CN115418479B - Novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio - Google Patents
Novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio Download PDFInfo
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- 229910052744 lithium Inorganic materials 0.000 title claims abstract description 86
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 title claims abstract description 85
- 239000012267 brine Substances 0.000 title claims abstract description 75
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 75
- 238000000034 method Methods 0.000 title claims abstract description 62
- 230000008569 process Effects 0.000 title claims abstract description 43
- GCICAPWZNUIIDV-UHFFFAOYSA-N lithium magnesium Chemical compound [Li].[Mg] GCICAPWZNUIIDV-UHFFFAOYSA-N 0.000 title claims abstract description 27
- 238000001179 sorption measurement Methods 0.000 claims abstract description 323
- 239000000945 filler Substances 0.000 claims abstract description 138
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims abstract description 102
- 239000010936 titanium Substances 0.000 claims abstract description 102
- 229910052719 titanium Inorganic materials 0.000 claims abstract description 102
- 238000002386 leaching Methods 0.000 claims abstract description 82
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 77
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 77
- 239000007788 liquid Substances 0.000 claims abstract description 65
- 239000000243 solution Substances 0.000 claims abstract description 59
- 238000005406 washing Methods 0.000 claims abstract description 44
- 238000003795 desorption Methods 0.000 claims abstract description 17
- 239000003480 eluent Substances 0.000 claims abstract description 15
- 238000000605 extraction Methods 0.000 claims abstract description 14
- 238000002156 mixing Methods 0.000 claims abstract description 7
- 239000000203 mixture Substances 0.000 claims abstract description 3
- 230000001105 regulatory effect Effects 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 56
- 239000003795 chemical substances by application Substances 0.000 description 37
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 24
- 238000012856 packing Methods 0.000 description 23
- 229910001416 lithium ion Inorganic materials 0.000 description 22
- 239000011777 magnesium Substances 0.000 description 12
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 10
- 239000003463 adsorbent Substances 0.000 description 10
- 229910052749 magnesium Inorganic materials 0.000 description 10
- 238000010521 absorption reaction Methods 0.000 description 8
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 8
- 230000008901 benefit Effects 0.000 description 8
- 238000011282 treatment Methods 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 7
- 239000002253 acid Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000002336 sorption--desorption measurement Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- LCKIEQZJEYYRIY-UHFFFAOYSA-N Titanium ion Chemical group [Ti+4] LCKIEQZJEYYRIY-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 229910052792 caesium Inorganic materials 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 description 1
- 229910052808 lithium carbonate Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 229910052701 rubidium Inorganic materials 0.000 description 1
- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-UHFFFAOYSA-N 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 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
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet 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
- C22B3/24—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition by adsorption on solid substances, e.g. by extraction with solid resins
-
- 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 belongs to the technical field of extracting lithium from salt lake brine, and discloses a novel process for extracting lithium from salt lake brine with a high magnesium-lithium ratio. The salt lake brine sequentially passes through a titanium filler adsorption column group and an aluminum filler adsorption column group which are connected in series; the adsorption columns in the adsorption column group are alternately used as the head columns, and the adsorption columns which are already used as the head columns to participate in adsorption enter a leaching stage; the titanium filler adsorption column which is used as the head column to participate in adsorption is connected in series for leaching, resolving and washing; the aluminum filler adsorption column which is used as the head column to participate in adsorption is leached in parallel and analyzed in series, and the analysis liquid of the titanium filler adsorption column and the analysis liquid of the aluminum filler adsorption column are mixed to form qualified lithium-containing extraction liquid. Or, introducing salt lake brine into an aluminum filler adsorption column group, eluting and resolving the aluminum filler adsorption column to obtain eluent and resolving liquid; mixing the leaching solution and the desorption solution, and introducing the mixture into a titanium filler adsorption column group; eluting, resolving and washing the titanium filler adsorption column to obtain the resolved liquid which is qualified lithium-containing extracting liquid.
Description
Technical Field
The invention belongs to the technical field of extracting lithium from salt lake brine, and particularly relates to a novel process for extracting lithium from salt lake brine with a high magnesium-lithium ratio.
Background
Salt lake brine is a valuable inorganic salt resource, and besides being rich in potassium, sodium, magnesium and boron, the reserves of high-value rare elements such as lithium, rubidium and cesium are also large. The development and utilization of rare elements have important significance for comprehensive utilization and sustainable development of salt lake resources. The lithium and the compound thereof are closely related to the life of people, are applied to various industrial fields, and become important strategic materials for national economy and national defense construction. The ascertained reserve ratio of the Chinese salt lake lithium resource is up to 80.54%, but the magnesium-lithium ratio is high and the separation is difficult. With the deep industry transformation and the enhancement of environmental protection consciousness of the whole people, sustainable, green and comprehensive deep development and utilization of resources have become a necessary trend.
The traditional lithium extraction method mainly comprises a precipitation method, a carbonization method, a solvent extraction method, a calcination method and the like, and the above methods have the problems of large occupied area, high energy consumption and low yield, and are difficult to extract lithium from brine with high magnesium-lithium ratio. Most of the lithium resources in China are stored in salt lake brine, and most of the lithium resources belong to high-magnesium-lithium-ratio brine, so that the extraction of lithium from the high-magnesium-lithium-ratio brine becomes an important point for the development of the lithium resources in China. Adsorption methods developed in recent years are widely favored because of their advantages such as good selectivity for lithium ions and simple process.
Patent document with publication number CN214829053U discloses a salt lake brine adsorption lithium extraction device, comprising: the adsorption tank is filled with titanium adsorbent and is used for adsorbing lithium ions in brine; the first solid-liquid separator is used for separating the adsorbent obtained in the adsorption tank; the analysis column is used for analyzing the adsorbent obtained in the first solid-liquid separator; the first dilute acid adding tank and the second dilute acid adding tank are respectively connected to the resolving column and are used for feeding dilute acid into the resolving column; and the precipitation reactor is connected with the analysis column and is used for carrying out lithium precipitation operation on the analysis liquid obtained in the analysis column. However, the adsorption lithium extraction device is only aimed at high-lithium sodium brine, the titanium filler is required to be in a large amount, the pH value is required to be continuously regulated in the adsorption process, and the cost is high.
Patent document with publication number CN1511964a discloses a method for extracting lithium from salt lake brine by adsorption, which comprises the steps of feeding salt lake brine into an adsorption-desorption device containing aluminum salt adsorbent for adsorption-desorption; wherein the aluminum salt type adsorbent in the adsorption-desorption device adsorbs lithium in the salt lake brine, and then the eluent is used for eluting and desorbing lithium ions; (2) And (3) refining the eluent to prepare qualified lithium-rich brine required by lithium carbonate or lithium chloride. The aluminum adsorbent is independently adopted to treat the salt lake brine, so that the lithium ion adsorption efficiency is low and the production cost is high.
Disclosure of Invention
Aiming at the problems existing in the prior art, the invention aims to provide a novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio.
The term "magnesium-lithium ratio" as used herein refers to the ratio of the concentration of magnesium ions to the concentration of lithium ions in the same concentration unit in the solution.
In order to achieve the above object, the present invention provides the following specific technical solutions.
A novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio comprises the following steps:
the salt lake brine sequentially passes through a titanium filler adsorption column group and an aluminum filler adsorption column group which are connected in series.
Further, in a preferred embodiment of the present invention, the titanium-based filler adsorption column group contains n1 adsorption columns, wherein n 1. Gtoreq.4. It is further preferred that no more than n1-1 adsorption columns are connected in series each time participate in adsorption.
Further, in a preferred embodiment of the present invention, the group of aluminum-based packing adsorption columns contains n2 adsorption columns, wherein n 2. Gtoreq.4. It is further preferred that no more than n2-1 adsorption columns are connected in series each time that participate in adsorption.
Further, in a part of the preferred embodiments of the present invention, the salt lake brine passing through the titanium-based packing adsorption column group is adjusted to an initial value before entering the aluminum-based packing adsorption column.
Further, in some preferred embodiments of the present invention, the adsorption cycle number of the salt lake brine in the titanium-based filler adsorption column group and the aluminum-based filler adsorption column group is at least 2 times, and the adsorption columns in the adsorption column group are alternately used as the head columns, and the adsorption columns which have been used as the head columns to participate in the adsorption enter the leaching stage.
Further, in some preferred embodiments of the present invention, the method further comprises the steps of:
the titanium filler adsorption columns which are used as the head columns to participate in adsorption are connected in series for leaching. The specific leaching process comprises the following steps: and taking pure water at 20 ℃ as a leaching agent, wherein the flow rate is 6-10 BV/h, and when the concentration of lithium ions in the leaching agent is less than 1mg/L, ending leaching.
Further, in some preferred embodiments of the present invention, the method further comprises the steps of:
and the aluminum filler adsorption columns which are used as the head columns to participate in adsorption are connected in parallel for leaching. The specific leaching process comprises the following steps: pure water at 20 ℃ is used as eluent, the flow rate is 15-20 BV/h, and when the concentration ratio of magnesium and lithium in the eluent is less than 12: and 1, ending leaching.
Further, in some preferred embodiments of the present invention, the method further comprises the steps of:
and (3) performing tandem analysis on the eluted titanium packing adsorption column. The specific analysis process comprises the following steps: and (3) taking 0.1-0.2mol/L of dilute hydrochloric acid or dilute sulfuric acid as a resolving agent, wherein the flow rate of the resolving agent is 3-5 BV/h. When the content of lithium ions in the analysis liquid is less than 300ppm, the analysis is finished.
Further, in some preferred embodiments of the present invention, the method further comprises the steps of:
and (3) carrying out tandem analysis on the leached aluminum filler adsorption column. The specific analysis process comprises the following steps: pure water at 50-60 ℃ is used as a resolving agent, and the flow rate is 6-10 BV/h. When the content ratio of magnesium and lithium in the analytic solution is 5:1, the analysis is ended.
Further, in some preferred embodiments of the present invention, the method further comprises the steps of:
the resolved titanium filler adsorption columns are connected in series for water washing. The specific water washing process comprises the following steps: and (3) washing with pure water at 20 ℃ at a flow rate of 6-10 BV/h. When the lithium content in the aqueous washing liquid is less than 1ppm, the aqueous washing is completed.
The resolved aluminum filler adsorption column does not need to be washed by water.
Further, in some preferred embodiments of the present invention, the method further comprises the steps of:
the adsorption tail liquid and the leacheate of the aluminum filler adsorption column group are sent into a brine pool for re-adsorption;
mixing the first 2BV desorption liquids of the titanium filler adsorption column as eluent, and then the desorption liquids of the aluminum filler adsorption column;
the pH value of the water washing liquid of the titanium filler adsorption column is regulated, and the titanium filler adsorption column can be used for the water washing process.
By utilizing the advantage of large adsorption capacity of the titanium filler, the titanium filler fully adsorbs lithium ions in salt lake brine at first and analyzes out a lithium-containing solution with higher concentration. Because the concentration of lithium in the brine is gradually reduced in the adsorption process, the adsorption capacity of the titanium filler adsorbent for low-concentration brine is poor, and the advantage of high adsorption rate of the aluminum filler adsorbent is utilized, the brine adsorbed by the titanium filler is further adsorbed, and the recycling efficiency of lithium is improved.
The inventor creatively discovers that for the titanium packing adsorption column, the series leaching reduces the using amount of the leaching agent; the method has the advantages that the method improves the concentration of lithium in the analysis liquid, reduces the consumption of the analysis agent, saves the cost, shortens the time consumption of the whole process flow and improves the treatment efficiency; for the aluminum filler adsorption column, the parallel leaching is carried out, so that the loss of lithium in the aluminum filler in the leaching process is reduced; the method improves the concentration of lithium in the analysis liquid, reduces the consumption of the analysis agent, saves the cost, shortens the time consumption of the whole process flow and improves the treatment efficiency.
The resolving liquid of the titanium filler adsorption column and the resolving liquid of the aluminum filler adsorption column are mixed, so that the lithium-containing solution with large volume, high concentration and low magnesium-lithium ratio can be obtained, the pH value of the mixed resolving liquid can be increased, the temperature of the mixed resolving liquid can be reduced, and the subsequent membrane concentration process is convenient to carry out.
Based on the same inventive concept, the invention further provides a novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio, which comprises the following steps:
introducing salt lake brine into an aluminum filler adsorption column group, eluting and resolving the aluminum filler adsorption column to obtain eluent and resolving liquid; mixing the leaching solution and the desorption solution, and introducing the mixture into a titanium filler adsorption column group; and leaching and analyzing the titanium filler adsorption column to obtain an analysis solution, namely the qualified lithium-containing extraction solution.
Further, in a part of the preferred embodiments of the present invention, the number of adsorption columns in the group of aluminum-based packing adsorption columns is n3, wherein n3 is not less than 3; the number of the adsorption columns connected in series and participating in adsorption at each time is not more than n 3-1.
Further, in a part of the preferred embodiments of the invention, the salt lake brine is circulated through the aluminum-based filler adsorption column group for a plurality of times until the concentration of lithium ions in the adsorption tail liquid of the aluminum-based filler adsorption column group is more than or equal to 10 mg/L.
Further, in some preferred embodiments of the present invention, the adsorption columns in the group of adsorption columns are alternately taken as the head column, and the adsorption columns which have been taken as the head column to participate in the adsorption enter the rinsing stage.
Further, in some preferred embodiments of the present invention, the aluminum-based packing adsorption columns participating in adsorption as the head column are rinsed in parallel. The specific leaching process comprises the following steps: pure water at 20 ℃ is used as eluent, the flow rate is 15-20 BV/h, and when the concentration ratio of magnesium and lithium in the eluent is less than 12: and 1, ending leaching.
Further, in a part of the preferred embodiments of the present invention, the eluted aluminum-based packing adsorption column is analyzed in series. The specific analysis process comprises the following steps: pure water at 50-60 ℃ is used as a resolving agent, and the flow rate is 6-10 BV/h. When the content ratio of magnesium and lithium in the analytic solution is 5:1, the analysis is ended.
Further, in a part of the preferred embodiments of the present invention, the number of adsorption columns in the titanium-based filler adsorption column group is n4, wherein n4 is not less than 3; the number of the adsorption columns connected in series and participating in adsorption at each time is not more than n 4-1.
Further, in a part of the preferred embodiments of the present invention, the mixed solution of the eluting solution and the resolving solution is circulated through the titanium-based packing adsorption column group for a plurality of times until the concentration of lithium ions in the adsorption tail solution of the titanium-based packing adsorption column group is more than or equal to 200 mg/L.
Further, in some preferred embodiments of the present invention, the adsorption columns in the titanium-based packing adsorption column group are alternately used as the head column, and the adsorption columns which have been used as the head column to participate in the adsorption enter the leaching stage.
Further, in some preferred embodiments of the present invention, the titanium-based packing adsorption column participating in the adsorption as the head column is rinsed in series. The specific leaching process comprises the following steps: and taking pure water at 20 ℃ as a leaching agent, wherein the flow rate is 6-10 BV/h, and when the content of lithium in the leaching agent is less than 1ppm, ending leaching.
Further, in a part of the preferred embodiments of the present invention, the eluted titanium-based packing adsorption column is analyzed in series. The specific analysis process comprises the following steps: and taking 0.1-0.2mol/L of dilute hydrochloric acid or dilute sulfuric acid as a resolving agent, wherein the flow rate is 3-5 BV/h. When the content of lithium ions in the analysis liquid is less than 300ppm, the analysis is finished.
Washing the parsed titanium packing adsorption column with water.
Further, in some preferred embodiments of the present invention, the method further comprises the steps of:
and (3) neutralizing the analytic solutions of the first 2BV of the titanium filler adsorption column by acid and alkali, and returning to the leaching stage, wherein other analytic solutions are qualified lithium-containing extracting solutions.
And (3) all the absorption tail liquid generated in the absorption stage of the titanium filler absorption column is discharged to a brine pool for absorption again.
And (3) after the pH value of the water washing liquid generated in the water washing stage of the titanium filler adsorption column is adjusted, returning to the water washing process.
By utilizing the advantage of high adsorption rate of the aluminum filler adsorption column, salt lake brine firstly passes through the aluminum filler adsorption column and then the lithium-containing solution with higher concentration is resolved. However, the leaching of the aluminum filler adsorption column in the leaching stage is not very sufficient, and after the leaching, the analytic solution has a higher magnesium-lithium ratio, but the lithium concentration in the analytic solution is improved by 4-5 times compared with the original salt lake brine. The titanium filler has poor adsorption capacity to low-lithium-concentration salt lake brine, but has strong adsorption capacity to high-lithium-concentration salt lake brine and large adsorption capacity. By utilizing the advantage of large adsorption capacity of the titanium filler adsorption column, the desorption liquid of the aluminum filler adsorption column is further adsorbed, and then leached and desorbed, so that the high-concentration lithium-containing solution can be obtained.
Compared with the prior art, the invention has the following obvious beneficial effects:
(1) Compared with the method which uses the titanium filler adsorption column group or the aluminum filler adsorption column group singly, the two-stage adsorption units of the titanium filler adsorption column group and the aluminum filler adsorption column group reduce the cost by 30-40%;
(2) The adjustment of the pH value of the absorption tail liquid of the titanium filler absorption column is avoided, and the absorption process is optimized;
(3) The problems that the subsequent flow is affected due to the fact that the temperature of the resolved tail liquid of the aluminum filler adsorption column is too high are avoided;
(4) In the lithium extraction process, no wastewater is discharged basically, and the waste of water resources and the loss of valuable metals are avoided.
Drawings
FIG. 1 is a schematic illustration of the process flow employed in example 1.
Fig. 2 is a schematic process flow diagram of examples 2 to 5.
Detailed Description
The present invention will be described more fully hereinafter with reference to the accompanying drawings, in which preferred embodiments are shown, for the purpose of illustrating the invention, but the scope of the invention is not limited to the specific embodiments shown.
Unless defined otherwise, all technical and scientific terms used hereinafter have the same meaning as commonly understood by one of ordinary skill in the art. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the scope of the present invention.
Unless otherwise specifically indicated, the various raw materials, reagents, instruments, equipment and the like used in the present invention are commercially available or may be prepared by existing methods.
Example 1
Taking brine of a salt lake as a treatment object. A schematic process flow diagram as shown in fig. 1 is employed. It should be noted that: the first 2BV analysis solutions of the titanium-based packing adsorption column are returned to the eluent pool as eluent, which is not shown in the figure.
The content of each metal in the brine of a salt lake is shown in table 1.
TABLE 1 main elements and contents of salt lake brine
(1) Adsorption of
The brine of a certain salt lake firstly passes through a titanium filler adsorption column group, wherein 4 adsorption columns are arranged in the titanium filler adsorption column group, and 3 adsorption columns which are connected in series are arranged in each adsorption. Wherein the titanium filler is titanium ion sieve adsorbent.
The flow rate of the brine of a certain salt lake passing through the titanium-series packing adsorption column group is 6BV/h, and the adsorption is 8BV. And when the lithium concentration of the effluent is less than 500mg/L, the effluent enters an aluminum packing adsorption column group. The number of adsorption columns of the aluminum filler adsorption column group is 4, and 3 adsorption columns connected in series are used for adsorption at each time. The aluminum filler is an aluminum molecular sieve adsorbent.
The pH of the effluent of the titanium filler adsorption column group is 1-1.5, and the pH is adjusted to 4.5-5 before entering the aluminum filler adsorption column.
And judging that the adsorption is finished when the lithium concentration of the aluminum filler adsorption column group liquid reaches below 50 mg/L. And after the primary adsorption process is finished, respectively taking down the head columns of the titanium-based and aluminum-based filler adsorption column groups, respectively taking the column 2 in the titanium-based and aluminum-based filler adsorption column groups as the head column, carrying out the primary adsorption again, and after the adsorption is finished, taking down the head columns of the titanium-based and aluminum-based filler adsorption column groups again, and finishing the adsorption stage.
(2) Rinsing
And (3) eluting the two titanium filler adsorption columns and the two aluminum filler adsorption columns separately. Eluting the titanium filler adsorption columns, connecting the two adsorption columns in series, and eluting the two adsorption columns by using pure water at 20 ℃ as eluent at the flow rate of 6BV/h and 4BV. And when the lithium ion content in the final BV leaching solution is less than 1mg/L, the leaching is finished.
Eluting the aluminum filler adsorption column, cleaning the two reaction columns separately, and eluting 1BV by using pure water at 20 ℃ as an eluting agent at a flow rate of 18 BV/h. The leaching stage is rapid leaching, so that the adsorbed lithium ions are prevented from being leached again. When the magnesium-lithium ratio in the eluent is less than 12: and 1, judging that the leaching is finished.
(3) Resolution
The titanium filler reaction column enters into analysis, the two reaction columns are connected in series, the analysis agent is dilute hydrochloric acid or sulfuric acid with the concentration of 0.1-0.2mol/L, the flow rate is 3BV/h, and the analysis is 5BV. And (3) after the first 2BV of the desorption solution is neutralized by acid and alkali, returning the desorption solution to a leaching agent pool, and obtaining the other desorption solutions which are qualified lithium-containing extraction solutions. And when the concentration content of the effluent lithium is lower than 300ppm, the analysis is completed. The magnesium-lithium ratio of the titanium filler adsorption column desorption solution is 0.2-0.5, and the pH value is 2-2.5.
The aluminum filler adsorption column enters into analysis, two reaction columns are connected in series, the analysis agent is pure water at 50-60 ℃, the flow rate is 6BV/h, and the analysis is 3BV. And when the magnesium-lithium ratio of the analysis liquid is 5:1, judging that the analysis process is finished. The temperature of the analysis liquid is 35-42 ℃.
And mixing the qualified titanium filler adsorption column desorption solution with the aluminum filler adsorption column desorption solution to obtain the lithium-containing extracting solution. The ratio of magnesium to lithium in the lithium-containing extracting solution is 2:1-3:1, the pH value is about 3, and the temperature is 23-25 ℃.
The mixing of the analysis liquids of the two systems can reduce the magnesium-lithium ratio, improve the pH of the analysis liquid of the titanium filler adsorption column, reduce the medicament input for adjusting the pH of the analysis liquid, reduce the temperature of the analysis liquid of the aluminum filler adsorption column, and facilitate the subsequent membrane concentration process.
(4) Washing with water
After the titanium filler adsorption column is resolved, the adsorption column is washed with water. Washing with pure water at 20 ℃ at a flow rate of 6BV/h and 3BV. When the lithium concentration content in the effluent is less than 1ppm, the water washing stage is completed. After the water washing is completed, the whole adsorption and analysis process is completed. The aluminum filler adsorption column is not washed by water.
The adsorption tail liquid generated in the adsorption stage and the leaching liquid generated in the leaching stage are all discharged to a brine pool for re-adsorption; and (3) after acid-base neutralization, the water washing liquid of the titanium filler adsorption column in the water washing stage is completely returned to the water washing process for reuse. The whole adsorption and analysis link has no extra wastewater discharge.
Comparative example 1
A salt lake brine as described in example 1 was used as a treatment target.
The adsorption columns with 8 titanium fillers are circularly adsorbed twice, 7 adsorption columns which are connected in series and participate in adsorption each time are used as the head columns, and the adsorption columns which participate in adsorption do not participate in the adsorption process any more;
the effluent of each adsorption column needs to be adjusted to an initial value;
the flow rate of brine in the adsorption stage is 6BV/h, and the brine is adsorbed by 6BV;
after the adsorption is finished, 2 head columns are connected in series for leaching, resolving and washing;
in the leaching stage, pure water at 20 ℃ is used as a leaching agent, the flow rate of the leaching agent is 6BV/h, and the leaching volume is 4BV;
the resolving agent in resolving stage is dilute hydrochloric acid or sulfuric acid with the concentration of 0.1-0.2mol/L, the flow rate of the resolving agent is 3BV/h, and the resolving volume is 5BV;
the pure water flow rate in the titanium-based water washing stage is 6BV/h, and the water washing volume is 3BV.
The analysis liquid is lithium-containing extraction liquid, and the pH value is 1-2.
Comparative example 2
A salt lake brine as described in example 1 was used as a treatment target.
8 aluminum filler adsorption columns are circularly adsorbed for 2 times, 7 adsorption columns which are connected in series and participate in adsorption each time are used as the head column, and the adsorption columns which participate in adsorption do not participate in the adsorption process any more;
the flow rate of brine in the adsorption stage is 6BV/h, and the adsorption is 8BV;
after the adsorption is finished, 2 head columns are eluted in parallel and analyzed in series;
in the leaching stage, pure water at 20 ℃ is used as a leaching agent, the flow rate of the leaching agent is 18BV/h, and the leaching agent is used for leaching 1BV;
in the analysis stage, pure water at 50-60 ℃ is used as an analysis agent, the flow rate of the analysis agent is 6BV/h, and the analysis volume is 3BV;
the analysis liquid is lithium-containing extraction liquid, the pH is 6-7, and the temperature is 35-42 ℃.
Comparative example 3
Sequentially passing salt lake brine through an aluminum filler adsorption column group and a titanium filler adsorption column group which are connected in series, and circularly adsorbing for 2 times;
4 adsorption columns in the aluminum filler adsorption column group, wherein 3 adsorption columns which participate in adsorption each time are connected in series, and the adsorption column which is used as the head column and participates in adsorption does not participate in adsorption any more;
4 adsorption columns of the titanium filler adsorption column group, 3 adsorption columns which participate in adsorption each time and are connected in series, wherein the adsorption column which is used as the head column to participate in adsorption does not participate in adsorption any more;
the flow rate of brine in the adsorption stage of the aluminum filler adsorption column is 6BV/h, and the adsorption is 8BV;
2 head columns of the aluminum filler adsorption column are eluted in parallel and are analyzed in series without water washing, wherein pure water at 20 ℃ is used as an eluting agent in the eluting stage, the flow rate of the eluting agent is 18BV/h, and the eluting agent is 1BV; in the analysis stage, pure water at 50-60 ℃ is used as an analysis agent, the flow rate of the analysis agent is 6BV/h, and the analysis volume is 3BV;
the flow rate of brine in the adsorption stage of the titanium packing adsorption column is 6BV/h, and the adsorption is 8BV;
2 head columns of the titanium filler adsorption column are connected in series for eluting, resolving and washing, wherein pure water at 20 ℃ is used as an eluting agent in the eluting stage, the flow rate of the eluting agent is 6BV/h, and the eluting volume is 4BV; the resolving agent in resolving stage is 0.1-0.2mol/L dilute hydrochloric acid or sulfuric acid, the flow rate is 3BV/h, and the resolving volume is 3BV; the flow rate of washing water in the washing stage is 6BV/h, and the washing volume is 3BV;
mixing the desorption solution of the titanium filler adsorption column and the aluminum filler adsorption column to obtain the lithium-containing extracting solution, wherein the pH value is 3-3.2, and the temperature is 23-25 ℃.
The amounts of treatments in example 1 and comparative examples 1 to 3 were examined and analyzed, and the results of the detection and analysis are shown in Table 2, such as lithium concentration, magnesium-lithium ratio, pH value, etc., in the finally obtained lithium-containing extract.
TABLE 2
As can be seen from table 2, the technical scheme of adopting the titanium-based and aluminum-based filler adsorption column groups of the present invention to be sequentially connected in series is as follows:
compared with pure titanium filler adsorption columns, the concentration of lithium ions in the lithium-containing extracting solution is reduced, and the magnesium and lithium are higher than the magnesium and lithium ions in the lithium-containing extracting solution, but the pH value of each titanium filler adsorption column does not need to be frequently regulated in the adsorption process, and the obtained lithium-containing extracting solution has large volume and higher pH value, so that the adding cost of the medicament is saved; meanwhile, the treatment capacity is large, the concentration of lithium ions in the system adsorption tail liquid is low, and the adsorption effect on lithium is better.
Compared with an aluminum filler adsorption column group, the lithium-containing extraction liquid has the advantages of higher concentration of lithium ions, low magnesium-lithium ratio and low temperature, and meanwhile, the volume of the obtained lithium-containing extraction liquid is large;
compared with the technical scheme that aluminum-series and titanium-series filler adsorption column groups are sequentially connected in series, the lithium ion adsorption system has the advantages that the concentration of lithium ions in the lithium-containing extracting solution is high, the magnesium-lithium ratio is low, the concentration of lithium ions in the adsorption tail liquid of the system is low, and the adsorption effect on lithium ions is better while the low magnesium-lithium ratio is ensured.
The technical scheme provided by the invention is a scheme with better comprehensive performance by comprehensively considering the concentration of lithium ions, the ratio of magnesium to lithium, the temperature, the pH value and the adsorption effect on lithium in the lithium-containing extracting solution.
Example 2
Taking brine of a salt lake as a treatment object. A schematic process flow diagram as shown in fig. 2 is employed. It should be noted that: the "first 2BV analytical solutions of the titanium-based packing adsorption column are returned to the eluent pool" is not shown in the figure.
The content of each metal in the brine of a salt lake is shown in table 3.
TABLE 3 Main elements and contents (mg/L) of salt lake brine
(1) Adsorption column adsorption of aluminum filler
Contains 126mg/L of Li + Mg/Li 970: the salt lake brine of 1 enters an aluminum filler adsorption column group, wherein the adsorption columns of the aluminum filler adsorption column group are column A, column B and column C3 adsorption columns, and 2 adsorption columns participating in adsorption are connected in series each time. The flow rate of brine is 10BV/h, and the adsorption is 20BV. First, column a and column B are connected in series, and column C does not participate in adsorption. After one round of adsorption is completed, the column A is taken down, the column B and the column C are connected in series, and then one round of adsorption is carried out, so that the adsorption condition is unchanged. After the adsorption is completed, the column B is taken down, and the adsorption stage is completed.
(2) Leaching aluminium filler adsorption column
The column A and the column B are leached separately, the leaching agent is pure water at 20 ℃, the flow rate is 15BV/h, and the leaching volume is 1BV.
(3) Adsorption column for resolving aluminum series packing
After the rinsing stage is completed, column a and column B are serially connected for resolution. The resolving agent is pure water at 50 ℃, the flow rate is 6BV/h, and the resolving volume is 3BV.
After the analysis is completed, the analysis liquid and the leaching liquid are mixed and enter the titanium packing adsorption column group.
(4) Titanium-based filler adsorption column group adsorption
The titanium-based packing adsorption column group comprises 3 adsorption columns: column E, column F, column G. Each time, 2 adsorption columns are connected in series. The flow rate of brine is 12BV/h, and the absorption is 15BV. Firstly, the column E and the column F are connected in series, after the adsorption is finished, the column E is taken down, the column F and the column G are connected in series, and then one round of adsorption is carried out, and the adsorption condition is unchanged. After the adsorption is completed, the column F is taken down, and the adsorption stage is completed.
(5) Eluting titanium-series filler adsorption column group
The column E and the column F are connected in series for leaching, the leaching agent is purified water at 20 ℃, the flow rate is 6BV/h, and the leaching volume is 3BV.
(5) Analysis titanium filler adsorption column group
After the rinsing stage is completed, column E and column F are serially connected for resolution. The resolving agent is hydrochloric acid with the concentration of 0.2mol/L, the flow rate is 3BV/h, and the resolving volume is 5BV. After the analysis is completed, an analysis solution is obtained. The analysis liquid is qualified lithium-containing extraction liquid.
(7) Titanium packing adsorption column group for water washing
Column E and column F were washed in series with water. The flow rate of water is 6BV/h, the leaching volume is 3BV, and the whole adsorption and analysis process is completed after the water washing is completed.
Example 3
Example 3 differs from example 2 only in that:
the flow rate of brine in the aluminum series adsorption stage is 12BV/h, and the adsorption is 20BV;
the flow rate of the leaching solution in the leaching stage of the aluminum system is 12BV/h;
the flow rate of the analysis liquid in the aluminum analysis stage is 6BV/h, and the analysis volume is 3BV;
the flow rate of the mixed solution in the titanium adsorption stage is 15BV/h, and the adsorption is 10BV;
the flow rate of the leaching solution in the titanium leaching stage is 8BV/h, and the leaching volume is 4BV;
the flow rate of the analysis liquid in the titanium analysis stage is 5BV/h, and the analysis volume is 7BV;
the pure water flow rate in the titanium-based water washing stage is 10BV/h, and the water washing volume is 4BV.
Example 4
Example 4 differs from example 2 only in that:
the flow rate of brine in the aluminum series adsorption stage is 15BV/h, and the adsorption is 18BV;
the flow rate of the leaching solution in the leaching stage of the aluminum series is 20BV/h, and the leaching is 1.5BV;
the flow rate of the analysis liquid in the aluminum analysis stage is 10BV/h, and the analysis volume is 5BV;
the flow rate of the mixed solution in the titanium adsorption stage is 15BV/h, and the adsorption is 10BV;
the flow rate of the leaching solution in the titanium leaching stage is 10BV/h, and the leaching volume is 4BV;
the flow rate of the analysis liquid in the titanium analysis stage is 5BV/h, and the analysis volume is 7BV;
the pure water flow rate in the titanium-based water washing stage is 10BV/h, and the water washing volume is 4BV.
Example 5
Example 5 differs from example 2 only in that:
the flow rate of brine in the aluminum series adsorption stage is 15BV/h, and the adsorption is 18BV;
the flow rate of the leaching solution in the leaching stage of the aluminum series is 20BV/h, and the leaching is 1.5BV;
the flow rate of the analysis liquid in the aluminum analysis stage is 10BV/h, and the analysis volume is 5BV;
the flow rate of the mixed solution in the titanium adsorption stage is 12BV/h, and the adsorption is 15BV;
the flow rate of the leaching solution in the titanium leaching stage is 6BV/h, and the leaching volume is 3BV;
the flow rate of the analysis liquid in the titanium analysis stage is 3BV/h, and the analysis volume is 5BV;
the pure water flow rate in the titanium-based water washing stage is 6BV/h, and the water washing volume is 3BV.
The results of the detection and analysis of the concentration of lithium and the ratio of magnesium to lithium in the analytical solution (i.e., the acceptable lithium-containing extract) of the titanium-based filler adsorption column in examples 2 to 5 are shown in Table 4.
TABLE 4 Table 4
As can be seen from Table 4, the solutions described in examples 2 to 5 were employed, and the content of lithium in the desorption solution of the titanium-based filler adsorption column was high and the content of magnesium and lithium was low.
The foregoing is merely a preferred embodiment of the present invention and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present invention, which are intended to be comprehended within the scope of the present invention.
Claims (8)
1. The novel process for extracting lithium from the salt lake brine with high magnesium-lithium ratio is characterized by comprising the following steps of:
the salt lake brine sequentially passes through a titanium filler adsorption column group and an aluminum filler adsorption column group which are connected in series;
before salt lake brine passing through the titanium-series filler adsorption column group enters the aluminum-series filler adsorption column group, regulating the pH value to be 4.5-5;
eluting, resolving and washing the titanium filler adsorption column;
leaching and analyzing the aluminum filler adsorption column;
the adsorption columns in the adsorption column group are alternately used as the head columns, and the adsorption columns which are already used as the head columns to participate in adsorption enter a leaching stage;
the titanium filler adsorption column which is used as the head column to participate in adsorption is connected in series for leaching, resolving and washing;
the aluminum filler adsorption column which is used as the head column to participate in adsorption is leached in parallel and analyzed in series.
2. The novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio as claimed in claim 1, wherein the titanium filler adsorption column group comprises n1 adsorption columns, wherein n1 is more than or equal to 4, and n1-1 adsorption columns which participate in adsorption and are connected in series are not more than one each time; the aluminum filler adsorption column group contains n2 adsorption columns, wherein n2 is more than or equal to 4, and n2-1 adsorption columns which participate in adsorption and are connected in series each time are not more than one.
3. The novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio as claimed in claim 1, wherein the desorption solution of the titanium filler adsorption column and the desorption solution of the aluminum filler adsorption column are mixed to obtain qualified lithium-containing extraction solution.
4. The novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio as claimed in claim 1, wherein the adsorption tail liquid of the aluminum filler adsorption column group, the titanium filler adsorption column and the leaching liquid of the aluminum filler adsorption column are directly discharged into a brine pool for re-adsorption; the washing liquid of the titanium filler adsorption column returns to the washing process.
5. The new process for extracting lithium from salt lake brine with high magnesium-lithium ratio as claimed in claim 4, wherein the first 2BV of the desorption solution of the titanium filler adsorption column is used for leaching.
6. The novel process for extracting lithium from the salt lake brine with high magnesium-lithium ratio is characterized by comprising the following steps of: introducing salt lake brine into an aluminum filler adsorption column group, eluting and resolving the aluminum filler adsorption column to obtain eluent and resolving liquid; mixing the leaching solution and the desorption solution, and introducing the mixture into a titanium filler adsorption column group; eluting, resolving and washing the titanium filler adsorption column to obtain resolving liquid which is qualified lithium-containing extracting liquid; the adsorption columns in the adsorption column group are alternately used as the head columns, and the adsorption columns which are already used as the head columns to participate in adsorption enter a leaching stage; the aluminum filler adsorption column which is used as the head column to participate in adsorption is eluted in parallel and analyzed in series; the titanium filler adsorption column which is used as the head column to participate in the adsorption is connected in series for leaching, resolving and washing.
7. The novel process for extracting lithium from salt lake brine with high magnesium-lithium ratio as claimed in claim 6, wherein the number of adsorption columns in the aluminum filler adsorption column group is n3, wherein n3 is more than or equal to 3, and the number of the aluminum filler adsorption columns which participate in adsorption each time and are connected in series is not more than n 3-1; the number of the adsorption columns in the titanium filler adsorption column group is n4, wherein n4 is more than or equal to 3, and the number of the titanium filler adsorption columns which participate in adsorption each time and are connected in series is not more than n 4-1.
8. The new process for extracting lithium from salt lake brine with high magnesium-lithium ratio as claimed in claim 6 or 7, wherein the adsorption tail liquid of the aluminum filler adsorption column group and the leaching liquid of the titanium filler adsorption column are discharged to a brine pool for re-adsorption; the first 2BV analytical solutions of the titanium filler adsorption column are used for leaching, and the washing solution of the titanium filler adsorption column returns to the washing process.
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Citations (8)
| 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 |
| CN107021513A (en) * | 2017-04-17 | 2017-08-08 | 四川大学 | The method that lithium is extracted from salt lake bittern |
| CN107058735A (en) * | 2016-12-14 | 2017-08-18 | 青海盐湖工业股份有限公司 | It is a kind of extract lithium continuous ion exchange unit and put forward lithium technique |
| CN108298570A (en) * | 2017-12-28 | 2018-07-20 | 核工业北京化工冶金研究院 | The method that absorption method brine proposes demagging in lithium leacheate |
| CN111410216A (en) * | 2020-05-09 | 2020-07-14 | 孟元 | Method for extracting lithium from water with high magnesium-lithium ratio and preparing lithium carbonate |
| CN112695211A (en) * | 2020-12-01 | 2021-04-23 | 西安蓝深环保科技有限公司 | Continuous ion exchange method for separating lithium from salt lake brine |
| WO2022007660A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdered adsorbent |
| CN114892025A (en) * | 2022-06-02 | 2022-08-12 | 北京万邦达环保技术股份有限公司 | Simulated moving bed lithium extraction adsorption process |
-
2022
- 2022-08-16 CN CN202210982456.7A patent/CN115418479B/en active Active
Patent Citations (8)
| 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 |
| CN107058735A (en) * | 2016-12-14 | 2017-08-18 | 青海盐湖工业股份有限公司 | It is a kind of extract lithium continuous ion exchange unit and put forward lithium technique |
| CN107021513A (en) * | 2017-04-17 | 2017-08-08 | 四川大学 | The method that lithium is extracted from salt lake bittern |
| CN108298570A (en) * | 2017-12-28 | 2018-07-20 | 核工业北京化工冶金研究院 | The method that absorption method brine proposes demagging in lithium leacheate |
| CN111410216A (en) * | 2020-05-09 | 2020-07-14 | 孟元 | Method for extracting lithium from water with high magnesium-lithium ratio and preparing lithium carbonate |
| WO2022007660A1 (en) * | 2020-07-07 | 2022-01-13 | 浙江衢州明德新材料有限公司 | Method for extracting lithium from brine by using powdered adsorbent |
| CN112695211A (en) * | 2020-12-01 | 2021-04-23 | 西安蓝深环保科技有限公司 | Continuous ion exchange method for separating lithium from salt lake brine |
| CN114892025A (en) * | 2022-06-02 | 2022-08-12 | 北京万邦达环保技术股份有限公司 | Simulated moving bed lithium extraction adsorption process |
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