CN102676809B - Arsenic-alkali separation method for leaching agent after removing antimony from sodium carbonate type arsenic-alkali slag in antimony smelting process - Google Patents
Arsenic-alkali separation method for leaching agent after removing antimony from sodium carbonate type arsenic-alkali slag in antimony smelting process Download PDFInfo
- Publication number
- CN102676809B CN102676809B CN201210137936.XA CN201210137936A CN102676809B CN 102676809 B CN102676809 B CN 102676809B CN 201210137936 A CN201210137936 A CN 201210137936A CN 102676809 B CN102676809 B CN 102676809B
- Authority
- CN
- China
- Prior art keywords
- antimony
- arsenic
- alkali
- separation method
- concentrated
- 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.)
- Active
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Landscapes
- Manufacture And Refinement Of Metals (AREA)
- Inorganic Compounds Of Heavy Metals (AREA)
Abstract
The invention provides an arsenic-alkali separation method for a leaching agent after removing antimony from sodium carbonate type arsenic-alkali slag in an antimony smelting process. The arsenic-alkali separation method comprises the following steps of: (1) concentrating the leaching agent after removing the antimony until the density of a concentrated solution is 1.36-1.40, crystallizing and filtering; (2) concentrating a filtrate until the density of a concentrated solution is 1.42-1.45, crystallizing and filtering; (3) concentrating the filtrate until the density of a concentrated solution is 1.50-1.55, crystallizing and filtering; (4) concentrating the filtrate until the arsenic content in the concentrated solution is not less than 80 g/l, cooling and crystallizing to the temperature of 30-35 DEG C, and filtering; (5) circularly using the filtrate; re-dissolving a primary crystal, a secondary crystal or a third-time crystal with the arsenic content ofmore than 1 wt% with a saturated sodium carbonate solution; concentrating the solution until the density of a concentrated solution is 1.42-1.45; and crystallizing at the temperature of 80-100 DEG C. With the adoption of the arsenic-alkali separation method provided by the invention, the effective arsenic-alkali separation of the sodium carbonate type arsenic-alkali slag in the antimony smelting process and the comprehensive use of arsenic and alkali can be realized; and the arsenic-alkali separation method has no pollution on an environment.
Description
Technical field
The present invention relates to a kind for the treatment of process of antimony smelting arsenic alkali slag, especially relate to a kind of antimony and smelt the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag.
Background technology
It is the arsenic removal scum silica frost producing while adding soda ash arsenic removal in antimony smelting refining process that antimony is smelted soda ash type arsenic alkali slag, or the secondary arsenic alkali slag of its reduction generation, or alkali be take sodium carbonate as main arsenic alkali slag, its complicated, different and different with needle antimony composition before refining, and fluctuation range is large, antimony content is generally 1-45%, arsenic content is 0.1-20%, its major ingredient is sodium antimonate, antimonous acid sodium, sodium arseniate, Sodium metaarsenite, sodium carbonate, sodium sulfate, selenite, sodium hydroxide, antimony and silicate etc., and wherein the arsenic overwhelming majority is that form with sodium arseniate exists.At present,, environmentally safely there is huge potential safety hazard in domestic ten thousand tons of the about 20-30 of soda ash type arsenic alkali slag that store up.Conventionally to the processing of arsenic alkali slag, be to adopt hot water leaching, antimony and most of metaantimmonic acid sodium salt enter leached mud, then leach liquor is added to de-antimony agent, remove the antimonic salt in leach liquor, and this method can realize the separation of antimony arsenic in arsenic alkali slag substantially.The antimony slag forming returns to stibium blast furnace system and processes, and can realize the Efficient Cycle utilization of antimony resource.Leach liquor after de-antimony contains sodium carbonate, sodium sulfate, sodium arseniate, Sodium Selenite, sodium hydroxide etc., these several sodium salts mix, because its character has a lot of similarities, up to the present, also not having good separation method to carry out effectively separation to them effectively fully utilizes with the product to after separated.The effective separation and the comprehensive utilization that realize soluble sodium salt in above-mentioned leach liquor are the keys of arsenic alkali slag treatment technology.
Traditional antimony smelting arsenic alkali slag arsenic alkali separation method has chemical precipitation method, sodium arseniate composite salt method, CAM etc., as the propositions such as Jin Zhenan [refer to Jin Zhenan etc. by the treatment process of calcium hydroxide arsenic precipitation, process the novel process of antimony regulus arsenic alkali slag, non-ferrous metal metallurgy (Smelting Part), 1999,11(5): 11-14]; Adopt Na during Xu Li etc.
2s makes vulcanizing agent Sulphuration Dearsenication of Leaching Liquor from Arsenic Containing Alkaline Dregs Generated in Antimony Smelting is studied [while referring to Xu Li etc.; brief talk antimony regulus arsenic-containing waste residue treatment process; tinnery science and technology; 1997; (3): 30-33], antimony smelting deeply removing arsenic technology is comparatively perfect, but its can produce a large amount of arsenic trisulfide waste residues that contain after processing; cause secondary pollution, be unfavorable for environment protection.When sodium arseniate composite salt method is processed soda ash type arsenic alkali slag, although can realize the better separation of arsenic antimony, to the comprehensive utilization of arsenic alkali, can not effectively carry out, soda ash can not effectively separated and utilization, and sodium arseniate can not effectively utilize as product because its arsenic content is low.Composite salt can not be fully utilized, and can cause new potential safety hazard to environment again, becomes secondary pollutant.The arsenic containing solution of a CAM suitable treatment lower concentration, and processing power is low.
Summary of the invention
Technical problem to be solved by this invention is, the comprehensive utilization of a kind of effective separation that realizes arsenic alkali in arsenic alkali slag and arsenic, alkali is provided, and the antimony of environmentally safe is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag simultaneously.
The technical scheme that the present invention solves its technical problem employing is: a kind of antimony is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, comprises the following steps:
(1) leach liquor after de-antimony is placed in to condensing crystal tank, at 100 ℃, concentrates, when concentrated solution density reaches 1.36-1.40, stop concentrating, 80-100 ℃ (preferably 86-95 ℃), carry out crystallization (crystallization time preferably >=25 minutes), filter, obtain primary crystallization thing, first-time filtrate;
(2) first-time filtrate is concentrated for the second time at 100 ℃, when concentrated solution density reaches 1.42-1.45, stop concentrating, 80-100 ℃ (preferably 86-95 ℃), carry out crystallization (crystallization time preferably >=20 minutes), filter, obtain secondary crystal thing, secondary filtrate;
(3) secondary filtrate is concentrated for the third time at 100 ℃, when concentrated solution density reaches 1.50-1.55, stop concentrating, 80-100 ℃ (preferably 86-95 ℃), carry out crystallization (crystallization time preferably >=10 minutes), filter, obtain three crystallisates, three filtrates;
(4) by three filtrates 100 ℃ carry out the 4th time concentrated, in concentrated solution, during arsenic content >=80g/l, stop concentrating, then crystallisation by cooling, to 30-35 ℃, filters, and obtains four crystallisates, four filtrates;
(5) four filtrates are returned to lower batch of first-time filtrate or secondary filtrate and concentrated together, recycle; Arsenic content is greater than to primary crystallization thing, secondary crystal thing or three crystallisates of 1wt%, after heavily molten with saturated sodium carbonate solution, at 100 ℃, being concentrated into concentrated solution density is 1.42-1.45, in 80-100 ℃ of (preferably 86-95 ℃) crystallization (crystallization time preferably >=30 minutes), obtain arsenic content lower than the crystalline alkali of 1wt% again.
The present invention utilizes the difference of the solubleness in differing temps interval such as sodium carbonate, sodium sulfate, sodium arseniate, and the leaching liquor of arsenic-containing alkaline dregs to after de-antimony, carries out substep condensing crystal, to complete the separation of arsenic alkali in arsenic alkali slag in differing temps interval.
Utilize the present invention, can realize the comprehensive utilization that antimony is smelted effective separation of arsenic alkali in soda ash type arsenic alkali slag and arsenic, alkali, whole flow process closed cycle, without new three waste products generations, environmentally safe.There is good economic benefit, significant environmental benefit.
Utilize the present invention to process soda ash type arsenic alkali slag, sodium arseniate content >=38wt% in the 4th crystallisate of gained, after drying, can be used as glass fining agent etc.; Gained arsenic content, lower than the crystalline alkali of 1wt%, can be used for the production of antimony smelting and glass industry etc., remarkable in economical benefits.
Embodiment
Below in conjunction with embodiment, the invention will be further described.
Embodiment 1
The present embodiment comprises the following steps:
(1) the leach liquor 1000ml(getting after de-antimony contains arsenic 11.9g/l), at 100 ℃, concentrate 60 minutes, the volume of concentrated solution is 400ml, density 1.375, stopped concentrating, 80 ℃ of crystallizations 40 minutes, filter, obtain primary crystallization thing, first-time filtrate, in primary crystallization thing, contain arsenic 0.43wt%;
(2) first-time filtrate is concentrated for the second time at 100 ℃, the volume that is concentrated into concentrated solution is 300ml, and concentrated solution density is 1.42,80 ℃ of crystallizations 30 minutes, filters, and obtains secondary crystal thing and secondary filtrate, contains arsenic 1.43wt% in secondary crystal thing;
(3) secondary filtrate is concentrated for the third time at 100 ℃, the volume that is concentrated into concentrated solution is 225ml, and concentrated solution density is 1.515,80 ℃ of crystallizations 20 minutes, filters, and obtains three crystallisates and three filtrates, contains arsenic 2.09wt% in three crystallisates;
(4) three filtrates are concentrated at 100 ℃, when in concentrated solution, arsenic content is 80g/l, stop concentrating, then crystallisation by cooling to 30 ℃, filter, obtain four crystallisates, four filtrates, four times crystallisates are 38.0% containing arsenic 13.696wt%(folding sodium arseniate content), four times filtrate arsenic content is 11.6g/l;
(5) four filtrates are returned to lower batch of first-time filtrate or secondary filtrate and concentrated together, recycle; Arsenic content is greater than to the secondary crystal thing (containing arsenic 1.43wt%) of 1wt%, three crystallisates (containing arsenic 2.09wt%), with saturated sodium carbonate solution heavy molten after, at 100 ℃, being concentrated into concentrated solution density is 1.43, again in 86 ℃ of crystallizations, crystallization time 60 minutes, obtains the crystalline alkali of arsenic content 0.76wt%.
Embodiment 2
The present embodiment comprises the following steps:
(1) get leach liquor (containing the arsenic 11.6g/l) 1000ml after de-antimony, 100 ℃ concentrated 50 minutes to volume be 500ml, concentrated solution density is 1.365,90 ℃ of crystallizations 30 minutes, filter, obtain primary crystallization thing and first-time filtrate, in primary crystallization thing, contain arsenic 0.73wt%;
(2) first-time filtrate is concentrated for the second time in 100 ℃, the volume that is concentrated into concentrated solution is 360ml, and concentrated solution density is 1.43, in 90 ℃ of crystallizations 20 minutes, filters, and obtains secondary crystal thing and secondary filtrate, in secondary crystal thing containing arsenic 1.48wt%;
(3) secondary filtrate is concentrated for the third time in 100 ℃, the volume that is concentrated into concentrated solution is 260ml, and concentrated solution density is 1.50, in 90 ℃ of crystallizations 10 minutes, filters, and obtains three crystallisates and three filtrates, in three crystallisates containing arsenic 2.05wt%;
(4) three filtrates are concentrated in 100 ℃ again, the volume that is concentrated into concentrated solution is 200ml, arsenic content 85g/l, then crystallisation by cooling to 33 ℃, filter, obtaining four crystallisates and four filtrates, is 38.1% containing arsenic 13.73wt%(folding sodium arseniate content in four crystallisates), four times filtrate arsenic content is 1.65g/l;
(5) four filtrates are returned to lower batch of first-time filtrate or secondary filtrate and concentrated together, recycle; Arsenic content is greater than to the secondary crystal thing (containing arsenic 1.48wt%) of 1wt%, three crystallisates (containing arsenic 2.05wt%), with saturated sodium carbonate solution heavy molten after, at 100 ℃, being concentrated into concentrated solution density is 1.42, again in 95 ℃ of crystallizations, crystallization time 50 minutes, obtains the crystalline alkali of arsenic content 0.89wt%.
Embodiment 3
The present embodiment comprises the following steps:
(1) by the leach liquor after de-antimony (containing arsenic 8.57g/l) 5.1m
3be placed in 8m
3in condensing crystal tank, at 100 ℃, being concentrated into concentrated solution volume is 2.3m
3, concentrated solution density is 1.385,95 ℃ of crystallizations 180 minutes, filters, and obtains primary crystallization thing 419.9kg, first-time filtrate, contains arsenic 0.71wt% in primary crystallization thing;
(2) first-time filtrate separately being allocated into front batch the 4th crystallization and filtration gained filtrate to filtrate volume is 3.1m
3, at 100 ℃, concentrate for the second time, being concentrated into concentrated solution volume is 2.66m
3, concentrated solution density is 1.42,95 ℃ of crystallizations 180 minutes, filters, and obtains secondary crystal thing 352kg, secondary filtrate, contains arsenic 1.69wt% in secondary crystal thing;
(3) secondary filtrate is concentrated for the third time at 100 ℃, being concentrated into concentrated solution volume is 1.6m
3, concentrated solution density is 1.51,95 ℃ of crystallizations 180 minutes, filters, and obtains three crystallisate 311kg, three filtrates, in three crystallisates, arsenic content is 2.18wt%;
(4) three filtrates are concentrated at 100 ℃, be concentrated into arsenic content in concentrated solution and reach 105.96g/l, crystallisation by cooling to 32 ℃, filter, obtain four crystallisate 300kg, four filtrates, in four crystallisates, arsenic content is that 18.59wt%(folding sodium arseniate content is 51.56%), in four filtrates, arsenic content is 15.87g/l;
(5) four filtrates are returned to lower batch of secondary filtrate and concentrated together, recycle; Arsenic content is greater than to the secondary crystal thing of 1wt%, three crystallisates, after heavily molten with saturated sodium carbonate solution, at 100 ℃, being concentrated into concentrated solution density is 1.42, again in 90 ℃ of recrystallizations, crystallization time 180 minutes, filters, and obtains recrystallization thing 550kg, in recrystallization thing, arsenic content reaches 0.77wt%, and filtrated stock can be used for continuing to process the crystalline alkali that arsenic content is greater than 1wt%.
Claims (9)
1. antimony is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, comprises the following steps:
(1) leach liquor after de-antimony is placed in to condensing crystal tank, at 100 ℃, concentrates, when concentrated solution density reaches 1.36-1.40, stop concentrating, at 80-100 ℃, carry out crystallization, filter, obtain primary crystallization thing, first-time filtrate;
(2) first-time filtrate is concentrated for the second time at 100 ℃, when concentrated solution density reaches 1.42-1.45, stop concentrating, at 80-100 ℃, carry out crystallization, filter, obtain secondary crystal thing, secondary filtrate;
(3) secondary filtrate is concentrated for the third time at 100 ℃, when concentrated solution density reaches 1.50-1.55, stop concentrating, at 80-100 ℃, carry out crystallization, filter, obtain three crystallisates, three filtrates;
(4) by three filtrates 100 ℃ carry out the 4th time concentrated, in concentrated solution, during arsenic content >=80g/l, stop concentrating, then crystallisation by cooling, to 30-35 ℃, filters, and obtains four crystallisates, four filtrates;
(5) four filtrates are returned to lower batch of first-time filtrate or secondary filtrate and concentrated together, recycle; Arsenic content is greater than to primary crystallization thing, secondary crystal thing or three crystallisates of 1wt%, with saturated sodium carbonate solution heavy molten after, at 100 ℃, being concentrated into concentrated solution density is 1.42-1.45, then in 80-100 ℃ of crystallization, obtains arsenic content lower than the crystalline alkali of 1wt%.
2. antimony as claimed in claim 1 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (1), Tc is 86-95 ℃, crystallization time >=25 minute.
3. antimony as claimed in claim 1 or 2 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (2), Tc is 86-95 ℃, crystallization time >=20 minute.
4. antimony as claimed in claim 1 or 2 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (3), Tc is 86-95 ℃, crystallization time >=10 minute.
5. antimony as claimed in claim 3 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (3), Tc is 86-95 ℃, crystallization time >=10 minute.
6. antimony as claimed in claim 1 or 2 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (5), Tc is 86-95 ℃, crystallization time >=30 minute.
7. antimony as claimed in claim 3 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (5), Tc is 86-95 ℃, crystallization time >=30 minute.
8. antimony as claimed in claim 4 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (5), Tc is 86-95 ℃, crystallization time >=30 minute.
9. antimony as claimed in claim 5 is smelted the leach liquor arsenic alkali separation method after the de-antimony of soda ash type arsenic alkali slag, it is characterized in that, in step (5), Tc is 86-95 ℃, crystallization time >=30 minute.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210137936.XA CN102676809B (en) | 2012-05-07 | 2012-05-07 | Arsenic-alkali separation method for leaching agent after removing antimony from sodium carbonate type arsenic-alkali slag in antimony smelting process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210137936.XA CN102676809B (en) | 2012-05-07 | 2012-05-07 | Arsenic-alkali separation method for leaching agent after removing antimony from sodium carbonate type arsenic-alkali slag in antimony smelting process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102676809A CN102676809A (en) | 2012-09-19 |
| CN102676809B true CN102676809B (en) | 2014-04-09 |
Family
ID=46809354
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210137936.XA Active CN102676809B (en) | 2012-05-07 | 2012-05-07 | Arsenic-alkali separation method for leaching agent after removing antimony from sodium carbonate type arsenic-alkali slag in antimony smelting process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102676809B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102942197A (en) * | 2012-11-20 | 2013-02-27 | 锡矿山闪星锑业有限责任公司 | Arsenic alkali separation method for sodium arsenate composite salt |
| CN103526049B (en) * | 2013-10-30 | 2015-09-09 | 四川鑫龙碲业科技开发有限责任公司 | The method of a kind of pyrometallurgical smelting antimony arsenic removal |
| WO2015113141A1 (en) | 2014-01-31 | 2015-08-06 | Goldcorp Inc. | Process for separation of at least one metal sulfide compristng arsenic and/or antimony from a mixed sulfide concentrate |
| CN104818387B (en) * | 2015-04-22 | 2017-03-29 | 南昌航空大学 | A kind of method of sodium salt in separating-purifying arsenic alkaline slag |
| CN111118301B (en) * | 2019-12-31 | 2020-11-27 | 焱鑫环保科技有限公司 | Method for recycling arsenic slag resources by arsenic and alkali in freezing separation alkali slag water leaching solution |
| CN115491495B (en) * | 2022-09-17 | 2024-07-05 | 湖南省和清环境科技有限公司 | Harmless and recycling wet treatment process for arsenic alkali residues |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1594090A (en) * | 2004-06-23 | 2005-03-16 | 柳州华锡集团有限责任公司 | Method for separating and recovering sodium arsenate and alkali by fractional crystallization method |
| CN102199708A (en) * | 2011-05-18 | 2011-09-28 | 南昌航空大学 | Method for treating arsenic-alkali residue generated in antimony smelting |
-
2012
- 2012-05-07 CN CN201210137936.XA patent/CN102676809B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1594090A (en) * | 2004-06-23 | 2005-03-16 | 柳州华锡集团有限责任公司 | Method for separating and recovering sodium arsenate and alkali by fractional crystallization method |
| CN102199708A (en) * | 2011-05-18 | 2011-09-28 | 南昌航空大学 | Method for treating arsenic-alkali residue generated in antimony smelting |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102676809A (en) | 2012-09-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102676809B (en) | Arsenic-alkali separation method for leaching agent after removing antimony from sodium carbonate type arsenic-alkali slag in antimony smelting process | |
| CN101691239B (en) | Comprehensive utilization method for bittern | |
| KR20190082167A (en) | A method for producing nickel sulfate, manganese, lithium, cobalt and cobalt oxide from battery waste | |
| CN104099474B (en) | A kind of electroplating sludge recycles technique | |
| CN107151746A (en) | The alkaline process handling process of lithium ore | |
| CN101899582A (en) | Method for extracting vanadium pentoxide from vanadium slag | |
| CN110004294B (en) | Method for treating scheelite alkali decomposition slag | |
| CN105803483B (en) | A kind of preparation method of electro deposited nickel, cobalt | |
| CN105274359B (en) | Method for extracting and separating valuable metals from secondary lead smelting slag | |
| CN102199708A (en) | Method for treating arsenic-alkali residue generated in antimony smelting | |
| CN108396158A (en) | A kind of processing method of the complex salt crystal object of electrolytic manganese process | |
| CN102701263B (en) | Method for preparing copper sulfate in mode that stanniferous copper slag is leached in selective mode and free of evaporation | |
| CN110143604A (en) | A kind of method of alkali, selenium and arsenic in recycling antimony smelting arsenic alkali slag | |
| CN106745289A (en) | A kind of production method of new-energy automobile power battery positive electrode manganese sulfate | |
| CN102674466A (en) | New process of utilizing manganese waste liquid to produce manganese sulfate | |
| CN101338365B (en) | Synthesizing method for molybdenum-nickel ore | |
| CN111500864A (en) | Method for recycling electroplating sludge based on chromium recovery | |
| CN109402408A (en) | A method of recycling valuable metal from Bellamya aeruginosa | |
| CN113816399A (en) | Method for recycling NaCl and recycling Fe, Mn and Mg resources in titanium slag | |
| CN113880149B (en) | Process for preparing high-purity nickel sulfate by taking ammonium salt-containing crude nickel sulfate as main raw material in copper electrolysis plant | |
| CN102602993A (en) | Method for recovering zirconium element from zirconium oxychloride crystallized mother liquor raffinate | |
| CN104773748A (en) | Method for preparing low-iron polyaluminium sulfate by using aluminiferous waste sulfuric acid mother liquor | |
| CN109336141B (en) | Method for improving recovery rate of lithium in wastewater | |
| CN105948084B (en) | A kind of method that magnesium sulfate monohydrate is produced using copper tailing as raw material | |
| CN112553468B (en) | Method for producing high-purity manganese sulfate by adopting metal manganese anode mud |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |