CN108300873A - A kind of clean Au-Sn deposit circulating leaching method - Google Patents
A kind of clean Au-Sn deposit circulating leaching method Download PDFInfo
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- 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
- C22B30/00—Obtaining antimony, arsenic or bismuth
- C22B30/02—Obtaining antimony
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
- C22B3/46—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes by substitution, e.g. by cementation
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- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
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Abstract
The invention discloses a kind of circulating leaching method of golden antimony separation in clean Au-Sn deposit, this method carries out two sections of high price villaumites to Au-Sn deposit first and leaches, and obtains rich antimony leachate and leached mud, leached mud is Gold Concentrate under Normal Pressure；Secondly, iron plate/powder is added in leachate into line replacement, output finished product sponge antimony and displaced liquid, the main ingredient of displaced liquid is frerrous chloride；Finally, displaced liquid enters diaphragm electrodeposition progress electrodeposition iron, obtains iron plate/powder and high price iron chloride/antimony solution, and iron plate/powder of gained is returned carries out replacement Treatment to leachate, and part is opened a way, two sections of leachings of the high price chloride solution return Au-Sn deposit of gained.The technique of the present invention forms golden antimony separation, the leaching of antimony depth and the removal of impurities of leaching process solution, leachate closed cycle in Au-Sn deposit, there is no waste water and waste residue discharge, solve the hyperplasia of iron in traditional handicraft, difficult separation problem simultaneously, clean and effective, reagent consumption are less, it can be achieved that the cleaning extraction of all kinds of Au-Sn deposits.
Description
Technical field
The invention belongs to non-ferrous metallurgy fields, more particularly to a kind of clean Au-Sn deposit circulating leaching and leaching
Go out the method that liquid removes iron.
Background technology
Antimony is the peculiar strategy metal in China, is widely used in material, chemical industry, building materials field.The smelting of antimony at present
Based on sulphide ore, blast furnace volatilization roasting (melting)-reduction melting technique is mainly used, has been continued to use more than 50 years, it should
Technique have to adaptability to raw material it is strong, be suitable for processing high-grade antimony concentrate, antimony straight gyrus high income, needle antimony oxygen it is purer and production energy
The advantages that power is big.But exists and generate a large amount of low concentration SOs2Smoke pollution environment, high energy consumption and fume amount are big, and dust collecting system is huge
The shortcomings of, as environmental requirement increasingly improves, which has been not suitable with the requirement of development.
For this purpose, from the seventies in last century, people carry out always cleaning antimony regulus new process and fundamental research, wherein
Antimony hydrometallurgy has been unfolded numerous studies due to not having the advantages of arsenic antimony pollution, low energy consumption, good operational environment, mainly there is acid system
It leaches and two process routes of alkaline Leaching.Wet processing is with " vulcanized sodium leaching-Na3SbS3Solution electrodeposition method " is most representative,
The technique is strong to adaptability to raw material, once there is of short duration industrial production, after closed due to alkaline consumption is big, current efficiency is low the problems such as.And it is sour
Method because solves the problems, such as solution recycle, equipment anticorrosion and quick-fried antimony, be mainly used to chloride-hydrolysis at present and produce stibium trioxide,
Without being used to produce metallic antimony.
Patent CN107190142A uses chlorine as Oxidation Leaching agent, leaches rich antimony gold concentrate in acid condition, then
Sponge antimony is produced with iron plate/powder substitution, has the advantages that the leaching rate of antimony is high, main problem, which is chlorine, has harmfulness, strong chlorine
The corrosion of change system is big, leachate is not opened a way, chlorination Slag treatment is cumbersome.Patent CN104831315A proposes a kind of alkaline system
The technique of middle vulcanized sodium leaching-electrodeposition antimony, antimony leaching rate is high, but process system acid and alkali consumption is big, wastewater flow rate is big.Patent
CN106319199A proposes a kind of technique of pyrogenic process roasting-alkali leaching calcining, equally exists the process environments problem of traditional pyrogenic process,
Technique is longer simultaneously.Patent CN104212981A discloses the technique that a kind of ozone leaches Au-Sn deposit as oxidant, and antimony leaches
Rate is up to 95% or more, but ozone prepares power consumption height, infusion solution purification does not solve.
Highlighted wait proposes in the paper " stibnite concentrate wet cleaning New Metallurgical Technology " delivered on Central South University's journal
The experimental study of " closed cycle of leaching-purification-electrodeposition " technique of stibnite concentrate, but either their research
Or the in-pulp electrolysis production practices of stibnite, the leaching rate of iron lead to iron ion hyperplasia in system and cause up to 5%~20%
Whole system is uneven, i.e. the hyperplasia of iron is most important problem, and highlighting in process also can not be to iron using vulcanization removal of impurities
It is removed, which does not solve the problems, such as iron hyperplasia；Meanwhile regeneration SbCl is used in the technique5Solution goes to leach brightness antimony
Mine, but SbCl5Solution-stabilized existing pH required values are small, and acidity is big, corrodes greatly to equipment, and the cathode in diaphragm electrodeposition
It is easy that chlorine is precipitated.
From the point of view of the protection of the occupational disease of clean metallurgical and production process, automation, antimony hydrometallurgy has inborn
Advantage, but to solve leaching process oxidant selection, liquor capacity expansion, purification of leaching liquor/except iron and equipment anticorrosion the problems such as.
Based on this, on the basis of summarizing each antimony hydrometallurgy technological advantage, this project proposes golden antimony point in a kind of clean Au-Sn deposit
From circulating leaching method, pass through high price leachings, iron plate/powder substitution, diaphragm electrodeposition complete golden antimony in Au-Sn deposit detach, antimony depth
Leaching, leachate cleaning remove iron, the oxidants such as at high price and the big dual oxide of environmental hazard, chlorine, ozone are eliminated, with electricity
Solution preocess regenerates high price oxidant and replaces.Purpose is that form complete Whote-wet method puies forward antimony new method, reaches three wastes emission reduction, reagent
Subtract consumption, the production process of cleaning green.
Invention content
The problem of for background technology, the present invention propose that a kind of Au-Sn deposit Whote-wet method technique detaches golden antimony and production
The method of metallic antimony, process closed cycle, green emission reduction.
The purpose of the present invention is achieved by the following technical programs：
The circulating leaching method of golden antimony separation, includes the following steps in a kind of clean Au-Sn deposit：
S1. high price leaches：Au-Sn deposit is leached using the high price chloride solution containing ferric iron and/or quinquevalence antimony,
Leachate and lower slurries are obtained, lower slurries add certain above-mentioned high price villaumite and carry out secondary leaching, then obtain leachate and leaching
Slag, leached mud are Gold Concentrate under Normal Pressure；
S2. iron plate/powder substitution antimony：Iron plate/powder is added in the leachate that S1 walks output into line replacement, output finished product sea
The main ingredient of continuous antimony and displaced liquid, displaced liquid is frerrous chloride, and frerrous chloride is the raw material of next step S3 electrodeposition；
S3. electrodeposition is except iron and leaching agent regeneration：The displaced liquid that step S2 is obtained carries out diaphragm electrodeposition, cathode output iron
Piece/powder and raffinate, anode output high price iron chloride/antimony solution.Iron plate/powder return to step S3 and part are opened a way, and high price iron chloride/
Antimony solution whole return to step S1 is leached, and completes the cleaning regeneration of high price villaumite.
Scientific design of the present invention production stage, each process linking is smooth, and material stream and energy stream are fully used, first
The high price for first carrying out Au-Sn deposit leaches, using containing Fe3+、Sb5+High price acid chlorization solution leach antimony ore, have according in solution
It is different, it can be achieved that antimony leaching rate 50~90% in Au-Sn deposit to imitate ion concentration, and gold and arsyl are not originally leached, in the process mainly
Following reaction occurs：
Sb2S3+6FeCl3=2SbCl3+6FeCl2+3S0 (1)
Sb2S3+3SbCl5=5SbCl3+3S0 (2)
SbCl3+ Cl-=SbCl4 - (3)
FeS+2FeCl3=3FeCl2+S0 (4)
FeS+SbCl5=FeCl2+SbCl3+S0 (5)
By isolated rich antimony leachate and leached mud, leached mud it is Gold Concentrate under Normal Pressure after two-stage leaching, rich antimony leachate
It is main that following reaction occurs with iron plate/powder substitution recycling wherein metallic antimony：
2SbCl3+ 3Fe=2Sb+3FeCl2 (6)
Displaced liquid removes iron by diaphragm electrodeposition again, and cathode obtains iron plate/powder, returns to displacement sponge antimony, electrode raffinate is then
Anode is pumped into be aoxidized；Oxidation reaction, Fe therein all occur for entire Anodic2+And Sb3+Occur oxidation reaction and
It is regenerated as Fe3+And Sb5+, return to the leaching step of the first step.It is main in the process that following reaction occurs：
Cathode：Fe2++2e-=Fe (7)
Anode：Fe2+-e-=Fe3+(E0=0.771V) (8)
Sb3+-2e-=Sb5+(E0=0.785V) (9)
From the above mentioned, entire technique realizes the closed cycle utilization of leaching agent, and needing to open a way, it is only pollution-free to arrange outside
Iron plate/powder, and the only clean electric energy consumed is arranged between each step scientific and reasonable.
Preferably, Au-Sn deposit described in step S1 can be the high/low grade Au-Sn deposit containing gold, arsenic, lead.
Preferably, during step S1 high prices leach, Controlled acidity is 0.5~4g/L, and liquid-solid ratio is 5~20：1,
Temperature is 30~80 DEG C, and the time is 2~5h, Fe in solution3+And Sb5+Content be respectively 60~150g/L and 1~5g/L；Into
The preferred Fe of one step3+Content is 80~100g/L.
It is further preferred that liquid-solid ratio is 6~12：1, temperature is 30~70 DEG C, and the time is 2~5h.
Preferably, the condition of iron plate/powder substitution described in step S2 is：Temperature be 20~60 DEG C, the time be 1~5h, iron plate/
Powder dosage is 1.0~1.5 times of theoretical amount, that is, the stoichiometric coefficient for pressing formula (6) progress displacement antimony completely calculates.
It is further preferred that iron plate described in step S2/powder substitution process temperature is 30~50 DEG C, the time is 2~3h.
Preferably, in step S3, it is graphite or titanium plate, cathode that the diaphragm for electrolytic cell, which uses anion-exchange membrane, anode,
For titanium plate or stainless steel plate.
It is further preferred that electrolytic deposition process current strength is 150~400A/m2, temperature be 20~60 DEG C, the time be 10~
30h, 20~60mm of pole span；Still further preferably current strength is 200~350A/m2。
Preferably, iron plate/powder of open circuit is the 5~30% of the total iron plate of cathode output/powder amount, and anolyte 100% returns to leaching
Go out.
Preferably, raffinate obtained by step S3 is sent to step S3 anodes.
Compared with the prior art, the beneficial effects of the present invention are：
(1) present invention mainly utilizes regenerated FeCl3Anolyte leaches Au-Sn deposit, wherein SbCl5It is a small amount of to exist, mainly
FeCl3(90% or more), antimony leaching rate improves the leaching rate of antimony up to 99% after two sections are leached.Meanwhile FeCl3Solution is steady
Fixed existing pH requires relatively low, and pH is less than 1, and when electrolysis does not have chlorine to emerge, at the same reduce to equipment corrosion.
(2) the invention carries out electrodeposition to solution after displacement antimony and removes iron, while solving antimony hydrometallurgy process
The problem of middle iron hyperplasia, iron plate/powder that electrodeposition obtains later can return again into line replacement antimony, extra iron plate/powder open circuit
It sells outside, the high price iron/antimony solution obtained after electrodeposition also can return to and be leached again, realize the cycle of entire technical process.
(3) present invention realizes depth leaching and the leaching process solution closed cycle of Au-Sn deposit, is arranged without waste water and waste residue
Go out, while solving the hyperplasia of iron in traditional handicraft, difficult separation problem, clean and effective, reagent consumption are less, it can be achieved that each eka-gold antimony
The cleaning of mine is extracted.
Description of the drawings
Attached drawing 1 is the method for the present invention process flow chart.
Attached drawing 2 is the color change for leaching finishing slag, iron plate/powder and each solution of 1 output of the embodiment of the present invention.
Specific implementation mode
It is further illustrated the present invention with reference to specific embodiment.Following embodiments only for illustration, Bu Nengli
Solution is limitation of the present invention.Unless stated otherwise, the raw material and equipment used in following embodiments, which are this field, routinely to be made
Raw material and equipment.
Embodiment 1
The present embodiment process flow chart is as shown in Fig. 1.
The ingredient (wt.%) of golden antimony concentrate as test raw material is：Sb 50.54、Fe 8.16、S 25.04、SiO2
12.63、Al2O32.95,1.02 CaO, As 0.81, MgO 0.30, the 53g/t containing gold；High price chloride as leaching agent
Composition is (g/L)：Fe3+100.47、Sb5+2.80, acidity 1.03g/L.
S1. high price leaches：The stibnite concentrate 200g for weighing mentioned component, by liquid-solid ratio 10：1 is added the above-mentioned height of 2000mL
Valence chloride leaching liquid, reacts 2h at 50 DEG C；500mL high price chloride leachings are added in slurries after separation leachate
Liquid, the reaction was continued at 50 DEG C 1h are separated by filtration to obtain finishing slag 93.5g and rich antimony liquid 2392mL, through analyze in finishing slag containing antimony 1.03%,
Containing golden 101g/t, calculate antimony leaching rate be 99.04%.
S2. sponge antimony is replaced：The leachate 2000mL that step S1 is obtained is taken, 60g iron powders are added and remove antimony, process into line replacement
Middle maintenance temperature 50 C, time 2h, through analyze displaced liquid in antimony content be 0.89g/L, iron content 128.67g/L；
S3. electrodeposition is except iron and leaching agent regeneration：The displaced liquid that step S2 is obtained is added in diaphragm cell, wherein cloudy
Pole 1020mL, anode 980mL carry out diaphragm electrodeposition and remove iron, and diaphragm for electrolytic cell uses anion-exchange membrane, and anode is graphite, cloudy
Extremely titanium plate.200A/m is maintained in electrolytic deposition process2, 40 DEG C of temperature, time 20h, interpolar away from for 40mm, isolated sun after reaction
Pole liquid and cathode iron plate/powder, wherein iron plate/powder weight 35.16g, it is 99.02% to calculate cathode efficiency, is contained in cathode raffinate
Fe2+92.71g/L, catholyte contain Fe3+69.28g/L、Sb5+1.20g/L。
Iron plate/powder return to step S3 and part open a way obtained by the present embodiment step S3, and anode high price iron chloride/antimony solution is complete
Portion return to step S1 is leached, and raffinate obtained by step S3 is sent to step S3 anodes, and overall process is discharged without waste water and waste residue, and anode does not also have
Irritant gas generates, entire production process zero-emission.
The color change for leaching finishing slag, iron plate/powder and solution for testing output is as shown in Fig. 2, leaches finishing slag color hair
In vain, sharp contrast is formed with the Dark grey of raw ore；Gained iron powder fragmentates shape, and surface area is larger, is just suitable for displacement sponge
Antimony；And from the point of view of the color of each solution, the anolyte color after ferroelectric is most deep, illustrates Fe3+Concentration is high, and the catholyte after ferroelectric
Lighter, a large amount of precipitations with iron, which are formed, to be verified.
Embodiment 2
The present embodiment is the circulating leaching process for continuing embodiment 1, and Au-Sn deposit composition used is the same as embodiment 1, high price used
Leachate is that the electrodeposition that 1 step S3 of embodiment is obtained removes iron anode liquid.
S1. high price leaches：The stibnite concentrate 50g for weighing mentioned component, by liquid-solid ratio 10：1 is added 500mL ferroelectric anodes
Liquid reacts 2h at 70 DEG C, and the electrodeposition that 1 step S3 of 300mL embodiments is obtained is added after separation leachate and removes iron anode liquid,
1h is reacted at 70 DEG C, finishing slag 23.4g and rich antimony liquid 723mL is separated by filtration to obtain, through analyzing in finishing slag containing antimony 1.52%, containing gold
108g/t, calculate antimony leaching rate be 99.29%.
S2. sponge antimony is replaced：The leachate 700mL that step S1 is obtained is taken, 20g iron powders are added and remove antimony, process into line replacement
Middle maintenance temperature 60 C, time 1h, through analyze displaced liquid in antimony content be 1.82g/L, iron content 125.19g/L；
S3. electrodeposition is except iron and leaching agent regeneration：The displaced liquid that step S2 is obtained is added in microdiaphragm electrolytic cell,
Middle cathode 350mL, anode 330mL carry out diaphragm electrodeposition and remove iron, and diaphragm for electrolytic cell uses anion-exchange membrane, and anode is graphite,
Cathode is titanium plate.200A/m is maintained in electrolytic deposition process2, temperature 50 C, time 10h, interpolar away from for 60mm, it is isolated after reaction
Anolyte and cathode iron plate/powder, wherein iron plate/powder weight 12.04g, it is 99.11% to calculate cathode efficiency, in cathode raffinate
Containing Fe2+84.67g/L, catholyte contain Fe3+65.34/L、Sb5+1.03g/L。
Iron plate/powder return to step S3 and part open a way obtained by the present embodiment step S3, and anode high price iron chloride/antimony solution is complete
Portion return to step S1 is leached, and raffinate obtained by step S3 is sent to step S3 anodes, and overall process is discharged without waste water and waste residue, and anode does not also have
Irritant gas generates, entire production process zero-emission.
Embodiment 3
Test raw material, reagent and step are the same as embodiment 1.
S1. high price leaches：The stibnite concentrate 300g for weighing mentioned component, by liquid-solid ratio 6：1 is added the above-mentioned height of 1800mL
Valence chloride leaching liquid, reacts 3h at 30 DEG C；The above-mentioned high price chlorides of 1500mL are added in slurries after separation leachate
Leachate is separated by filtration to obtain finishing slag 136.03g and rich antimony liquid 3417mL after the reaction was continued at 30 DEG C 2h, contains antimony in finishing slag through analyzing
2.06%, the 115g/t containing gold, calculate antimony leaching rate be 98.13%.
S2. sponge antimony is replaced：The leachate 3000mL that step S1 is obtained is taken, 85g iron powders are added and remove antimony, process into line replacement
Middle 30 DEG C of maintenance temperature, time 3h, through analyze displaced liquid in antimony content be 2.18g/L, iron content 118.04g/L；
S3. electrodeposition is except iron and leaching agent regeneration：The displaced liquid that step S2 is obtained is added in diaphragm cell, wherein cloudy
Pole 1550mL, anode 1500mL carry out diaphragm electrodeposition and remove iron, and diaphragm for electrolytic cell uses anion-exchange membrane, and anode is titanium plate, cloudy
Extremely stainless steel plate.400A/m is maintained in electrolytic deposition process2, 30 DEG C of temperature, time 15h, interpolar away from for 20mm, detached after reaction
To anolyte and cathode iron plate/powder, wherein iron plate/powder weight 79.68g, it is 99.46% to calculate cathode efficiency, cathode raffinate
In contain Fe2+50.32g/L, catholyte contain Fe3+110.04g/L、Sb5+2.02g/L。
Iron plate/powder return to step S3 and part open a way obtained by the present embodiment step S3, and anode high price iron chloride/antimony solution is complete
Portion return to step S1 is leached, and raffinate obtained by step S3 is sent to step S3 anodes, and overall process is discharged without waste water and waste residue, and anode does not also have
Irritant gas generates, entire production process zero-emission.
Embodiment 4
The present embodiment is the circulating leaching process of embodiment 3, and Au-Sn deposit composition used is leached with embodiment 1, high price used
Liquid is that the electrodeposition that 3 step S3 of embodiment is obtained removes iron anode liquid.
S1. high price leaches：The stibnite concentrate 100g for weighing mentioned component, by liquid-solid ratio 12：1 is added 1200mL ferroelectric sun
Pole liquid reacts 2h at 50 DEG C, and the electrodeposition that 3 step S3 of 300mL embodiments is obtained is added after separation leachate and removes iron anode liquid,
2h is reacted at 50 DEG C.It is separated by filtration to obtain finishing slag 47.03g and rich antimony liquid 1402mL, through analyzing in finishing slag containing antimony 1.76%, containing gold
100g/t, calculate antimony leaching rate be 99.59%.
S2. sponge antimony is replaced：The leachate 1400mL that step S1 is obtained is taken, 45g iron powders are added and remove antimony, process into line replacement
Middle 30 DEG C of maintenance temperature, time 3h, through analyze displaced liquid in antimony content be 2.31g/L, iron content 128.10g/L；
S3. electrodeposition is except iron and leaching agent regeneration：The displaced liquid that step S2 is obtained is added in microdiaphragm electrolytic cell,
Middle cathode 700mL, anode 650mL carry out diaphragm electrodeposition and remove iron, and diaphragm for electrolytic cell uses anion-exchange membrane, and anode is graphite,
Cathode is titanium plate.500A/m is maintained in electrolytic deposition process2, 30 DEG C of temperature, time 15h, interpolar away from for 50mm, it is isolated after reaction
Anolyte and cathode iron plate/powder, wherein iron plate/powder weight 44.50g, it is 99.23% to calculate cathode efficiency, in cathode raffinate
Containing Fe2+56.34g/L, catholyte contain Fe3+124.85/L、Sb5+2.03g/L。
Iron plate/powder return to step S3 and part open a way obtained by the present embodiment step S3, and anode high price iron chloride/antimony solution is complete
Portion return to step S1 is leached, and raffinate obtained by step S3 is sent to step S3 anodes, and overall process is discharged without waste water and waste residue, and anode does not also have
Irritant gas generates, entire production process zero-emission.
Claims (9)
1. a kind of clean Au-Sn deposit circulating leaching method, which is characterized in that include the following steps：
S1. high price leaches：Au-Sn deposit is leached using the high price chloride solution containing ferric iron and/or quinquevalence antimony, must be soaked
Go out liquid and lower slurries, lower slurries add certain above-mentioned high price chloride solution and carry out secondary leaching, then obtain leachate and leaching
It slags tap, leached mud is Gold Concentrate under Normal Pressure；
S2. iron plate/powder substitution antimony：S1 is walked to the leachate of output, iron plate/powder is then added into line replacement, obtains sponge antimony and sets
Change rear liquid；
S3. electrodeposition is except iron and leaching agent regeneration：The displaced liquid progress diaphragm electrodeposition that step S2 is obtained, cathode output iron plate/
Powder and raffinate, anode output high price iron chloride/antimony solution；
Wherein, iron plate/powder return to step S3 obtained by step S3 and part are opened a way, high price iron chloride/antimony solution whole return to step
S1 is leached.
2. clean Au-Sn deposit circulating leaching method according to claim 1, which is characterized in that leached in step S1 high prices
During, it is 0.1~2g/L that two sections, which are leached equal Controlled acidity, and liquid-solid ratio is 5~20：1, temperature is 30~80 DEG C, the time 1
~5h, Fe in solution3+And Sb5+Content be respectively 60~150g/L and 1~5g/L.
3. clean Au-Sn deposit circulating leaching method according to claim 2, which is characterized in that the liquid-solid ratio be 6~
12：1, temperature is 30~70 DEG C, and the time is 2~5h.
4. clean Au-Sn deposit circulating leaching method according to claim 1, which is characterized in that iron plate described in step S2/
Powder substitution process temperature is 20~60 DEG C, and the time is 1~5h, and iron plate/powder dosage is 1.0~1.5 times of theoretical amount.
5. clean Au-Sn deposit circulating leaching method according to claim 4, which is characterized in that iron plate described in step S2/
Powder substitution process temperature is 30~50 DEG C, and the time is 2~3h.
6. clean Au-Sn deposit circulating leaching method according to claim 1, which is characterized in that in step S3, the electricity
It is graphite or titanium plate to solve slot diaphragm and use anion-exchange membrane, anode, and cathode is titanium plate or stainless steel plate.
7. clean Au-Sn deposit circulating leaching method according to claim 6, which is characterized in that in step S3, electrodeposition mistake
Journey current strength is 150~400A/m2, temperature is 20~60 DEG C, and the time is 10~30h, 20~60mm of pole span.
8. clean Au-Sn deposit circulating leaching method according to claim 1, which is characterized in that in step S3, open circuit
Iron plate/powder is the 5~30% of the total iron plate of cathode output/powder amount.
9. clean Au-Sn deposit circulating leaching method according to claim 1, which is characterized in that raffinate is sent obtained by step S3
Toward step S3 anodes.
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