CN109761249A - Parse the method and system of lithium in aluminium oxide factory richness lithium adsorbent - Google Patents
Parse the method and system of lithium in aluminium oxide factory richness lithium adsorbent Download PDFInfo
- Publication number
- CN109761249A CN109761249A CN201811496554.XA CN201811496554A CN109761249A CN 109761249 A CN109761249 A CN 109761249A CN 201811496554 A CN201811496554 A CN 201811496554A CN 109761249 A CN109761249 A CN 109761249A
- Authority
- CN
- China
- Prior art keywords
- parsing
- lithium
- hydro
- thermal
- slurries filtration
- 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
Landscapes
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention discloses a kind of method and system of lithium in parsing aluminium oxide factory richness lithium adsorbent, this method includes the continuous fair current of n times or counter-flow water Thermal desorption process, and the hydro-thermal resolving successively includes parsing ingredient, hydro-thermal resolving reaction and parsing slurries filtration；The system includes N grades of fair currents or counter-flow water thermal analysis apparatus, and the hydro-thermal resolver includes the parsing dosage bunker being sequentially connected, hydro-thermal reaction unit, slurry dashpot, parsing slurries filtration machine and filtrate receiver.New process of the invention mentions the rich lithium adsorbent of lithium generation for sodium aluminate solution using absorption method, and the parsing of lithium is further carried out using the principle of high temperature and pressure leaching by hydrothermal process；Hydro-thermal reaction unit has accomplished the energy consumption of entire unit minimum using full pipeline material slurry and slurry heat transfer technology；By repeatedly adverse current parsing technique, desorbed solution lithium content is made to be greater than 0.5g/l, lithium resolution factor >=90% in adsorbent.
Description
Technical field
The invention belongs to technical field of inorganic chemical industry, are related to a kind of from the sperm of Bayer process or sintering process production aluminium oxide
The method for extracting the lithium salts of high added value, and in particular to a kind of to parse the method for lithium in aluminium oxide factory richness lithium adsorbent and be
System.
Background technique
Lithium carbonate, a kind of inorganic compound, chemical formula Li2CO3, it is colourless monoclinic system crystal body or white powder.It is close
2.11g/cm3 is spent, 618 DEG C of fusing point, diluted acid is dissolved in, is slightly soluble in water, solubility is big compared under hot water in cold water, does not dissolve in alcohol and third
Ketone.It is widely used in the industries such as battery, glass-ceramic, lubricant, pharmacy.
Lithium carbonate is the basic material for producing secondary lithium salts and lithium metal product, thus it is maximum to become dosage in lithium industry
Lithium product, other lithium products are all the downstream product of lithium carbonate on it.The production technology of lithium carbonate is according to raw material sources
Difference can be divided into salt lake bittern and extract and ore extraction.Currently, external mainly produce carbonic acid using salt lake bittern extraction process
Lithium, China then mainly use solid mineral extraction process.Although China also actively exploitation saline lake lithium resource, due to technology,
The limitation of the factors such as resource, development rate are relatively slow.
Ore extracts lithium technique: ore extracts lithium and the solids lithium ore such as spodumene, lepidolite is mainly used to produce carbonic acid
Lithium and other lithium products.The with a long history of lithium resource is extracted from ore, technology is also more mature, and main production has lime burning
Connection and sulfuric acid process, wherein sulfuric acid process is main method used at present, and process flow chart is as shown in Figure 1.
Salt lake bittern extracts lithium technique: salt lake bittern extraction lithium technique refers to extracts lithium carbonate from the salt lake bittern containing lithium
With other lithium salts products.The salt lake bittern extractive technique used in the world at present mainly has the precipitation method (carbonate precipitation method, aluminic acid
Salt precipitation method, boron magnesium and boron lithium coprecipitation), calcining leaching method, carbonizatin method, solvent extraction, ion-exchange etc., wherein molten
Agent extraction and ion-exchange realize heavy industrialization application not yet.The typical precipitation method, calcining leaching method, ion are handed over
It is as shown in Figure 2, Figure 3 and Figure 4 to change method process flow chart difference.
It recently as the fast development of New Energy Sources In China technology and popularizes, lithium ion battery production scale rapid development is led
The lithium carbonate market longer term is caused to be in a supply falls short of demand situation, in addition to demand pull factor, domestic high-quality spodumene mine is deficient
Weary, saline lakes of China high-magnesium brine separating magnesium and lithium is difficult, and external lithium industry giant's production capacity increase is limited to cause supply insufficient.
According to the Henan Zhong Lv branch company Lee's spring tide et al. result of study (Li Chunchao, Huang Jian, " lithium mistake in alumina producing
In journey there are behaviors " " light metal " the 6th phase in 2005, P17-19), into the lithium in sodium aluminate solution in subsequent kind point or
It is all precipitated and enters in aluminum hydroxide crystals with aluminium hydroxide in carbon point, basic noresidue in mother liquor, therefore can not add up.
New technique separates lithium a small amount of in sodium aluminate concentrate solution before kind point by precipitating reagent from sodium aluminate solution, and further mentions
The pure lithium carbonate product for qualification is expanded for China or even in the world and mentions lithium raw material, especially promotes the economy of alumina industry
Benefit is significant.
The Central China area universal lithium content of bauxite is higher, average oxygen-containing by taking Henan Province, the mining area Yu Shan, Xinan County as an example
Change lithium about 0.085%, lithium disperses preservation (Ji Qinghai, Ji fruit etc., " Xinan County in the mineral such as bauxite, kaolinite, illite
The research of Yu Shan Geological Characteristics of Bauxite and accompanying element " " mineral products protection and utilization " the 3rd phase in 2014, P10-14), lithium is being visitd
About 80% enters solution in ear method process in leaching, and 20% drains with red mud, eventually enters into finished product into the lithium in sodium aluminate solution
In aluminium oxide, table 1 is the measurement to lithium content is aoxidized in Central China regional several main oxidation aluminium enterprise alumina product, number
According to source Zhengzhou Inst of Light Metals inspection center.
Lithium content in 1 Central China area portion alumina producer finished product aluminium oxide of table
| Factory | Li2O, % |
| A factory | 0.094 |
| B factory | 0.11 |
| C factory | 0.13 |
| D factory | 0.12 |
| E factory | 0.13 |
As seen from Table 1, Li in Central China area aluminium oxide factory products2O is generally higher, usual import aluminium oxide Li2O
Only 0.006%, if aluminium oxide yield is by 12,000,000 tons/year of estimations, every year via metallurgical-grade aluminum oxide band by 0.1% estimation
The Li walked2O is up to 12000 tons, these lithium resources are not utilized rationally, and What is more, and rich lithium aluminium is used for a long time and makees
It is more than reasonable interval for lithium enrichment in the electrolysis plant electrolyte of raw material, causes electrolytic cell degrading, it in turn must not be quantity-unlimiting
Use rich lithium aluminium.
Being consulted domestic and international pertinent literature there are no the report of lithium in parsing aluminium oxide factory richness lithium adsorbent.
Therefore, present invention proposition parses lithium from middle part province aluminium oxide factory richness lithium adsorbent, i.e., money is rationally utilized
Source, and improve aluminium oxide quality, solve the trouble and worry of electrolysis plant.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides lithiums in a kind of parsing aluminium oxide factory richness lithium adsorbent
Method and system.
A kind of method for parsing lithium in aluminium oxide factory richness lithium adsorbent, including n times are provided according to an aspect of the present invention
Continuous fair current or counter-flow water Thermal desorption process, N are the positive integer greater than 2, and the hydro-thermal resolving successively includes that parsing is matched
Material, hydro-thermal resolving reaction and parsing slurries filtration, the solid phase of first time parsing ingredient are rich lithium adsorbent, described second
Solid phase to n-th parsing ingredient is respectively to parse the filter cake obtained after slurries filtration, the first time to the N-1 times for the first time
The liquid phase for parsing ingredient to the N-1 times is respectively to parse the filtrate obtained after slurries filtration, the n-th to n-th for the second time
The liquid phase for parsing ingredient is clean hot water, and the filtrate obtained after the first time parsing slurries filtration is rich lithium desorbed solution.
In the above-mentioned technical solutions, the reaction temperature of the hydro-thermal resolving reaction is 160-220 DEG C, reaction time 0.5-
2h, L/S 5-30.
A kind of system for parsing lithium in aluminium oxide factory richness lithium adsorbent, including N are provided according to a further aspect of the invention
Grade fair current or counter-flow water thermal analysis apparatus, N are the positive integer greater than 2, and the hydro-thermal resolver includes the parsing being sequentially connected
Dosage bunker, hydro-thermal reaction unit, slurry dashpot, parsing slurries filtration machine and filtrate receiver；
The fluid inlet end of described first to N-1 parsing dosage bunker is connected with second to N filtrate receiver discharge port respectively,
The filtered solid outlet that the solid phase input end of described second to N parsing dosage bunker parses slurries filtration machine with first to N-1 respectively
It is connected, the discharge end of the described first to N parsing dosage bunker is connected with first to N hydro-thermal reaction unit feed end respectively；
Described first to N slurry dashpot feed end and discharge end respectively with described first to N hydro-thermal reaction machine
The discharge end of group is connected with the described first to N parsing slurries filtration machine feed end, the described first to N parsing slurries filtration machine
Filtrate (liquid be connected respectively with described first to N filtrate receiver feed inlet.
In the above-mentioned technical solutions, the hydro-thermal reaction unit includes that the high-pressure diaphragm pump being sequentially connected, multi-stage pipeline are pre-
Hot device, pipeline heater and stop pipeline, the feed end and discharge end of the high-pressure diaphragm pump respectively with the parsing dosage bunker
Discharge end be connected with the cold phase feed end of the multi-stage pipeline preheater, the cold phase feed end of the pipeline heater and cold phase
Discharge end is connected with the cold phase discharge end of the multi-stage pipeline preheater and the stop pipeline feed end respectively, and the pipeline adds
The hot phase feed end of hot device connects high steam, the hot phase feed end and hot phase discharge end of the multi-stage pipeline preheater respectively with
The stop pipeline discharge end is connected with the feed end of the slurry dashpot.
In the above-mentioned technical solutions, the parsing dosage bunker and/or the slurry dashpot are that conventional carbon steel normal pressure stirs
Mix slot.
In the above-mentioned technical solutions, the parsing slurries filtration machine is vacuum filter or flame filter press.
Further, in the above-mentioned technical solutions, the series of the multi-stage pipeline preheater is greater than 6 grades.
Still further, in the above-mentioned technical solutions, the multi-stage pipeline preheater is three casings or Quadruplet pipe, preferably
Quadruplet pipe.
Still further, in the above-mentioned technical solutions, the stop pipeline is single tube.
Compared with prior art, beneficial effects of the present invention are as follows:
(1) new process mentions the rich lithium adsorbent of lithium generation for sodium aluminate solution using absorption method, further uses high temperature
The principle of high pressure leaching by hydrothermal process carries out the parsing of lithium, belongs to pioneering both at home and abroad；
(2) hydro-thermal reaction unit accomplishes the energy consumption of entire unit using full pipeline material slurry and slurry heat transfer technology
It is minimum；
(3) by repeatedly adverse current parsing technique, make desorbed solution lithium content greater than 0.5g/l, lithium resolution factor in adsorbent >=
90%.
Detailed description of the invention
Fig. 1 is the process flow chart that sulfuric acid roasting method mentions lithium from spodumene in the prior art；
Fig. 2 is the process flow chart that the precipitation method mention lithium from concentrated brine in the prior art；
Fig. 3 is the process flow chart that calcining leaching method mentions lithium from brine in the prior art；
Fig. 4 is the process flow chart that prior art ion exchange methods mention lithium from brine；
Fig. 5 be the embodiment of the present invention in slave aluminium oxide factory richness lithium adsorbent in parse lithium process flow chart；
Fig. 6 be the embodiment of the present invention in slave aluminium oxide factory richness lithium adsorbent in parse lithium system composition schematic diagram；
Fig. 7 be the embodiment of the present invention in slave aluminium oxide factory richness lithium adsorbent in parse lithium hydro-thermal reaction unit group
At schematic diagram；
In figure:
First parsing dosage bunker 11, the first hydro-thermal reaction unit 12, the first slurry dashpot 13, the first parsing slurries filtration
Machine 14, the first filtrate receiver 15, the second parsing dosage bunker 21, the second hydro-thermal reaction unit 22, the second slurry dashpot 23, the second solution
Slurries filtration machine 24, the second filtrate receiver 25 are analysed, third parses dosage bunker 31, third hydro-thermal reaction unit 32, third slurry buffering
Slot 33, third parse slurries filtration machine 34, and third filtrate receiver 35, high-pressure diaphragm pump 201, multi-stage pipeline preheater 202, pipeline adds
Hot device 203 stops pipeline 204.
Specific embodiment
To facilitate the understanding of the present invention, with reference to the accompanying drawings and examples, fluid pressure type gas compression of the invention is purified
System and its compression purification method make further more comprehensively with detailed description.
Presently preferred embodiments of the present invention is given in Figure of description；But the present invention can be with many different forms
It realizes, and is not limited to embodiment described herein；On the contrary, purpose of providing these embodiments is makes to the present invention
Disclosure understanding it is more thorough and comprehensive.
Unless otherwise defined, all technical and scientific terms used herein and belong to technical field of the invention
The normally understood meaning of technical staff is identical.Term as used herein in the specification of the present invention is intended merely to description tool
The purpose of the embodiment of body, it is not intended that in the limitation present invention.Term " and or " used herein includes one or more phases
Any and all combinations of the listed item of pass.
Embodiment
As shown in fig. 6, the embodiment of the invention provides a kind of system of lithium in parsing aluminium oxide factory richness lithium adsorbent, packet
Include three-level counter-flow water thermal analysis apparatus, every level-one aquathermolysis analysis apparatus includes that the parsing dosage bunker being sequentially connected, hydro-thermal are anti-
Answer unit, slurry dashpot, parsing slurries filtration machine and filtrate receiver.
It is described first parsing dosage bunker 11 and second parsing dosage bunker 21 fluid inlet end respectively with the second filtrate receiver 25
It is connected with 35 discharge port of third filtrate receiver, the fluid inlet end of the third parsing dosage bunker 31 connects clean water；It is described wait solve
The aluminium oxide factory richness lithium adsorbent of analysis is added in the first parsing dosage bunker 11, the second parsing dosage bunker 21 and third solution
The solid phase input end for analysing dosage bunker 31 parses the filter cake of slurries filtration machine 24 with the first parsing slurries filtration machine 14 and second respectively
Outlet is connected, and the first parsing dosage bunker 11, second parses the discharge end difference of dosage bunker 21 and third parsing dosage bunker 31
It is connected with the feed end of the first hydro-thermal reaction unit 12, the second hydro-thermal reaction unit 22 and third hydro-thermal reaction unit 32.
The feed end of the first slurry dashpot 13, the second slurry dashpot 23 and third slurry dashpot 33 respectively with
The first hydro-thermal reaction unit 12, the second hydro-thermal reaction unit 22 are connected with the discharge end of third hydro-thermal reaction unit 32, out
Expect that end parses slurries filtration machine 24 with the first parsing slurries filtration machine 14, second respectively and third parses slurries filtration machine 34
Feed end is connected, and the first parsing slurries filtration machine 14, second parses slurries filtration machine 24 and third parses slurries filtration machine
34 filtrate (liquid is connected with first filtrate receiver 15, the second filtrate receiver 25 and 35 feed inlet of third filtrate receiver respectively.
Specifically, as shown in fig. 7, the first hydro-thermal reaction unit 12, the second hydro-thermal reaction unit 22 and third hydro-thermal
Reaction unit 32 respectively includes the high-pressure diaphragm pump 201 being sequentially connected, multi-stage pipeline preheater 202, pipeline heater 203 and stops
Stay pipeline 204, the feed end and discharge end of the high-pressure diaphragm pump 201 respectively with the discharge end of the parsing dosage bunker and described
The cold phase feed end of multi-stage pipeline preheater 202 is connected, the cold phase feed end and cold phase discharge end point of the pipeline heater 203
It is not connected with the cold phase discharge end of the multi-stage pipeline preheater 202 and 204 feed end of stop pipeline, the pipeline heating
The hot phase feed end of device 203 connects high steam, the hot phase feed end and hot phase discharge end point of the multi-stage pipeline preheater 202
It is not connected with the feed end of stop 204 discharge end of pipeline and the slurry dashpot.
In detail, the parsing dosage bunker and/or the slurry dashpot are conventional carbon steel atmospheric agitation slot.
In detail, the parsing slurries filtration machine is vacuum filter or flame filter press.
In detail, the series of the multi-stage pipeline preheater 202 is greater than 6 grades.
In detail, the multi-stage pipeline preheater 202 is three casings or Quadruplet pipe, preferably Quadruplet pipe.
In detail, the stop pipeline 204 is single tube.
Utilize above system, the method for parsing lithium in aluminium oxide factory richness lithium adsorbent, as shown in figure 5, specifically including three
Secondary continuous counter-flow water Thermal desorption process, the hydro-thermal resolving successively includes parsing ingredient, hydro-thermal resolving reaction each time
With parsing slurries filtration, the solid phase of the first time parsing ingredient is rich lithium adsorbent, and described second and third time parsing are matched
The solid phase of material is respectively the filter cake obtained for the first time and after second of parsing slurries filtration, and the first time and second of parsing are matched
The liquid phase of material is respectively second and third time parses the filtrate obtained after slurries filtration, the liquid phase of the third time parsing ingredient
For clean hot water, it is rich lithium desorbed solution that the first time, which parses the filtrate obtained after slurries filtration,.
In a specific embodiment, with certain aluminium oxide factory sperm, sperm is containing Nk=160g/l, Rp=1.08, Li+=
0.050g/l, by adsorbing, the processes such as molten, the rich lithium adsorbent of output contain Li again2O reaches 4.0% filter cake, enters solution per hour
The flow for analysing the dry rich lithium adsorbent of process is 1.0t/h, carries out slurrying with secondary desorbed solution, controls slurry L/S=15 ± 1, beat
Enter the first hydro-thermal reaction unit, 85 DEG C of slurry temperature, mineral slurry flux about 15m3/h。
89 × 5mm of inner tube 57 × 4mm of Φ, outer tube Φ of multi-stage pipeline preheater 7, every grade of casing length 80m (one way) have
Imitate heat exchange area 14m2, 8 inner and outer pipes caliber of pipeline heater is identical as multi-stage pipeline preheater 7, length 160m (round trip), stops
Pipeline 9 caliber 89 × 5mm of Φ, length 1520m (19 journey).240 DEG C of hydro-thermal reaction unit design maximum heating temperature, autoclave diaphragm
Pump 6 design pressure 6.0Mpa.
Specifically, as shown in fig. 7, the first hydro-thermal reaction unit 12, the second hydro-thermal reaction unit 22 and third hydro-thermal
Reaction unit 32 respectively includes the high-pressure diaphragm pump 201 being sequentially connected, multi-stage pipeline preheater 202, pipeline heater 203 and stops
Stay pipeline 204, the feed end and discharge end of the high-pressure diaphragm pump 201 respectively with the discharge end of the parsing dosage bunker and described
The cold phase feed end of multi-stage pipeline preheater 202 is connected, the cold phase feed end and cold phase discharge end point of the pipeline heater 203
It is not connected with the cold phase discharge end of the multi-stage pipeline preheater 202 and 204 feed end of stop pipeline, the pipeline heating
The hot phase feed end of device 203 connects high steam, the hot phase feed end and hot phase discharge end point of the multi-stage pipeline preheater 202
It is not connected with the feed end of stop 204 discharge end of pipeline and the slurry dashpot.
Pipeline heater 203 exports slurry temperature and controls 220 DEG C, and ore pulp adverse current enters multiple valve after stopping pipeline 204
It exchanges heat in 202 outer tube of road preheater, the final slurry temperature of first order pipeline preheater outer tube is down to 95 DEG C, slow into slurry
Jet-bedding, high steam consumption are 1.0-1.5t/h.
Parsing slurries filtration machine selects DU1.3 × 8m rubber belt type vacuum filter, filter area 10.4m2, filter cake after filtering
Moisture content 65-70%.
After counter-flow water Thermal desorption three times, final filter cake contains Li2O≤0.3%, the total resolution factor >=92.5%, the first of lithium
Desorbed solution contains Li in filtrate receiver 15+=1150mg/l.
Finally, being not intended to limit the scope of the present invention the above is only preferred embodiment of the invention.It is all this
Within the spirit and principle of invention, any modification, equivalent replacement, improvement and so on should be included in protection model of the invention
Within enclosing.
Claims (8)
1. a kind of method of lithium in parsing aluminium oxide factory richness lithium adsorbent, which is characterized in that including the continuous fair current of n times or inverse
Flowing water Thermal desorption process, N are the positive integer greater than 2, and the hydro-thermal resolving successively includes parsing ingredient, hydro-thermal resolving reaction
With parsing slurries filtration, the solid phase of the first time parsing ingredient is rich lithium adsorbent, described to parse ingredient to n-th for the second time
Solid phase be respectively for the first time to obtained filter cake after the N-1 time parsing slurries filtration, the first time to the N-1 times parsing matches
The liquid phase of material is respectively to parse the filtrate obtained after slurries filtration to n-th for the second time, and the liquid phase of the n-th parsing ingredient is
Clean hot water, it is rich lithium desorbed solution that the first time, which parses the filtrate obtained after slurries filtration,.
2. the method according to claim 1, wherein the reaction temperature of the hydro-thermal resolving reaction is 160-220
DEG C, reaction time 0.5-2h, L/S 5-30.
3. the system of lithium in a kind of parsing aluminium oxide factory richness lithium adsorbent, which is characterized in that including N grades of fair currents or adverse current hydro-thermal
Resolver, N are the positive integer greater than 2, and the hydro-thermal resolver includes the parsing dosage bunker being sequentially connected, hydro-thermal reaction machine
Group, slurry dashpot, parsing slurries filtration machine and filtrate receiver；
The fluid inlet end of described first to N-1 parsing dosage bunker is connected with second to N filtrate receiver discharge port respectively, described
The solid phase input end of second to N parsing dosage bunker is connected with the filtered solid outlet of the first to N-1 parsing slurries filtration machine respectively,
The discharge end of described first to N parsing dosage bunker is connected with first to N hydro-thermal reaction unit feed end respectively；
Described first to N slurry dashpot feed end and discharge end respectively with described first to N hydro-thermal reaction unit
Discharge end is connected with the described first to N parsing slurries filtration machine feed end, the filter of the described first to N parsing slurries filtration machine
Liquid outlet is connected with described first to N filtrate receiver feed inlet respectively.
4. system according to claim 3, which is characterized in that the hydro-thermal reaction unit include the high pressure that is sequentially connected every
Membrane pump, multi-stage pipeline preheater, pipeline heater and stop pipeline, the feed end and discharge end of the high-pressure diaphragm pump respectively with
It is described parsing dosage bunker discharge end be connected with the cold phase feed end of the multi-stage pipeline preheater, the pipeline heater it is cold
Phase feed end and cold phase discharge end respectively with the cold phase discharge end of the multi-stage pipeline preheater and the stop pipeline feed end
Be connected, the hot phase feed end of the pipeline heater connects high steam, the hot phase feed end of the multi-stage pipeline preheater and
Hot phase discharge end is connected with the feed end of the stop pipeline discharge end and the slurry dashpot respectively.
5. system according to claim 3, which is characterized in that the parsing dosage bunker and/or the slurry dashpot are
Conventional carbon steel atmospheric agitation slot.
6. system according to claim 3, which is characterized in that the parsing slurries filtration machine is vacuum filter or sheet frame
Filter.
7. system according to claim 4, which is characterized in that the series of the multi-stage pipeline preheater is greater than 6 grades.
8. the system according to claim 4 or 7, which is characterized in that
The multi-stage pipeline preheater is three casings or Quadruplet pipe, preferably Quadruplet pipe；
And/or the stop pipeline is single tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811496554.XA CN109761249B (en) | 2018-12-07 | 2018-12-07 | Method and system for resolving lithium in lithium-rich adsorbent of alumina plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811496554.XA CN109761249B (en) | 2018-12-07 | 2018-12-07 | Method and system for resolving lithium in lithium-rich adsorbent of alumina plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109761249A true CN109761249A (en) | 2019-05-17 |
| CN109761249B CN109761249B (en) | 2021-07-27 |
Family
ID=66451319
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811496554.XA Active CN109761249B (en) | 2018-12-07 | 2018-12-07 | Method and system for resolving lithium in lithium-rich adsorbent of alumina plant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109761249B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112981140A (en) * | 2021-01-29 | 2021-06-18 | 格尔木藏格锂业有限公司 | Method for extracting lithium-rich solution from ultra-low lithium concentration brine by multi-stage combined adsorption method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102918170A (en) * | 2010-11-26 | 2013-02-06 | 韩国地质资源研究院 | Apparatus and method for adsorbing and desorbing lithium ions using a ccd process |
| CN104383901A (en) * | 2014-12-03 | 2015-03-04 | 青海盐湖工业股份有限公司 | Method for restoring property of lithium adsorbent |
| KR20150076303A (en) * | 2013-12-26 | 2015-07-07 | 재단법인 포항산업과학연구원 | Method of recovering manganese in sea water and method of preparing lithium absorbent |
| CN105692659A (en) * | 2016-01-26 | 2016-06-22 | 中国科学院过程工程研究所 | Method for extracting lithium from fly ash |
| CN105883927A (en) * | 2016-04-07 | 2016-08-24 | 黄冈师范学院 | Method for desorption of lithium manganate series adsorbent precursor |
| 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 |
| CN108083301A (en) * | 2017-11-10 | 2018-05-29 | 江苏旌凯中科超导高技术有限公司 | The method that lithium is extracted from bittern using magnetic powder aluminium system lithium adsorbent |
-
2018
- 2018-12-07 CN CN201811496554.XA patent/CN109761249B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102918170A (en) * | 2010-11-26 | 2013-02-06 | 韩国地质资源研究院 | Apparatus and method for adsorbing and desorbing lithium ions using a ccd process |
| KR20150076303A (en) * | 2013-12-26 | 2015-07-07 | 재단법인 포항산업과학연구원 | Method of recovering manganese in sea water and method of preparing lithium absorbent |
| CN104383901A (en) * | 2014-12-03 | 2015-03-04 | 青海盐湖工业股份有限公司 | Method for restoring property of lithium adsorbent |
| CN105692659A (en) * | 2016-01-26 | 2016-06-22 | 中国科学院过程工程研究所 | Method for extracting lithium from fly ash |
| CN105883927A (en) * | 2016-04-07 | 2016-08-24 | 黄冈师范学院 | Method for desorption of lithium manganate series adsorbent precursor |
| 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 |
| CN108083301A (en) * | 2017-11-10 | 2018-05-29 | 江苏旌凯中科超导高技术有限公司 | The method that lithium is extracted from bittern using magnetic powder aluminium system lithium adsorbent |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112981140A (en) * | 2021-01-29 | 2021-06-18 | 格尔木藏格锂业有限公司 | Method for extracting lithium-rich solution from ultra-low lithium concentration brine by multi-stage combined adsorption method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109761249B (en) | 2021-07-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2016184055A1 (en) | Process method for extracting magnesium and lithium from brine and coproducing hydrotalcite | |
| CN109650413B (en) | Method and system for enriching lithium from sodium aluminate solution in alumina plant | |
| JP5850550B2 (en) | Method for producing taurine | |
| CN107500318B (en) | The method of lithium carbonate is extracted from aluminium oxide factory sodium aluminate solution | |
| CN102145905B (en) | Method for preparing metallurgy-level aluminum oxide by using fluidized bed pulverized fuel ash | |
| CN104495899B (en) | A kind of carbide slag and flyash work in coordination with the method for recycling | |
| CN102583446B (en) | Method for preparing potassium chloride through decomposing carnallite by concentrated brine | |
| CN104016393B (en) | A kind of by dolomite for light calcium carbonate and method of magnesium oxide | |
| CN102897810B (en) | Method for producing aluminum oxide by using fly ash | |
| CN111268706B (en) | Method for producing high-purity magnesium hydroxide, high-purity magnesium oxide and high-purity magnesite serial magnesium products by using salt lake brine | |
| CN102139894A (en) | Novel method for preparing battery grade lithium carbonate by using tantalum niobium tailings lithium mica | |
| CN103496746A (en) | Method for preparing cell-grade high-purity manganese sulfate by low-grade manganese ore high-pressure crystallization | |
| CN105800653A (en) | Method for extracting aluminum oxide from fly ash on basis of soda-lime sintering process | |
| CN113511663A (en) | Process for preparing lithium carbonate by extracting lithium from oil field underground brine | |
| CN212609591U (en) | System for extracting sodium sulfate and sodium chloride from wastewater by separating salt based on nanofiltration membrane technology | |
| CN103663516B (en) | A kind of method utilizing aluminous fly-ash to prepare aluminium hydroxide | |
| CN103539182B (en) | Method for preparing aluminum chloride hexahydrate by using pulverized fuel ash as raw material through ferrous chloride induced crystallization | |
| CN109761249A (en) | Parse the method and system of lithium in aluminium oxide factory richness lithium adsorbent | |
| CN113955775B (en) | Method for extracting lithium carbonate from lithium-rich clay by acid-base combined method | |
| CN204589321U (en) | Water electrolysis is utilized to prepare pure hydrogen and oxygen reclamation system | |
| CN107162029B (en) | Red mud method of comprehensive utilization | |
| CN109650416A (en) | The method and system of purification concentration aluminium oxide factory desorbed solution containing lithium | |
| CN111689469B (en) | Process for preparing high-purity hydrogen by adopting palladium alloy membrane purification | |
| CN104030331A (en) | Method for producing aluminum oxide by utilizing high-alumina fly ash | |
| CN109336154A (en) | A method of using coal ash for manufacturing for crystalline sulfuric acid aluminium |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20210616 Address after: 472100 Shanxian Industrial Park, Sanmenxia City, Henan Province Applicant after: KAIMAN ALUMINUM (SANMENXIA) Co.,Ltd. Address before: 472100 Kaiman Aluminum Industrial Park, Sanmenxia City, Henan Province Applicant before: SANMENXIA LIANLI NEW MATERIAL Co.,Ltd. |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |