CN1019317B - Method of iron removing in the process of cadmium extraction - Google Patents
Method of iron removing in the process of cadmium extractionInfo
- Publication number
- CN1019317B CN1019317B CN88103877A CN88103877A CN1019317B CN 1019317 B CN1019317 B CN 1019317B CN 88103877 A CN88103877 A CN 88103877A CN 88103877 A CN88103877 A CN 88103877A CN 1019317 B CN1019317 B CN 1019317B
- Authority
- CN
- China
- Prior art keywords
- cadmium
- solution
- copper
- sections
- value
- 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.)
- Expired
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)
Abstract
The present invention relates to a ferrum removing method depositing oxidized ferrous ions in a solution in a goethite mode by using oxygen in the air and copper ions in a system as oxidizing agents in the process of extracting cadmium by a wet method using copper-cadmium residue as raw material. The method can fully utilize the existing equipment and can be operated in conventional acidity and at middle temperature. Compared with the prior art, the present invention saves potassium permanganate, copper sulphate and industrial oxygen, has the characteristics of low consumption, low cost, high purifying degree, high product quality, high recovery rate of metal, good performance of iron slag removal and filtration, etc., and radially eliminates arsenic contamination in the system; the concentration of arsenic hydride for fieldwork is lower than that of the national specified limitation.
Description
The present invention is a kind of in the process of wet method extraction cadmium; utilize oxygenant to make after the ferrous ion oxidation in the solution method for removing iron with the coprecipitation of impurity arsenic; belong to purification and environmental protection technical field in the hydrometallurgy, especially suiting at clean melt cinder of wet-process zinc metallurgy-copper-cadmium slag is that raw material extracts in the Production Flow Chart of cadmium and uses.
What extract the cadmium employing from copper-cadmium slag is wet processing, and its main process has: (1) oxidation copper-cadmium slag makes it easy dissolving; (2) leach copper-cadmium slag with acid-containing solution; (3) from leach supernatant liquor, replace Spongy Cadmium; (4) dissolving again (liquid making) of Spongy Cadmium; (5) electrolytic deposition process of cadmium; (6) remelting of cadmium and refining.The composition of copper-cadmium slag is relevant with the clean liquid method and the clean liquid degree of depth thereof that Zn system adopts, but it is general except containing a large amount of zinc, copper and cadmium, also contain impurity such as a spot of arsenic, antimony, iron, cobalt, in the acidleach process, can both enter solution and cause trouble, therefore need remove respectively to carrying cadmium.The work of deironing is generally finished in cadmium leaching and cadmium liquid making operation in the solution, and impurity arsenic antimony is removed together with iron usually.What the cadmium of great majority refining both at home and abroad producer adopted is that traditional Manganse Dioxide or potassium permanganate oxidation removes iron processes, and what introduce among the special public clear 57-53853 of the 546th～549 page of volume and Japanese Patent in the 246th～247 page of " copper-lead-zinc smelting design aids " (metallurgical industry press in June, 1978 version) of " heavy metal metallurgy " (metallurgical industry press in February, 1981 version) volume two is exactly this method.Though adopt this method for removing iron can reach the deironing requirement, thereby the easy reduction of iron influences the new liquid quality of cadmium in the operation afterwards.Have in addition that raw materials consumption is big, production cost is high, labour intensity is big, quality product is low, metal recovery rate is low and operating environment is seriously polluted, shortcomings such as the solution strainability is bad, especially under the strong oxidation of Manganse Dioxide and potassium permanganate, impurity arsenic in the copper-cadmium slag sharply enters solution, particularly when handling Zn system with the copper-cadmium slag of the clean liquid output of arsenic salt method especially like this.Utilize the glue three water iron oxide precipitations that form after the ferrous ion oxidation to come arsenic-adsorbing not thorough, it is too high to cause cadmium supernatant liquor after the liquid-solid separation to contain arsenic, severe contamination arsine gas concentration severe overweight in the air at whole cadmium system job scene, domestic certain cadmium system of factory is when adopting traditional Manganse Dioxide and potassium permanganate process deironing, and the pernicious intoxication accident of hydrogen arsenide often takes place.
The refining cadmium producer that also has is an oxygenant with oxygen and copper sulfate, and the ferrous ion oxidation is removed.Introduce a kind of copper-cadmium slag of industrial oxygen iron removal by oxidation that adopts on the 12nd～16 page of the 5th phase of " non-ferrous metal " nineteen eighty-three and comprehensively reclaimed novel process, its purpose be in view of copper-cadmium slag dissolution rate under normal condition low, consumption is than the shortcoming of multi-oxidizer, step-down acid normal temperature leaches and is the leaching of high temperature peracid, industrial oxygen iron removal by oxidation and the comprehensive valuable metal that reclaims in the copper-cadmium slag, the technical qualification of its iron removal are:
1. cadmium leaching process
Initial solid-to-liquid ratio 1: 2, beginning acid: 250～280g/l, temperature: more than 95 ℃, the time: 2 hours.Being neutralized to the pH value with slag charge is 1～2, and being diluted to solid-to-liquid ratio is 1: 4, continues heating 1 hour, is neutralized to pH value 5～5.2 with zinc oxide paste again hydrolytic precipitation such as germanium gallium copper is separated with zinc, cadmium, adds press filtration behind No. 3 flocculation agent.Leach liquor is transferred about pH to 2 with acid, is heated to 60～70 ℃ of stirrings, adds to make it oxidation after the heavy cadmium of zinc powder filters.Displaced liquid is heated to more than 95 ℃, add copper sulfate 1～3g/l, blast industrial oxygen and carry out iron removal by oxidation, the pH value of solution value is 4～4.5, reacted 1～2 hour, (as contain ferrous Gao Kezai add potassium permanganate) press filtration immediately after checking iron-free, liquid returns Zn system after the deironing, and scum is sent to the production iron oxide red.
2. Spongy Cadmium dissolution process
Solid-to-liquid ratio: 1: 1, beginning acid: 450～500g/l, temperature: more than 95 ℃, stir: 2～3 hours, add fresh Spongy Cadmium copper removal and fall acid, be diluted to solid-to-liquid ratio 1: 3 behind the no copper, endpoint pH is 3～4, and pH=4 is transferred in the back, adds potassium permanganate deironing (0.2～0.3kg/m under heating condition
3), transfer pH to 5～5.2 again after looking into iron-free, add No. 3 flocculation agent press filtrations, the Lu slag returns leaching, and Lu liquid send cadmium electrodeposition operation.
Still there is following point in method for removing iron in this comprehensive recycling process:
1, still need consume the potassium permanganate oxidant of some amount;
2, need in the cadmium system, add copper sulfate from the outside and expend a large amount of industrial oxygens;
3, the form of Lu slag does not obtain changing, and its strainability is still bad;
4, need high temperature between the deironing operational period, certainly will cause energy consumption to increase;
5, changed the common process of cadmium factory, existing installation can't satisfy the highly acid processing requirement of high temperature;
6, fail to solve arsenic evil problem at all, take place may still existing of the pernicious poisoning of hydrogen arsenide in the operation process.
The objective of the invention is to improve the above-mentioned deficiency of prior art, and provide a kind of potassium permanganate strong oxidizer that need not consume, do not need to add the method for removing iron of copper sulfate to system, making full use of existing installation and the routine operation condition is being changed under the little situation, by changing the form of removing scum, improve the strainability of solution and solve the arsenic evil that operation process produces.
Purpose of the present invention is achieved by following approach.Be that raw material extracts in the wet process of cadmium with clean melt cinder of wet-process zinc metallurgy-copper-cadmium slag promptly, utilize the characteristics of " high-copper hangs down iron " in the cadmium solution, blast inherent bivalent cupric ion in oxygen in the dispersion air in the solution and the solution by former pneumatic blending equipment fully, the acidity of control solution will form FeooH form precipitation after the ferrous ion oxidation in the solution.Because the FeooH that generates has good strainability and impurity arsenic, antimony are had the intensive adsorption, along with the precipitation of FeooH, impurity arsenic, antimony also sink in the slag in the lump and are exhausted from system.
The technological operation condition of the method for removing iron that the present invention provides is:
Cadmium leaches operation
Temperature: 60 ℃, the operational cycle: 4～5 hours, beginning acid: 120～150g/l, charging hop count; Be at least three sections.Stop to add copper-cadmium slag and carry out air blast and stir the residual acid of neutralization when the pH of solution value is 2～3, endpoint pH is 4.5～4.7 back press filtrations, contains cadmium filtrate and adds zinc powder and replace under normal condition and separate out Spongy Cadmium;
Cadmium liquid making operation
Temperature: 75～85 ℃, the operational cycle: 7～9 hours, beginning acid: 280～330g/l, charging hop count; Be at least three sections.When solution contains sour 5g/l, stop to add Spongy Cadmium, and air blast stir the residual acid of neutralization to terminal pH value be 5.0～5.5 back press filtrations, filtrate air blast stirring is once more removed copper and trace iron.
For realizing purpose of the present invention, the primitive reaction formula of removing with pyrrhosiderite form precipitation after utilizing oxygen and cupric ion with the ferrous ion oxidation in the cadmium system is:
Influencing the factor that above-mentioned reaction forward carries out has: the concentration of ferrous ion in the solution, the concentration of oxygen molecule, the pH value of the concentration of cupric ion and solution.
Wherein the concentration of oxygen is bigger, and speed of response is faster.When iron protoxide the concentration that improves oxygen in the solution, produce superfine little bubble after should making air spray go into solution as far as possible, execute-in-place can adopt compress wind directly to stir, the also mode that can adopt mechanical stirring to combine with pneumatic blending, for example compress wind is delivered to below the rotating disk turbine type stirring arm earlier, disperseed raising air utilization coefficient thereby whereby air is sheared with strong wind one's intention as revealed in what one says pipe.Help the formation of pyrrhosiderite though temperature raises, reduced air in solution solubleness and increased energy consumption.Therefore implement the method for removing iron that the present invention provides, can carry out in the mode that moderate temperature (60～90 ℃) adopts mechanical stirring to combine with the air blast pneumatic blending down.
Bivalent cupric ion concentration is also relevant with speed of response in the solution, experiment is learnt, bivalent cupric ion is 1: 1 o'clock with the ratio of the numerical value of ferrous ion concentration, with the atmospheric oxidation ferrous ion for up to 10 hours, when the ratio of numerical value is at least 3: 1, could shorten the time of atmospheric oxidation ferrous ion.Therefore implement the method for removing iron that the present invention provides, require that the ratio of bivalent cupric ion and the numerical value of ferrous ion concentration was at least 3: 1 in the solution.And when cadmium leached with liquid making operation deironing operation, the ratio of inherent bivalent cupric ion and the numerical value of ferrous ion concentration was generally all on 3: 1 in the solution, and therefore implementing the method for removing iron that the present invention provides does not need to add copper sulfate by the outside in system.
The pH value and the speed of response relation of solution are very big.When pH value＜1.9, ferrous ion in the solution is hardly by airborne oxygen oxidation, have only when pH value＞3.0, reaction (1) just is able to actual carrying out, equally, when pH value＜2.5, reaction (2) can reverse carrying out, have only pH value＞2.5 o'clock, the bivalent cupric ion in the solution just can the direct oxidation ferrous ion.Therefore implement the method for removing iron that the present invention provides, the pH during the air blast iron protoxide should keep greater than 3.0 at least.
In order to realize purpose of the present invention better, the form that requires gained to remove iron in the scum is the pyrrhosiderite form, but finds in test often to be mixed with in the slag of Lu three water iron oxide precipitation things, causes the strainability fundamental turn for the better of failing.This is because in the prior art copper-cadmium slag or the Spongy Cadmium that adds all had a preoxidation process, make ferrous part or most of high ferro form that is oxidized in copper-cadmium slag or the Spongy Cadmium, in leaching or liquid making process, the inherent ferric ion is difficult to directly form pyrrhosiderite form iron precipitation in the solution, when the pH value of solution value raises, at first be hydrolyzed to three water iron oxide precipitations.Therefore for realizing the method for removing iron that the present invention provides better, should change the practice of pre-oxidation copper-cadmium slag in the prior art, accomplish that raw material does not land, not oxidation, to keep the fresh state of copper-cadmium slag.In order not influence the leaching of cadmium, can slightly do improvement to common process, adopting increases the charging hop count, and the way that shortens feed time and prolongation reaction churning time solves.In the present invention, the copper-cadmium slag that require to add is inoxidized fresh feed, and reinforced hop count is at least three sections, and wherein the solution acidity of each segment endpoint is controlled to be during sectional feeding:
One section acidity: 55～65g/l
Two sections acidity: 25～35g/l
Three sections acidity: pH value=2～3
The air blast churning time that stops to add behind the copper-cadmium slag should be 3 hours at least, and the pH value of solution remained on 3.2～4.2 when air blast was stirred, and required the reinforced hop count of the Spongy Cadmium of adding to be at least three sections, and wherein the solution acidity of each segment endpoint is controlled to be during sectional feeding:
One section acidity: 150～180g/l
Two sections acidity: 80～120g/l
Three sections acidity: 5～10g/l
The air blast churning time that stops to add behind the Spongy Cadmium should be 3 hours at least, and the pH value of solution remained on 3.2～4.2 when air blast was stirred.
The present invention compared with prior art has following advantage: (following column of figure is a mean value)
One, improved the quality of cadmium supernatant liquor, contained arsenic and be reduced to 0.059g/l by original 0.31g/l, purified the degree of depth and improve 80%, iron content is reduced to 0.25g/l by original 0.33g/l, purifies the degree of depth and improves 32%;
Two, improved the quality of the new liquid of cadmium, iron content is reduced to 0.0057g/l by original 0.083g/l, purifies the degree of depth and improves 93%;
Three, the quantity of slag reduces, and slag contains zinc to be reduced, and the slag rate reduces 7～8%, and slag contains zinc and reduces by 30%;
Four, the quality of separating out of cadmium improves, and is that No. two cadmiums are upgraded to whole product single-minded cadmiums by original part, and product can export and exchange;
Five, electrolysis waste solution contains cadmium reduction by 20%, reduces the consumption of displacement zinc powder;
Six, the Lu performance of crossing of Lu slag improves, and operator's labour intensity can reduce by 60%;
Seven, environmental pollution is light, has properly settled the arsenic evil problem in the leaching process, and hydrogen arsenide concentration is lower than state specified standards in the operating environment, thereby has stopped the generation of pernicious hydrogen arsenide poisoning accident.
Embodiment 1
Copper-cadmium slag is formed: (%) Zn:40～45; Cd:3～5; Cu:4～5; Fe:0.8～1.0; As:0.1～0.5; Sb＜0.05; Co:0.1～0.2.
The technological operation condition of cadmium leaching process is:
Temperature: 60 ℃
Operational cycle: 4 hours
Beginning acid: 120g/l
Charging hop count: three sections
Segmentation adds copper-cadmium slag, and two section feedings were to acidity 25g/l after a section feeding was seen copper to acidity 55g/l, and three section feedings to pH value of solution value is 2 behind goodbye copper, stops charging and air blast and stirs 3 hours, and the air blast blast is 2Kg/cm
2, the pH value of solution remains 3.2～3.5, the ratio of cupric ion and the numerical value of ferrous ion concentration satisfies 3～5: 1 requirement, with in the milk of lime and residual acid to terminal pH value be 4.5 press filtrations afterwards, filtrate adds zinc powder and sinks cadmium, filter residue and send the copper system handles.
The technological operation condition of cadmium liquid making process is:
Temperature: 75 ℃
Operational cycle: 7 hours
Beginning acid: 280～290g/l
Charging hop count: three sections
Segmentation adds Spongy Cadmium, and each segment endpoint acidity is: one section acidity 155g/l, and two sections acidity 85g/l, three sections acidity 10g/l when three section feedings during to 10g/l, stop charging, carry out air blast and stir 3 hours, and the air blast blast is 2 kilograms/cm
2The pH value of solution remains on 3.2～3.5, cupric ion satisfies 3～5: 1 requirement with the ratio of the numerical value of ferrous ion concentration, with pressing the Lu in pH5.0～5.2 backs to terminal with residual acid in the milk of lime, filtrate press filtration after copper removal and trace iron are stirred in air blast, filtrate is sent cadmium electrodeposition operation, and the Lu slag returns cadmium and leaches operation.
Experimental result, compared with the prior art, iron level reduces by 20% in the cadmium supernatant liquor, and arsenic content reduces by 70%, and on-the-spot hydrogen arsenide concentration is reduced to 0.3mg/m
3Below (past 3mg/m
3), iron level reduces by 80% in the new liquid of cadmium, and the slag rate reduces 7%, and slag contains zinc and reduces by 20%, and electrolysis waste solution contains cadmium and reduces by 12%, and product is the single-minded cadmium, and labour intensity reduces by 50%.
Embodiment 2
The fresh copper-cadmium slag of oxidation not, its composition is identical with embodiment 1.
The technological operation condition that cadmium leaches operation is:
Temperature: 60 ℃
Operational cycle: 5 hours
Beginning acid: 135g/l:
Charging hop count: three sections
One section acidity: 60g/l, two sections acidity: 30g/l, three sections acidity: pH value=2.5, stop expecting back air blast stirring 3.5 hours, the air blast blast is identical with example 1, and the pH value of solution value keeps 3.6～3.8 during stirring, cupric ion satisfies 5: 1 requirement with the ratio of the numerical value of ferrous ion concentration, with in the milk of lime and residual acid pH value 4.7 back press filtrations to terminal, Lu liquid send down operation to replace Spongy Cadmium, and the Lu slag send the copper system.
The technological operation condition of cadmium liquid making process is:
Temperature: 80 ℃
Operating time: 8.5 hours
Beginning acid: 320g/l
Charging hop count: three sections
One section acidity: 170g/l, two sections acidity: 100g/l, three sections acidity: 5g/l, stop charging after, air blast was stirred 4 hours, the air blast blast is identical with example, and the pH value of solution remains on 3.6～3.8, and cupric ion satisfies 5: 1 requirement with the ratio of the numerical value of ferrous ion concentration, with in the milk of lime and residual acid pH5.2～5.4 back press filtrations to terminal, filtrate press filtration after copper removal and trace iron are stirred in air blast, filtrate is sent the cadmium electrodeposition, and the Lu slag returns cadmium and leaches.
Experimental result, compared with the prior art, iron level reduces by 30% in the cadmium supernatant liquor, and arsenic content reduces by 80%, and on-the-spot hydrogen arsenide concentration is reduced to 0.3mg/m
3Below, iron level reduces by 90% in the new liquid of cadmium, and the slag rate reduces 7%, and slag contains zinc and reduces by 30%, and electrolysis waste solution contains cadmium and reduces by 18%, and all prods is the single-minded cadmium, and labour intensity reduces by 50%.
Embodiment 3
Fresh copper-cadmium slag is not crossed in oxidation, and its composition is identical with example 1.
The technological operation condition of cadmium leaching process is:
Temperature: 60 ℃
Operational cycle: 5 hours
Beginning acid: 145g/l
Charging hop count: three sections
One section acidity: 65g/l, two sections acidity: 35g/l, three sections acidity: pH value=3.Stop expecting back air blast stirring 4 hours, the air blast blast is identical with example 1, and the pH value of solution value remains on 4.0～4.2 during stirring, and all the other conditions are identical with example 2.
The technological operation condition of cadmium liquid making process:
Temperature: 85 ℃
Operational cycle: 9 hours
Beginning acid: 330g/l
Charging hop count: three sections
One section acidity: 180g/l, two sections acidity: 110g/l, three sections acidity: 5g/l.The stirring that stops after the charging is 4.5 hours, and the air blast blast is identical with example 1, and pH value of solution keeps 4.0～4.2, and all the other conditions are identical with example 2.
Experimental result, compared with the prior art, iron level reduces by 35% in the cadmium supernatant liquor, and arsenic content reduces by 85%, and on-the-spot hydrogen arsenide concentration is reduced to 0.3mg/m
3Below, iron level reduces by 88% in the new liquid of cadmium, and the slag rate reduces 8%, and slag contains zinc and reduces by 32%, and electrolysis waste solution contains cadmium and reduces by 22%, and all prods is the single-minded cadmium, and labour intensity reduces by 55%.
Claims (7)
1, a kind of is being that raw material extracts in the wet process of cadmium with clean melt cinder of wet-process zinc metallurgy-copper-cadmium slag, with airborne oxygen and bivalent cupric ion is oxygenant, with the sedimentary method for removing iron of ferrous ion oxidation posthydrolysis in the solution, it is characterized in that the ratio of inherent bivalent cupric ion and the numerical value of ferrous ion concentration was at least 3: 1 in the solution, will after the ferrous ion oxidation be with the sedimentary technical qualification of pyrrhosiderite form:
Cadmium leaches operation
Temperature: 60 ℃
Operational cycle: 4～5 hours
Beginning acid: 120～150g/l
Charging hop count: be at least three sections
When the pH of solution value is 2～3, stop to add copper-cadmium slag, and air blast stirs the residual acid of neutralization, endpoint pH is 4.5～4.7 back press filtrations, filtrate adds zinc powder and replaces under normal condition and separate out Spongy Cadmium;
Cadmium liquid making operation
Temperature: 75～85 ℃
Operational cycle: 7～9 hours
Beginning acid: 280～330g/l
Charging hop count: be at least three sections
When solution contains sour 5g/l, stop to add Spongy Cadmium, and the residual acid of air blast stirring neutralization 5.0～5.5 back press filtrations to terminal, filtrate air blast is once more stirred copper removal and trace iron.
2, according to the said method for removing iron of claim 1, the copper-cadmium slag that it is characterized in that adding in the cadmium leaching operation is the fresh feed of end through oxidation.
3, according to claim 1 or 2 said method for removing iron, each segment endpoint solution contains acid and is when it is characterized in that adding copper-cadmium slag:
One section: 55～65g/l
Two sections: 25～35g/l
Three sections: pH value=2～3
4, according to the said method for removing iron of claim 3, the air blast churning time that it is characterized in that stopping to add behind the copper-cadmium slag should be 3 hours at least, and the pH value of solution maintains 3.2～4.2.
5, according to the said method for removing iron of claim 1, each segment endpoint solution contains acid and is when it is characterized in that adding Spongy Cadmium:
One section: 150～180g/l
Two sections: 80～120g/l
Three sections: 5～10g/l
6, according to claim 1 or 5 said method for removing iron, the air blast churning time that it is characterized in that stopping to add behind the Spongy Cadmium should be 3 hours at least, and the pH value of solution maintains 3.2～4.2.
7,, it is characterized in that the technical qualification of deironing are according to the said method for removing iron of claim 1:
Cadmium leaches operation:
Temperature: 60 ℃
Operating time: 5 hours
Beginning acid: 130～150g/l
Charging hop count: three sections
The acidity of each segment endpoint solution is during the fresh copper-cadmium slag that adds that not oxidised crosses:
One section: 60g/l
Two sections: 30g/l
Three sections: pH value=2.5
Air blast was stirred 3.5～4.0 hours after stopping to add copper-cadmium slag, the pH value of solution is maintained 3.6～3.8, cupric ion is 5: 1 with the ratio of the numerical value of ferrous ion concentration in the solution, be neutralized to endpoint pH 4.7 back press filtrations with milk of lime at last, contain cadmium filtrate and add zinc powder and under normal condition, replace and separate out Spongy Cadmium;
Cadmium liquid making operation
Temperature: 80～85 ℃
Operational cycle: 8.5～9 hours
Beginning acid: 320～330g/l
Charging hop count: three sections
The acidity of each segment endpoint solution is when adding Spongy Cadmium:
One section acidity: 170g/l
Two sections acidity: 100g/l
Three sections acidity: 5g/l
After stopping charging, air blast was stirred 4～4.5 hours, and the pH value of solution remains on 3.6～3.8, and cupric ion is 5: 1 with the ratio of the numerical value of ferrous ion concentration in the solution, use in the milk of lime at last and residual acid pH value 5.2～5.4 back press filtrations to terminal, filtrate air blast is once more stirred copper removal and trace iron.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN88103877A CN1019317B (en) | 1988-06-23 | 1988-06-23 | Method of iron removing in the process of cadmium extraction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN88103877A CN1019317B (en) | 1988-06-23 | 1988-06-23 | Method of iron removing in the process of cadmium extraction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1038843A CN1038843A (en) | 1990-01-17 |
| CN1019317B true CN1019317B (en) | 1992-12-02 |
Family
ID=4832806
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN88103877A Expired CN1019317B (en) | 1988-06-23 | 1988-06-23 | Method of iron removing in the process of cadmium extraction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1019317B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100494424C (en) * | 2007-08-31 | 2009-06-03 | 侯仁义 | Hydrogenation method for high-pure cadmium |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1069090C (en) * | 1998-09-09 | 2001-08-01 | 高文唐 | Comprehensive recovery method of wet-process zinc smelting liquid-cleaning slag |
| CN101967574B (en) * | 2010-11-29 | 2012-09-05 | 常州市新盛电器有限公司 | Method for reducing cadmium content in process of producing lead brass sectional materials |
| CN102249450B (en) * | 2011-05-11 | 2012-08-29 | 天津理工大学 | Method for removing trace cadmium from aqueous solution |
| CN102382980B (en) * | 2011-11-02 | 2013-04-17 | 郴州丰越环保科技股份有限公司 | Method for directly purifying cadmium from sponge cadmium |
| CN102517455A (en) * | 2011-12-29 | 2012-06-27 | 株洲冶炼集团股份有限公司 | Method for recovering cadmium from copper cadmium residues |
| CN106521555B (en) * | 2016-11-02 | 2018-04-20 | 中南大学 | A kind of method of antimony electrolyte selectivity iron removaling |
| CN106498442B (en) * | 2016-11-02 | 2018-04-10 | 中南大学 | A kind of antimony electrolyte selectivity iron removaling and the method for preparing ferrous oxalate |
| CN108913910A (en) * | 2018-07-18 | 2018-11-30 | 河南金利金铅集团有限公司 | A kind of method that lead smelts the recycling of bottom convertor cigarette ash cadmium metal |
| CN110819807B (en) * | 2019-08-23 | 2021-03-19 | 中国东方电气集团有限公司 | Recovery system and method for mercury cadmium telluride material |
-
1988
- 1988-06-23 CN CN88103877A patent/CN1019317B/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100494424C (en) * | 2007-08-31 | 2009-06-03 | 侯仁义 | Hydrogenation method for high-pure cadmium |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1038843A (en) | 1990-01-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1252293C (en) | Reduction of zinc oxide from complex sulfide concentrates using chloride processing | |
| CN1189578C (en) | Production of zinc oxide from complex sulfide concentrates using chloride processing | |
| CN102031381B (en) | Process for preparing sodium pyroantimonate from arsenic- and stibium-containing smoke ash | |
| CN102382980B (en) | Method for directly purifying cadmium from sponge cadmium | |
| CN105293564A (en) | Method for recycling zinc-containing dust ash in steel plant | |
| CN113684368A (en) | Method for co-processing arsenic sulfide slag and arsenic-containing smoke dust in copper smelting | |
| CN101871046A (en) | Method for recycling heavy metal pollution wastes | |
| CN1676634A (en) | Pressure oxidation leaching method for nickel-cobalt oxide ore | |
| CN106048217A (en) | Comprehensive recycling method for zinc oxide powder | |
| CN111647754A (en) | Comprehensive utilization method of zinc-containing dust and sludge in steel plant | |
| CN1019317B (en) | Method of iron removing in the process of cadmium extraction | |
| CN1239720C (en) | Method for producing high purity metal zinc from zinc oxide ore | |
| CN1253589C (en) | Method for wet zinc refining without iron slag | |
| CN113862464B (en) | Method for recovering copper and scattered metal in black copper sludge | |
| CN1133752C (en) | Direct zinc sulfide concentrate leaching-out process with coupled synergic leaching-out and solvent extraction and separation | |
| WO2023221907A1 (en) | Method for synchronously removing fluorine, chlorine and iron in solution | |
| CN1045796C (en) | Method for extracting gold, silver and valuable metals from high-arsenic copper anode mud | |
| CN113044815A (en) | Method and system for comprehensively treating selenium-tellurium-containing waste | |
| CN1236082C (en) | Wet method copper-extracting process | |
| CN113981217B (en) | Method for selectively separating copper, zinc and iron in low-grade complex chalcopyrite | |
| CN215667159U (en) | System for comprehensive treatment contains selenium tellurium waste material | |
| CN113528852B (en) | Production method for dearsenifying and deleading high-arsenic lead copper matte | |
| CN1048287C (en) | Process for direct extraction of sulfide mineral by combound catalytic oxidation | |
| CN1164775C (en) | Ammonium salt liquid phase oxidation direct leaching method for nonferrous metal sulfide mineral | |
| CN1238535C (en) | Process for separating antimoney from gold-antimoney ore using wet metallurgical technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C13 | Decision | ||
| GR02 | Examined patent application | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |