed in claim 7, it is characterised in that described dedoping step is at 80-95 DEG C
Carry out in the range of system temperature.
9. the method for concentration of lithium leachate as claimed in claim 7, it is characterised in that: the described mistake that first alkali liquor is carried out
It is the 5th filter plant (5) of 0.1-100 μm and to molecular weight >=1000 that filter includes making the first alkali liquor to pass sequentially through filtration particle diameter
6th filter plant (6) of interception rate >=95% of material；The described filtration being carried out the 3rd alkali liquor includes making the 3rd alkali liquor
By filtering the 7th filter plant (7) that particle diameter is 0.1-100 μm；At first concentrated solution liquid outlet of the 7th filter plant (7)
It is provided with the 6th valve (700).
10. the method for concentration of lithium leachate as claimed in claim 9, it is characterised in that: the of described 7th filter plant (7)
One concentrated solution liquid outlet and the second collection device (11) are connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610634839.XA CN106276987B (en) | 2016-08-05 | 2016-08-05 | The method for concentration of lithium leachate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610634839.XA CN106276987B (en) | 2016-08-05 | 2016-08-05 | The method for concentration of lithium leachate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106276987A true CN106276987A (en) | 2017-01-04 |
| CN106276987B CN106276987B (en) | 2018-07-06 |
Family
ID=57665162
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610634839.XA Active CN106276987B (en) | 2016-08-05 | 2016-08-05 | The method for concentration of lithium leachate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106276987B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1542147A (en) * | 2003-04-30 | 2004-11-03 | 中国科学院青海盐湖研究所 | Nano-filtration method for separating magnesium and enriching lithium from salt lake brine |
| CN102659144A (en) * | 2012-04-26 | 2012-09-12 | 雅安华汇锂业科技材料有限公司 | Method for preparing high purity level lithium hydroxide monohydrate |
| CN102923743A (en) * | 2012-11-19 | 2013-02-13 | 河北工程大学 | Technical method for comprehensively extracting aluminum and lithium from coal ash through acid process |
| CN103074502A (en) * | 2013-01-29 | 2013-05-01 | 中国科学院青海盐湖研究所 | Salt lake brine treatment method for separating lithium from high-magnesium-lithium-ratio salt lake brine |
| WO2013146391A1 (en) * | 2012-03-30 | 2013-10-03 | 東レ株式会社 | Method for separation and recovery of alkali metal and alkali metal separation and recovery apparatus |
| CN103738984A (en) * | 2013-12-26 | 2014-04-23 | 江苏久吾高科技股份有限公司 | Method and device for extracting bitten lithium chloride |
| CN104313321A (en) * | 2014-11-17 | 2015-01-28 | 赣州有色冶金研究所 | Impurity removal method and system for lepidolite leaching solution |
| CN204569443U (en) * | 2015-04-14 | 2015-08-19 | 中国海洋石油总公司 | The device that bromine bittern produces refined brine is carried in a kind of utilization |
-
2016
- 2016-08-05 CN CN201610634839.XA patent/CN106276987B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1542147A (en) * | 2003-04-30 | 2004-11-03 | 中国科学院青海盐湖研究所 | Nano-filtration method for separating magnesium and enriching lithium from salt lake brine |
| WO2013146391A1 (en) * | 2012-03-30 | 2013-10-03 | 東レ株式会社 | Method for separation and recovery of alkali metal and alkali metal separation and recovery apparatus |
| CN102659144A (en) * | 2012-04-26 | 2012-09-12 | 雅安华汇锂业科技材料有限公司 | Method for preparing high purity level lithium hydroxide monohydrate |
| CN102923743A (en) * | 2012-11-19 | 2013-02-13 | 河北工程大学 | Technical method for comprehensively extracting aluminum and lithium from coal ash through acid process |
| CN103074502A (en) * | 2013-01-29 | 2013-05-01 | 中国科学院青海盐湖研究所 | Salt lake brine treatment method for separating lithium from high-magnesium-lithium-ratio salt lake brine |
| CN103738984A (en) * | 2013-12-26 | 2014-04-23 | 江苏久吾高科技股份有限公司 | Method and device for extracting bitten lithium chloride |
| CN104313321A (en) * | 2014-11-17 | 2015-01-28 | 赣州有色冶金研究所 | Impurity removal method and system for lepidolite leaching solution |
| CN204569443U (en) * | 2015-04-14 | 2015-08-19 | 中国海洋石油总公司 | The device that bromine bittern produces refined brine is carried in a kind of utilization |
Non-Patent Citations (3)
| Title |
|---|
| 张仁志: "《环境综合实验》", 30 April 2015, 中国环境出版社 * |
| 胡洪波等: "《生物工程单元操作实验》", 31 March 2014, 上海交通大学出版社 * |
| 邢红等: "膜法盐湖卤水提锂工艺研究", 《盐业与化工》 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106276987B (en) | 2018-07-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107837557B (en) | The continuous crystallizing system and its technique of a kind of coarse granule, low water-insoluble cobaltous sulfate | |
| CN210001701U (en) | system for treating mine water with high suspended matter and high mineralization degree | |
| CN109179715A (en) | The circulating filtration recyclable device and technique of titanium dioxide granule in wastewater from TiO2 factory | |
| CN112919717A (en) | Intelligent desalting system for mine water | |
| US20170182460A1 (en) | Silica products from geothermal fluids by reverse osmosis | |
| JP2018524256A (en) | Method for producing silica concentrate | |
| CN106282557A (en) | The method for concentration of lithium leachate | |
| TW201235090A (en) | Abrasive recovery method and abrasive recovery device | |
| CN205803020U (en) | A kind of system of Production By Sulfuric Acid Process lithium salts | |
| CN106145487A (en) | A kind of technique processing rare-earth trade high-concentration ammonia nitrogenous wastewater reuse | |
| JP7128546B2 (en) | Method and system for preparing lithium carbonate from lithium ore | |
| CN208617612U (en) | Evaporative crystallization unit equipment for high-salt wastewater processing system | |
| CN101987765A (en) | Sewage treatment method and system used by same | |
| CN106276987A (en) | The method for concentration of lithium leachate | |
| CN105439347B (en) | A kind of mother liquor treatment process and system for the concentration of clopyralid feed separation | |
| CN207986914U (en) | A kind of washes zero-discharge treatment system | |
| CN108793557B (en) | Desulfurization wastewater bypass flue evaporation treatment process and system | |
| CN218435031U (en) | Metal surface treatment liquid recycling system | |
| JP2018512354A (en) | Method for producing colloidal silica concentrate | |
| CN105925800B (en) | The method and apparatus for concentrating lithium leachate | |
| CN205627649U (en) | Lithium production is with intermetallic compound porous material membrane crossflow filtration enrichment facility | |
| CN215828549U (en) | Intelligent zero-emission system for mine water | |
| CN201762103U (en) | Separating system for inorganic acid and inorganic acid salt in waste acid | |
| CN209481353U (en) | MVR vapo(u)rization system arranges dense structure | |
| CN105925801B (en) | Concentrate method of the high salinity containing mixture solution and its application in lithium leachate is handled |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Concentration method for lithium leaching liquid Effective date of registration: 20200708 Granted publication date: 20180706 Pledgee: Chengdu SME financing Company Limited by Guarantee Pledgor: SICHUAN SIDANENG ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Registration number: Y2020980003915 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20220119 Granted publication date: 20180706 Pledgee: Chengdu SME financing Company Limited by Guarantee Pledgor: SICHUAN SIDANENG ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Registration number: Y2020980003915 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Concentration method of lithium leaching solution Effective date of registration: 20220317 Granted publication date: 20180706 Pledgee: Chengdu SME financing Company Limited by Guarantee Pledgor: SICHUAN SIDANENG ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Registration number: Y2022510000066 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20230106 Granted publication date: 20180706 Pledgee: Chengdu SME financing Company Limited by Guarantee Pledgor: SICHUAN SIDANENG ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Registration number: Y2022510000066 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Concentration method of lithium leaching solution Effective date of registration: 20230215 Granted publication date: 20180706 Pledgee: Chengdu SME financing Company Limited by Guarantee Pledgor: SICHUAN SIDANENG ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd. Registration number: Y2023980032391 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |