CN108277357B - A kind of method of steel works sintering head dedusting ash separation and recovery silver and lead - Google Patents
A kind of method of steel works sintering head dedusting ash separation and recovery silver and lead Download PDFInfo
- Publication number
- CN108277357B CN108277357B CN201810099938.1A CN201810099938A CN108277357B CN 108277357 B CN108277357 B CN 108277357B CN 201810099938 A CN201810099938 A CN 201810099938A CN 108277357 B CN108277357 B CN 108277357B
- Authority
- CN
- China
- Prior art keywords
- lead
- silver
- sections
- dedusting ash
- section
- 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
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/02—Working-up flue dust
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet processes
- C22B11/042—Recovery of noble metals from waste materials
- C22B11/044—Recovery of noble metals from waste materials from pyrometallurgical residues, e.g. from ashes, dross, flue dust, mud, skim, slag, sludge
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B13/00—Obtaining lead
- C22B13/04—Obtaining lead by wet processes
- C22B13/045—Recovery from waste materials
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
-
- 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
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Organic Chemistry (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention relates to a kind of methods of steel works sintering head dedusting ash separation and recovery silver and lead, belong to resource comprehensive utilization technical field.Sintering machine head end dedusting ash is uniformly mixed with ammonium carbonate first, adds water to size mixing and is leached to obtain lead silver enrichment slag；Ammonium chloride is added into obtained lead silver enrichment slag, and sodium chlorate or hypochlorite oxidation agent carry out two sections of counter flow oxidations and leach, one section of obtained leachate is using metallic lead displacement recycling silver, output sponge silver and displaced liquid, for displaced liquid using crystallisation by cooling output lead chloride, crystalline mother solution returns to two sections of leachings；Two sections are leached two sections of obtained leachates and return to one section of leaching.The invention firstly uses ammonium carbonates as transforming agent and leaching agent, by in material lead and silver be converted into ceruse and silver carbonate, simultaneously by the harmful elements separated and dissolved such as soluble zinc, potassium, sodium and chlorine, these foreign ions are avoided to the adverse effect of lead silver package etc., and these impurity is avoided to be enriched in leaching finishing slag.
Description
Technical field
The present invention relates to a kind of methods of steel works sintering head dedusting ash separation and recovery silver and lead, belong to resource comprehensive and return
Receive technical field.
Background technique
The steel and iron industry production in China mainly uses " blast furnace ironmaking-oxygen top blown converter steel making " process flow.Iron ore
Sintering is the important link in steel production.Sintering machine head end dedusting ash is that the sintering flue gas of iron ore sintering head output passes through electricity
The dust that deduster is collected, yield account for about the 2% ~ 4% of Sintering Yield, the annual resulting dedusting ash total amount in the whole nation
It is 15,000,000 tons or so.The pollution control of sintering machine head end dedusting ash and valuable resource synthetical recovery are major iron and steel enterprise's energy-saving and emission-reduction
Important topic.
Currently, most of steel plant are directly incorporated sintering feed using sintering flue gas dedusting ash as Iron Ore Powder again.This method
It can use iron and carbon in dedusting ash, realizing the synthetical recovery of iron and carbon, but valuable metal lead and silver cannot be returned
It receives；Simultaneously because separating treatment is not carried out to blast furnace harmful element to zinc contained therein, alkali metal, chlorine element etc., so that
Continuous circulation collection during the sintering of these objectionable impurities elements and blast furnace ironmaking, influences the normal production of iron and steel enterprise, together
When also bring new environmental issue.
Currently, the reported method for recycling valuable metal from sintering machine head end dedusting ash and separating harmful element is mainly
Recycle the elements such as potassium, sodium and iron." the side of sintering machine head end dedusting ash extraction k-na salt that patent application 201410397569.6 provides
Method " is to mix sintering machine head end ash with distilled water, and suds are added and are dispersed, by leaching, removal of impurities, filtering is evaporated
Etc. processes, obtain k-na salt.This method simple process, but it is unable to comprehensive recovery of lead and silver.Patent application 201410248826.X
" a kind of technique and system for removing alkali metal in smelting iron and steel dedusting ash " provided, is to mix smelting iron and steel dedusting ash with water
It sizes mixing, carries out water logging, recycle the existing concentration in dressing plant and filter plant to carry out thickening filtration, it is former to obtain 12% ~ 15% sintering
Material.This method can effectively remove the alkali metal in dedusting ash, but lead silver cannot recycle.Patent application 201610791064.7
There is provided " a method of iron ore concentrate and non-ferrous metal are recycled using sintering machine head end ash ", it is that sintering machine head end ash is sized mixing with water,
By gravity separation, low intensity magnetic separation, closed circuit flotation, lead concentrate and non-ferrous metal enriched substance are obtained.This method can recycle
Iron ore concentrate, and the enriched substance of non-ferrous metal is obtained, but be unable to output nonferrous metal product.Patent application 201410048263.X is public
Open " from steel works sintering dust recycle silver, copper and zinc method ", be will be sintered ash carry out first washing remove it is therein can
Molten alkali metal, then using ammonium hydroxide complexing extraction, obtained argentiferous ammonia, cuprammonium, zinc ammonia complex mixed solution use formaldehyde again
Or acetaldehyde reduction recycling silver.This method is able to achieve the synthetical recovery of silver, copper and zinc, but it is complexed under conditions of pH is 10 ~ 13
Extraction, ammonia volatilization is serious, severe operational environment, and as reducing agent, there are security risks using formaldehyde or acetaldehyde.
Therefore, new technique and process flow are developed, realizes the synthetical recovery and nocuousness of lead silver in sintering machine head end dedusting ash
The separation of element, it has also become the important technology problem that iron and steel enterprise faces.
Summary of the invention
For the above-mentioned problems of the prior art and deficiency, the present invention provides a kind of steel works sintering head dust setting ash
Method from recycling silver and lead.The invention firstly uses ammonium carbonates as transforming agent and leaching agent, by the lead and silver turn in material
Ceruse and silver carbonate are turned to, while by the harmful elements separated and dissolved such as soluble zinc, potassium, sodium and chlorine, avoiding these impurity
The adverse effect of ion pair lead silver package etc., and these impurity is avoided to be enriched in leaching finishing slag, leaching finishing slag can return
Sintered material.High, the high feature of product purity with lead silver comprehensive recovery.The invention is realized by the following technical scheme.
A kind of method of steel works sintering head dedusting ash separation and recovery silver and lead, specific steps include: that will burn first
Knot head dedusting ash is uniformly mixed with ammonium carbonate, is added water to size mixing and is leached to obtain lead silver enrichment slag；To obtained lead silver enrichment
Ammonium chloride and sodium chlorate are added in slag or hypochlorite oxidation agent carries out two sections of counter flow oxidations and leaches, one section of obtained leaching
Liquid is using metallic lead displacement recycling silver, output sponge silver and displaced liquid, displaced liquid using crystallisation by cooling output lead chloride,
Crystalline mother solution returns to two sections of leachings；Two sections are leached two sections of obtained leachates and return to one section of leaching.
Specific step is as follows:
Step 1, alkaline leaching: being that 1:1 ~ 4 are uniformly mixed and are mixed by sintering machine head end dedusting ash and ammonium carbonate in mass ratio
Material is closed, is that 1:2 ~ 8g/mL adds water to size mixing by solid-to-liquid ratio, is 25 DEG C ~ 95 DEG C in temperature, speed of agitator is 100r/min ~ 600r/
It is leached under conditions of min, controls reaction time 60min ~ 300min, slurry pH is 7.5 ~ 9.8, and liquid is solid after reaction
Isolated lead silver enrichment slag and alkaline leaching liquid；
Step 2, one section of leaching: it is that 1:1 ~ 4 mix that the lead silver that step 1 obtains is enriched with slag with ammonium chloride in mass ratio
It is even, it sizes mixing by two sections of leachates that solid-to-liquid ratio is 1:3 ~ 15g/mL addition step 3 output, is 60 DEG C ~ 120 DEG C in temperature, stirring
Revolving speed is leached under conditions of being 100r/min ~ 600r/min, and the control reaction time is 120min ~ 300min, slurry pH
It is 1.5 ~ 6.8, solid-liquor separation obtains one section of leachate and one section of leached mud after reaction；
Step 3, two sections of leachings: one section of leached mud and sodium chlorate that step 2 is obtained or hypochlorite oxidation agent are by quality
Than being mixed for 30 ~ 100:1, sizes mixing by the crystalline mother solution that solid-to-liquid ratio is 1:3 ~ 15g/mL addition step 5 output, be in temperature
50 DEG C ~ 90 DEG C, speed of agitator be 100r/min ~ 600r/min under conditions of leached, the control reaction time for 120min ~
300min, slurry pH are 1.0 ~ 6.0, and solid-liquor separation obtains two sections of leachates and leaches finishing slag after reaction, two sections of leachings
Liquid return step 2 is recycled；
Step 4, displacement recycling silver: will be added lead flake in one section of leachate that step 3 obtains, be 60 DEG C ~ 100 DEG C in temperature
Under conditions of react 60min ~ 300min, solid-liquor separation output sponge silver and displaced liquid；
Step 5, crystallisation by cooling recycle lead: the displaced liquid that step 4 is obtained cools, and lead chloride crystal seed is added,
Temperature stops 2 ~ 8 hours under the conditions of being 15 DEG C ~ 40 DEG C, and solid-liquor separation obtains lead chloride and crystalline mother solution, and crystalline mother solution returns to step
Rapid 3 are recycled.
20 ~ 45wt% of sintering machine head end dedusting ash iron content in the step 1, containing 0.1 ~ 3wt% of zinc, containing 3 ~ 20wt% of potassium, contain sodium
0.3 ~ 5wt%, 100 ~ 800g/t of argentiferous and leaded 3 ~ 22wt%.
The step 2 is added into 4 ~ 6mol/L ammonium chloride solution when leaching for the first time, and subsequent leach is added the two of step 3 output
Section leachate is sized mixing.
The step 2 and step 3 pH values of pulp are regulated and controled using hydrochloric acid and ammonium hydroxide.
Lead flake additional amount is the 3 ~ 10 of the Theoretical Mass for cementing out the silver in one section of leachate completely in the step 4
Times.
The beneficial effects of the present invention are:
(1) the invention firstly uses ammonium carbonates as transforming agent and leaching agent, by material lead and silver be converted into carbonic acid
Lead and silver carbonate, while by the harmful elements separated and dissolved such as soluble zinc, potassium, sodium and chlorine, these foreign ions are avoided to lead
The adverse effect of silver package etc., and these impurity is avoided to be enriched in leaching finishing slag, sintered material can be returned to by leaching finishing slag.
High, the high feature of product purity with lead silver comprehensive recovery.
(2) present invention realizes the efficiently leaching of lead and silver using two sections of counter flow oxidation leaching-out techniques in the condition less than 120 DEG C
Out, while the lead in reasonable temperature gradient crystallisation by cooling recycling solution is controlled, without traditional evaporative crystallization steps, with energy consumption
Low, at low cost, lead recovery is high, the feature that process cleans are efficient, environmental-friendly.
Detailed description of the invention
Fig. 1 is process flow chart of the invention.
Specific embodiment
With reference to the accompanying drawings and detailed description, the invention will be further described.
Embodiment 1
As shown in Figure 1, the method for the steel works sintering head dedusting ash separation and recovery silver and lead, the specific steps of which are as follows:
Step 1, alkaline leaching: by sintering machine head end dedusting ash (sintering machine head end dedusting ash iron content 25.3wt%, 0.5wt% containing zinc,
11.2wt% containing potassium, 0.7wt% containing sodium, argentiferous 421g/t and leaded 5.8wt%) it with ammonium carbonate is in mass ratio that 1:1 is uniformly mixed
To mixed material, it is that 1:2g/mL adds water to size mixing by solid-to-liquid ratio, is 60 DEG C in temperature, under conditions of speed of agitator is 400r/min
Leached, control reaction time 120min, slurry pH is that 9.2 ~ 9.5(uses concentration for the adjusting of 8mol/L ammonia spirit),
Solid-liquor separation obtains lead silver enrichment slag and alkaline leaching liquid after reaction；
Step 2, one section of leaching: the lead silver enrichment slag that step 1 obtains is uniformly mixed in mass ratio for 1:2 with ammonium chloride,
It sizes mixing by two sections of leachates that solid-to-liquid ratio is 1:3g/mL addition step 3 output, is 90 DEG C in temperature, speed of agitator 300r/
It is leached under conditions of min, the control reaction time is 180min, and slurry pH is that 3.5(pH values of pulp uses concentration for 8mol/L
Hydrochloric acid is adjusted), solid-liquor separation obtains one section of leachate and one section of leached mud after reaction；It is added when wherein leaching for the first time
4mol/L ammonium chloride solution, dosage is identical as two sections of leachate dosages of step 3 output, and step 3 output is added in subsequent leach
Two sections of leachates are sized mixing；
Step 3, two sections of leachings: the one section of leached mud and hypochlorite oxidation agent that step 2 is obtained are 100:1 in mass ratio
It is mixed, sizes mixing by the crystalline mother solution that solid-to-liquid ratio is 1:3g/mL addition step 5 output, be 60 DEG C in temperature, speed of agitator is
Leached under conditions of 300r/min, the control reaction time be 180min, slurry pH be 2.0(pH values of pulp use concentration for
8mol/L hydrochloric acid is adjusted), solid-liquor separation obtains two sections of leachates and leaches finishing slag, two sections of leachate return steps after reaction
2 are recycled；
Step 4, displacement recycling silver: lead flake is added in one section of leachate that step 3 is obtained, and (lead flake additional amount is by one section
5 times of the Theoretical Mass that silver in leachate cements out completely), 180min is reacted under conditions of temperature is 70 DEG C, liquid is solid
Separate output sponge silver and displaced liquid；
Step 5, crystallisation by cooling recycle lead: the displaced liquid that step 4 is obtained cools, and 10g lead chloride crystal seed is added,
It is stopped 5 hours under the conditions of temperature is 20 DEG C, solid-liquor separation obtains lead chloride and crystalline mother solution, and crystalline mother solution return step 3 is followed
Ring uses.
Above-mentioned sponge silver, the lead chloride rate of recovery silver-colored after detecting are 87.3%, and the rate of recovery of lead is 93.7%.
Embodiment 2
As shown in Figure 1, the method for the steel works sintering head dedusting ash separation and recovery silver and lead, the specific steps of which are as follows:
Step 1, alkaline leaching: sintering machine head end dedusting ash (sintering machine head end dedusting ash iron content 45wt%, 0.1wt% containing zinc, is contained
Potassium 3wt%, 5wt% containing sodium, argentiferous 800g/t and leaded 3wt%) it with ammonium carbonate is in mass ratio that 1:4 is uniformly mixed to obtain mixture
Material is that 1:8g/mL adds water to size mixing by solid-to-liquid ratio, is 25 DEG C in temperature, and speed of agitator is leached under conditions of being 100r/min,
Reaction time 300min is controlled, slurry pH is that 7.5(uses concentration for the adjusting of 8mol/L ammonia spirit), liquid is solid after reaction
Isolated lead silver enrichment slag and alkaline leaching liquid；
Step 2, one section of leaching: the lead silver enrichment slag that step 1 obtains is uniformly mixed in mass ratio for 1:1 with ammonium chloride,
It sizes mixing by two sections of leachates that solid-to-liquid ratio is 1:6g/mL addition step 3 output, is 60 DEG C in temperature, speed of agitator 100r/
It is leached under conditions of min, the control reaction time is 300min, and slurry pH is that 1.5(pH values of pulp uses concentration for 8mol/L
Hydrochloric acid is adjusted), solid-liquor separation obtains one section of leachate and one section of leached mud after reaction；It is added when wherein leaching for the first time
6mol/L ammonium chloride solution, dosage is identical as two sections of leachate dosages of step 3 output, and step 3 output is added in subsequent leach
Two sections of leachates are sized mixing；
Step 3, two sections of leachings: by one section of leached mud and sodium chlorate oxidant that step 2 obtains in mass ratio be 30:1 into
Row mixing sizes mixing by the crystalline mother solution that solid-to-liquid ratio is 1:10g/mL addition step 5 output, is 50 DEG C in temperature, speed of agitator is
Leached under conditions of 100r/min, the control reaction time be 300min, slurry pH be 1.0(pH values of pulp use concentration for
8mol/L hydrochloric acid is adjusted), solid-liquor separation obtains two sections of leachates and leaches finishing slag, two sections of leachate return steps after reaction
2 are recycled；
Step 4, displacement recycling silver: lead flake is added in one section of leachate that step 3 is obtained, and (lead flake additional amount is by one section
3 times of the Theoretical Mass that silver in leachate cements out completely), 300min is reacted under conditions of temperature is 60 DEG C, liquid is solid
Separate output sponge silver and displaced liquid；
Step 5, crystallisation by cooling recycle lead: the displaced liquid that step 4 is obtained cools, and 10g lead chloride crystal seed is added,
It is stopped 8 hours under the conditions of temperature is 15 DEG C, solid-liquor separation obtains lead chloride and crystalline mother solution, and crystalline mother solution return step 3 is followed
Ring uses.
Above-mentioned sponge silver, the lead chloride rate of recovery silver-colored after detecting are 90.2%, and the rate of recovery of lead is 87.8%.
Embodiment 3
As shown in Figure 1, the method for the steel works sintering head dedusting ash separation and recovery silver and lead, the specific steps of which are as follows:
Step 1, alkaline leaching: sintering machine head end dedusting ash (sintering machine head end dedusting ash iron content 20wt%, 3wt% containing zinc, is contained into potassium
20wt%, 0.3wt% containing sodium, argentiferous 100g/t and leaded 22wt%) it is in mass ratio that 1:2 is uniformly mixed and is mixed with ammonium carbonate
Material is that 1:6g/mL adds water to size mixing by solid-to-liquid ratio, is 95 DEG C in temperature, speed of agitator is soaked under conditions of being 600r/min
Out, reaction time 60min is controlled, slurry pH is that 8.2(use concentration to adjust for 8mol/L ammonia spirit), liquid after reaction
Gu isolated lead silver enrichment slag and alkaline leaching liquid；
Step 2, one section of leaching: the lead silver enrichment slag that step 1 obtains is uniformly mixed in mass ratio for 1:4 with ammonium chloride,
It sizes mixing by two sections of leachates that solid-to-liquid ratio is 1:15g/mL addition step 3 output, is 120 DEG C in temperature, speed of agitator 600r/
It is leached under conditions of min, the control reaction time is 120min, and slurry pH is that 6.8(pH values of pulp uses concentration for 8mol/L
Ammonium hydroxide is adjusted), solid-liquor separation obtains one section of leachate and one section of leached mud after reaction；It is added when wherein leaching for the first time
5mol/L ammonium chloride solution, dosage is identical as two sections of leachate dosages of step 3 output, and step 3 output is added in subsequent leach
Two sections of leachates are sized mixing；
Step 3, two sections of leachings: by one section of leached mud and sodium chlorate oxidant that step 2 obtains in mass ratio be 80:1 into
Row mixing sizes mixing by the crystalline mother solution that solid-to-liquid ratio is 1:15g/mL addition step 5 output, is 90 DEG C in temperature, speed of agitator is
Leached under conditions of 600r/min, the control reaction time be 120min, slurry pH be 6.0(pH values of pulp use concentration for
8mol/L ammonium hydroxide is adjusted), solid-liquor separation obtains two sections of leachates and leaches finishing slag, two sections of leachate return steps after reaction
2 are recycled；
Step 4, displacement recycling silver: lead flake is added in one section of leachate that step 3 is obtained, and (lead flake additional amount is by one section
10 times of the Theoretical Mass that silver in leachate cements out completely), 60min is reacted under conditions of temperature is 100 DEG C, liquid is solid
Separate output sponge silver and displaced liquid；
Step 5, crystallisation by cooling recycle lead: the displaced liquid that step 4 is obtained cools, and 10g lead chloride crystal seed is added,
It is stopped 2 hours under the conditions of temperature is 40 DEG C, solid-liquor separation obtains lead chloride and crystalline mother solution, and crystalline mother solution return step 3 is followed
Ring uses.
Above-mentioned sponge silver, the lead chloride rate of recovery silver-colored after detecting are 82.7%, and the rate of recovery of lead is 94.2%.
In conjunction with attached drawing, the embodiment of the present invention is explained in detail above, but the present invention is not limited to above-mentioned
Embodiment within the knowledge of a person skilled in the art can also be before not departing from present inventive concept
Put that various changes can be made.
Claims (4)
1. a kind of method of steel works sintering head dedusting ash separation and recovery silver and lead, it is characterised in that specific steps include: head
Sintering machine head end dedusting ash is uniformly mixed with ammonium carbonate first, adds water to size mixing and is leached to obtain lead silver enrichment slag；To obtained lead
Ammonium chloride and sodium chlorate are added in silver enrichment slag or hypochlorite oxidation agent carries out two sections of counter flow oxidations and leaches, one obtained
Section leachate is using metallic lead displacement recycling silver, output sponge silver and displaced liquid, and displaced liquid is using crystallisation by cooling output
Lead chloride, crystalline mother solution return to two sections of leachings；Two sections are leached two sections of obtained leachates and return to one section of leaching；
Specific step is as follows:
Step 1, alkaline leaching: with ammonium carbonate being that 1:1 ~ 4 are uniformly mixed to obtain mixture by sintering machine head end dedusting ash in mass ratio
Material is that 1:2 ~ 8g/mL adds water to size mixing by solid-to-liquid ratio, is 25 DEG C ~ 95 DEG C in temperature, speed of agitator is 100r/min ~ 600r/min
Under conditions of leached, control reaction time 60min ~ 300min, slurry pH be 7.5 ~ 9.8, liquid divides admittedly after reaction
Slag and alkaline leaching liquid are enriched with from lead silver is obtained；
Step 2, one section of leaching: it is that 1:1 ~ 4 are uniformly mixed that the lead silver that step 1 obtains is enriched with slag with ammonium chloride in mass ratio, is pressed
Solid-to-liquid ratio is that two sections of leachates of 1:3 ~ 15g/mL addition step 3 output are sized mixing, and is 60 DEG C ~ 120 DEG C in temperature, speed of agitator is
Leached under conditions of 100r/min ~ 600r/min, the control reaction time be 120min ~ 300min, slurry pH be 1.5 ~
6.8, solid-liquor separation obtains one section of leachate and one section of leached mud after reaction；
Step 3, two sections of leachings: it is in mass ratio by one section of leached mud and sodium chlorate that step 2 obtains or hypochlorite oxidation agent
30 ~ 100:1 is mixed, and is sized mixing by the crystalline mother solution that solid-to-liquid ratio is 1:3 ~ 15g/mL addition step 5 output, is 50 DEG C in temperature
~ 90 DEG C, speed of agitator be 100r/min ~ 600r/min under conditions of leached, the control reaction time for 120min ~
300min, slurry pH are 1.0 ~ 6.0, and solid-liquor separation obtains two sections of leachates and leaches finishing slag after reaction, two sections of leachings
Liquid return step 2 is recycled；
Step 4, displacement recycling silver: lead flake will be added in one section of leachate that step 2 obtains, the item for being 60 DEG C ~ 100 DEG C in temperature
60min ~ 300min, solid-liquor separation output sponge silver and displaced liquid are reacted under part；
Step 5, crystallisation by cooling recycle lead: the displaced liquid that step 4 is obtained cools, and lead chloride crystal seed is added, in temperature
It is stopped 2 ~ 8 hours under the conditions of being 15 DEG C ~ 40 DEG C, solid-liquor separation obtains lead chloride and crystalline mother solution, and crystalline mother solution return step 3 is followed
Ring uses；
4 ~ 6mol/L aqueous ammonium chloride solution is added when the step 2 leaches for the first time, it is subsequent to leach two sections of leachings that step 3 output is added
Liquid is sized mixing out.
2. the method for steel works sintering head dedusting ash separation and recovery silver and lead according to claim 1, it is characterised in that:
20 ~ 45wt% of sintering machine head end dedusting ash iron content in the step 1, containing 0.1 ~ 3wt% of zinc, containing 3 ~ 20wt% of potassium, containing 0.3 ~ 5wt% of sodium,
100 ~ 800g/t of argentiferous and leaded 3 ~ 22wt%.
3. the method for steel works sintering head dedusting ash separation and recovery silver and lead according to claim 2, it is characterised in that:
The step 2 and step 3 pH values of pulp are regulated and controled using hydrochloric acid and ammonium hydroxide.
4. the method for steel works sintering head dedusting ash separation and recovery silver and lead according to claim 2, it is characterised in that:
Lead flake additional amount is 3 ~ 10 times of the Theoretical Mass for cementing out the silver in one section of leachate completely in the step 4.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810099938.1A CN108277357B (en) | 2018-02-01 | 2018-02-01 | A kind of method of steel works sintering head dedusting ash separation and recovery silver and lead |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810099938.1A CN108277357B (en) | 2018-02-01 | 2018-02-01 | A kind of method of steel works sintering head dedusting ash separation and recovery silver and lead |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108277357A CN108277357A (en) | 2018-07-13 |
| CN108277357B true CN108277357B (en) | 2019-06-11 |
Family
ID=62807313
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810099938.1A Active CN108277357B (en) | 2018-02-01 | 2018-02-01 | A kind of method of steel works sintering head dedusting ash separation and recovery silver and lead |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108277357B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108946795B (en) * | 2018-09-25 | 2020-12-18 | 马鞍山钢铁股份有限公司 | Method for preparing high-purity basic lead carbonate by using lead-containing dedusting ash |
| CN110369451B (en) * | 2019-07-22 | 2021-01-29 | 中南大学 | Method for synergistically and comprehensively utilizing sintering machine head ash and waste incineration fly ash |
| CN113088709B (en) * | 2021-03-30 | 2022-07-26 | 攀钢集团攀枝花钢铁研究院有限公司 | Method for synchronously separating potassium, lead and iron in sintering machine head ash |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB365964A (en) * | 1930-06-17 | 1932-01-28 | Paul Gamichon | Process for converting into soluble salts lead and other metals contained in lead bearing ores |
| GB1576497A (en) * | 1976-04-06 | 1980-10-08 | Asturienne Mines Comp Royale | Lead chloride preparation |
| CN101918600A (en) * | 2007-11-30 | 2010-12-15 | 恩吉泰克技术股份公司 | Process for producing metallic lead starting from desulfurized pastel |
| CN102952942A (en) * | 2012-04-01 | 2013-03-06 | 东北大学 | Method of utilizing medium-lower-grade zinc oxide ores as well as zinc oxide and lead oxide paragenic ores |
| CN103468947A (en) * | 2013-08-15 | 2013-12-25 | 贵州顶效开发区宏达金属综合回收有限公司 | Hydrometallurgical method for separating and extracting Mn, Fe, Pb and Ag from silver-manganese ore |
| CN103757420A (en) * | 2014-01-20 | 2014-04-30 | 北京矿冶研究总院 | Method for recovering lead and silver from zinc leaching residues |
| CN103937975A (en) * | 2014-03-25 | 2014-07-23 | 陕西锌业有限公司 | Method for directly extracting silver from wet method zinc smelting flotation silver concentrates |
-
2018
- 2018-02-01 CN CN201810099938.1A patent/CN108277357B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB365964A (en) * | 1930-06-17 | 1932-01-28 | Paul Gamichon | Process for converting into soluble salts lead and other metals contained in lead bearing ores |
| GB1576497A (en) * | 1976-04-06 | 1980-10-08 | Asturienne Mines Comp Royale | Lead chloride preparation |
| CN101918600A (en) * | 2007-11-30 | 2010-12-15 | 恩吉泰克技术股份公司 | Process for producing metallic lead starting from desulfurized pastel |
| CN102952942A (en) * | 2012-04-01 | 2013-03-06 | 东北大学 | Method of utilizing medium-lower-grade zinc oxide ores as well as zinc oxide and lead oxide paragenic ores |
| CN103468947A (en) * | 2013-08-15 | 2013-12-25 | 贵州顶效开发区宏达金属综合回收有限公司 | Hydrometallurgical method for separating and extracting Mn, Fe, Pb and Ag from silver-manganese ore |
| CN103757420A (en) * | 2014-01-20 | 2014-04-30 | 北京矿冶研究总院 | Method for recovering lead and silver from zinc leaching residues |
| CN103937975A (en) * | 2014-03-25 | 2014-07-23 | 陕西锌业有限公司 | Method for directly extracting silver from wet method zinc smelting flotation silver concentrates |
Non-Patent Citations (1)
| Title |
|---|
| 钢铁冶金烧结灰中铅的浸取回收和一氧化铅的制备;付志刚;《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》;20160415;第13,15-18,27页 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108277357A (en) | 2018-07-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102409183B (en) | Gold extraction method by pre-oxidation and cyanide leaching of refractory gold concentrate | |
| CN102206755B (en) | Method for separating and recovering valuable elements from neodymium-iron-boron wastes | |
| CN103789551B (en) | Prepare manganese sulfate electrolyte with electrolytic manganese anode mud and reclaim plumbous method | |
| CN102925686B (en) | Method for selectively separating and extracting vanadium and chromium from solution containing vanadium and chromium | |
| CN108277357B (en) | A kind of method of steel works sintering head dedusting ash separation and recovery silver and lead | |
| CN110093506A (en) | Valuable metal high efficiency extraction and its minimizing processing method in germanic zinc leaching residue | |
| CN103589873B (en) | A kind of method of valuable metal in recover silver cadmia | |
| CN104831060A (en) | Method for preparing zinc oxalate as zinc oxide powder precursor from middle/low-grade zinc oxide ore | |
| CN109371252A (en) | A kind of device and method of pyrogenic process and wet method combined processing antimony regulus arsenic alkaline slag | |
| CN103773967A (en) | Method for recycling silver, copper and zinc from sintered ash in iron and steel plant | |
| CN105349792B (en) | A kind of brass clinker recycling technique | |
| CN112553478A (en) | Method for quickly leaching nickel hydroxide cobalt sulfuric acid system | |
| CN109295296A (en) | A method of containing recycling antimony in antimony gold concentrate | |
| CN105948084B (en) | A kind of method that magnesium sulfate monohydrate is produced using copper tailing as raw material | |
| CN103484694A (en) | Method for extracting bismuth from copper-bismuth concentrate | |
| CN109055764B (en) | Comprehensive recovery method of high-chlorine low-zinc material | |
| CN106435200A (en) | Method for enriching as well as separating and recovering tellurium and bismuth from solution | |
| CN103266226B (en) | Method for extracting silver from silver-containing zinc concentrate and improving quality of zinc concentrate | |
| CN105399132B (en) | A kind of technique for preparing basic copper chloride and basic zinc chloride with brass clinker and flue dust containing zinc | |
| CN101914681B (en) | Pollution-free method for treating copper, lead and silver-containing material | |
| CN109082537B (en) | Comprehensive utilization method of roasted gold concentrate | |
| CN100402680C (en) | Pollution-free arsenic alkali slage treating technique | |
| CN109136575B (en) | Technological method for processing multi-metal dust by wet method | |
| CN106868299B (en) | A method of the leaching valuable metal from high silicon bidery metal | |
| CN104404258A (en) | Comprehensive utilization process of iron ore sintering dust ash |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |