CN107881342A - The method of comprehensive utilization of iron ion in arsenic-containing gold ore pressureleaching solution - Google Patents
The method of comprehensive utilization of iron ion in arsenic-containing gold ore pressureleaching solution Download PDFInfo
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- CN107881342A CN107881342A CN201711020686.0A CN201711020686A CN107881342A CN 107881342 A CN107881342 A CN 107881342A CN 201711020686 A CN201711020686 A CN 201711020686A CN 107881342 A CN107881342 A CN 107881342A
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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
- C22B3/04—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
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
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- C—CHEMISTRY; METALLURGY
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- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet processes
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Abstract
The present invention relates to a kind of method of comprehensive utilization of iron ion in arsenic-containing gold ore pressureleaching solution, is carried out as follows with condition：Three-level stirring acidifying：By aurin (in) ore deposit and use Oxidation Leaching liquid after first being started with sulfuric acid instead and stir into slurry and acidification reaction, decomposing carbonate, react and carried out in one to No. three tank diameter of series connection, Oxidation Leaching liquid presses formula V=980 ω/CH2SO4+2.625CFe3+Calculated value adds；It is dense：Ore pulp after acidifying is entered into concentrator to be settled, then is first added to acidifying solution and to be used remaining Oxidation Leaching liquid instead after alkali starts and carry out neutralization removal of impurities；Pressure oxidation：Acidifying ore pulp underflow is entered into autoclave and carries out pressure oxidation under certain condition；Solid-liquor separation：Pulp liquid-solid isolation will be aoxidized, H must be contained2SO430‑50g/L、Fe3+18 25g/L Oxidation Leaching liquid, Oxidation Leaching liquid are stored in solution tank reuse.It is realized the acid balance of system, stable effect of settling ore pulp, is ensured that flow is unimpeded, avoids hydrolyzing caused Fe (OH) using the iron replacement sulfur bronsted lowry acids and bases bronsted lowry in Oxidation Leaching liquid3Colloid is formed, has the advantages that economical, simple, efficient, factory application is pressed suitable for similar oxygen.
Description
Technical field
The present invention relates to a kind of method of comprehensive utilization of iron ion in arsenic-containing gold ore pressureleaching solution, suitable for similar oxygen pressure work
Factory applies.
Background technology
China's Gold Deposit Types are various, and wherein gold cures thing such as pyrite FeS2, the parcel such as mispickel FeAsS be difficult gold
One of the main reason for ore deposit gold recovery rate is low.Pressure oxidation is to handle the maximally effective work of sulfide parcel gold mine in the prior art
Skill, it is because pyrite FeS2Following two parallel competitive reactions be present in the oxidation under high-temperature and high-pressure conditions：
FeS2+7/2O2+H2O=FeSO4+H2SO4 (1)
FeS2+2O2=FeSO4+S0 (2)
There is also two reactions for mispickel FeAsS oxidation：
2FeAsS+13/2O2+3H2O=3H3AsO4+2FeSO4 (3)
2FeAsS+7/2O2+2H2SO4+H2O=2H3AsO4+2FeSO4+2S0 (4)
Gold mine pressure oxidation is typically reacted at a high temperature of 180-220 DEG C, so now S0Almost all is oxidized, reaction
(1), (3) are dominant, ferrous ion caused by reaction, continue to be oxidized to ferric ion by following reaction：
2FeSO4+1/2O2+H2SO4=Fe2(SO4)3+H2O (5)
Hydrolysis, generation bloodstone (Fe further occur for the ferric ion of generation2O3), ferric subsulfate (FeOHSO4)
Or precipitation as jarosite, its degree depend on the Fe of solution3+、H2SO4Concentration and the condition such as temperature, the leaching rate one of final iron
As in 20-65% or so.
Found through the present inventor's experimental study：Formula (3), the H of (4) generation3AsO4In finite concentration, acidity, concentration of iron and anti-
Under the conditions of between seasonable, stable precipitated ferric arsenate can be generated, so as to reduce the pollution of arsenic.
That is Fe2(SO4)3+2H3AsO4+4H2O=2FeAsO4·2H2O↓+3H2SO4 (5)
The gold mine high to carbonate content, before pressure oxidation is entered, it is also necessary to carbonate therein is first decomposed with acid, it is no
Then carbonate can generate CO in autoclave with sulfuric acid reaction2Gas, gas-phase space in kettle is occupied, reduce partial pressure of oxygen in kettle, from
And reduce and even stop pressure oxidation effect.The reaction equation of carbonate decomposition is shown below in ore：
CO3 2-+H2SO4→CO2↑+SO4 2- (6)
The acid solution leached with pressure oxidation is can contemplate in order to save the dosage of acid, during decomposing carbonate to be handled, but
For sulfur-bearing than relatively low (＜ 16%) and carbonate containing higher (＞ 25%) Gold Concentrate under Normal Pressure (in) ore deposit, due to sour caused by oxidation
Deficiency, sulfuric acid must also be added in decomposing carbonate process and adds alkali in and when cleaning, so as to increase cost.
The method of comprehensive utilization that iron ion in a kind of arsenic-containing gold ore pressureleaching solution is researched and developed for this just seems particularly urgent.
The content of the invention
It is an object of the invention to provide a kind of method of comprehensive utilization of iron ion in arsenic-containing gold ore pressureleaching solution, by right
The reasonable utilization of iron ion, it can effectively reduce the reagent consumption cost in production process and the settlement of arsenic can be promoted.
Sulfuric acid in pressure oxidation leachate return acidifying can with decomposing carbonate, such as reaction equation (6), but handle low-sulfur,
During the gold mine of high-carbon hydrochlorate, for the subacidity in oxidation solution with decomposing carbonate, the present invention utilizes the hydrolysising property of iron ion, such as anti-
Formula (7) is answered, by the control to hydrolysis, the molten iron solution in oxidation solution is produced acid, so as to reduce additional sulfuric acid dosage.
Meanwhile using the measure of Discrete control, it can effectively avoid hydrolyzing caused Fe (OH)3Forming colloid influences effect of settling ore pulp,
As following formula can two-way reaction：
Because the ore pulp needs after acidifying are dense, supernatant needs to neutralize removal of impurities, and iron can also significantly drop in front end precipitation
The dosing of low solution N-process, so passing through the reasonable control to raw material, acidity, it is possible to achieve optimal " acid balance "
State, reach most economical, environmentally friendly service condition.
The task of the present invention is completed by the following technical programs：
The method of comprehensive utilization of iron ion in arsenic-containing gold ore pressureleaching solution, applicable object are sulfur-bearing 10-16%, arsenic
0.8-3.5%, with calcium carbonate carbonate 25-45% aurin (in) the Oxidation Leaching liquid of ore deposit, concrete technology step and condition
It is as follows：
A. three-level stirring acidifying：By aurin (in) ore deposit and use the Oxidation Leaching liquid that step D obtains after first being started with sulfuric acid instead
Slurry and acidification reaction are stirred into, decomposing carbonate, reacts and is carried out in one to No. three tank diameter of series connection, from three tank diameters
Bottom is filled with air, and ore pulp adds from No.1 groove, and it is more from No.1 groove point to flow automatically to No. three grooves, sulfuric acid or even Oxidation Leaching liquid by groove
Point is distributed to be added, and addition presses formula V=980 ω/CH2SO4+2.625CFe3+Calculate, in formula：
V(m3/ t) --- the Oxidation Leaching liquid product that ore per ton adds, it is allowed to departure ± 10%
ω (%) --- with calcium carbonate carbonate content in ore
CH2SO4(kg/m3) --- H in leachate2SO4Concentration
CFe3+(kg/m3) --- Fe in leachate3+Concentration
The exit pH scope of one, two, No. three tank diameter ore pulp of control is respectively 1.5-2.2,2.2-2.5,2.5-3.2,
Obtain the ore pulp after the acidifying of No. three tank diameters.
B. it is dense：The ore pulp after acidifying is transported into concentrator from No. three tank diameters to be settled, obtains acidifying solution and concentration is
The acidifying ore pulp underflow of solid masses 45~50%, then first added after alkali starts to acidifying solution and use the remaining oxygen that step D is obtained instead
Change leachate and carry out neutralization removal of impurities, slag must be neutralized and enter Tailings Dam；
C. pressure oxidation：Acidifying ore pulp underflow is entered into autoclave and carries out pressure oxidation, 200-220 DEG C of oxidizing temperature, oxygen
0.4-1.0MPa is pressed, residence time 50-100min, obtains oxidation ore pulp；
D. solid-liquor separation：Pulp liquid-solid isolation will be aoxidized, H must be contained2SO430-50g/L、Fe3+18-25g/L oxidation leaching
Go out liquid and oxidizing slag, Oxidation Leaching liquid is stored in that solution tank is stand-by or direct return to step A three-levels stirring acidifying substitute sulfuric acid and
Neutralized after step B is dense except using mixedly, other process otherwise processeds can be entered by obtaining oxidizing slag.
The percentage being related in specification is mass percent.
The present invention has advantages below and effect compared with prior art：
1. using the iron in arsenic-containing gold ore pressure oxidation leachate, sulfuric acid source is provided for ore decomposition carbonate, can be made
Acidization, which is reduced, even removes additional sulfuric acid from.
It is 2. unimpeded by more influence effect of settling ore pulp on iron hydrolysis, flow.
3. the reagent consumption for neutralizing removal of impurities can be greatly lowered, the acid balance of system is realized.
4. by the precise controlling to technique, can effectively avoid hydrolyzing caused Fe (OH)3Form colloid consumption, fully profit
The characteristics of reacting is pressed with oxygen.
5. it is a kind of economic, simple, effective matching method, suitable for similar Yang Ya factories popularization and application.
Brief description of the drawings
Fig. 1 is the method for comprehensive utilization technique according to iron ion in a kind of arsenic-containing gold ore pressureleaching solution proposed by the present invention
Flow chart.
Each sign represents respectively in accompanying drawing：
1. the ore pulp 2. after acidifying is acidified ore pulp underflow 3. and is acidified the oxygen of 5. oxidizing slag of the oxidation ore pulp of ore pulp overflow 4. 6.
Change leachate 7. in and slag
Explanation is described in further detail below in conjunction with accompanying drawing.
Embodiment
As shown in figure 1, the present invention a kind of arsenic-containing gold ore pressureleaching solution in iron ion method of comprehensive utilization technique, fit
Object be sulfur-bearing 10-16%, arsenic 0.8-3.5%, with calcium carbonate carbonate 25-45% aurin (in) oxidation of ore deposit soaks
Go out liquid, concrete technology step and condition are as follows：
A. three-level stirring acidifying：By aurin (in) ore deposit and use the Oxidation Leaching liquid 6 that step D obtains after first being started with sulfuric acid instead
Slurry and acidification reaction are stirred into, decomposing carbonate, reacts and is carried out in one to No. three tank diameter of series connection, from three tank diameters
Bottom is filled with air, and ore pulp adds from No.1 groove, and No. three grooves, sulfuric acid or even Oxidation Leaching liquid 6 are flowed automatically to from No.1 groove point by groove
Multiple spot is distributed to be added, and addition presses formula V=980 ω/CH2SO4+2.625CFe3+Calculate, in formula：
V(m3/ t) --- the Oxidation Leaching liquid product that ore per ton adds, it is allowed to departure ± 10%
ω (%) --- with calcium carbonate carbonate content in ore
CH2SO4(kg/m3) --- H in leachate2SO4Concentration
CFe3+(kg/m3) --- Fe in leachate3+Concentration
The exit pH scope of one, two, No. three tank diameter ore pulp of control is respectively 1.5-2.2,2.2-2.5,2.5-3.2,
Obtain the ore pulp 1 after the acidifying of No. three tank diameters.
B. it is dense：The ore pulp 1 after acidifying is transported into concentrator from No. three tank diameters to be settled, obtains acidifying solution 3 and concentration
For the acidifying ore pulp underflow 2 of solid masses 45~50%, then first add after alkali starts to acidifying solution 3 use instead step D obtain it is surplus
Remaining Oxidation Leaching liquid 6 carries out neutralization removal of impurities, must neutralize slag (7) and enter Tailings Dam；
C. pressure oxidation：Acidifying ore pulp underflow 2 is entered into autoclave and carries out pressure oxidation, 200-220 DEG C of oxidizing temperature, oxygen
0.4-1.0MPa is pressed, residence time 50-100min, ore pulp 4 must be aoxidized；
D. solid-liquor separation：The solid-liquor separation of ore pulp 4 will be aoxidized, H must be contained2SO430-50g/L、Fe3+18-25g/L oxidation
Leachate 6 and oxidizing slag 5, Oxidation Leaching liquid 6 are stored in that solution tank is stand-by or direct return to step A three-levels stirring acidifying replacement sulfur
Neutralized after acid and step B are dense except using mixedly, other process otherwise processeds can be entered by obtaining oxidizing slag 5.
The method of the present invention may furthermore is that：
The aeration quantity of tri- tank diameters of step A is respectively 10-12,8-10,4-6Nm3/㎡·h。
The alkali of neutralization removal of impurities in the step B is lime.
Embodiment 1
Certain Gold Concentrate under Normal Pressure sulfur-bearing 15.2%, iron content 21%, containing arsenic 3.2%, carbonate containing (with calcium carbonate) 41.5%, pressurization
Oxidation solution after oxidation produces sour 185kg/t, starts by 220kg/t elder generations enriching sulfuric acid, after the Oxidation Leaching liquid 6 of solid-liquor separation is returned
Return stirring acidifying decomposing carbonate, acidifying solution 3 first adds lime to start to removal of impurities is neutralized by 180kg/t, after by the surplus of solid-liquor separation
Remaining Oxidation Leaching liquid 6 is returned to neutralize to remove and used mixedly.
Using the method for the present invention, concrete operation step and technological parameter are as follows：
(1) Oxidation Leaching liquid 6 contains H2SO442.1g/L, containing Fe3+21g/L。
(2) enter before autoclave aurin (in) ore deposit and step D Oxidation Leaching liquid 6 is stirred acidification reaction, decompose
Carbonate, react and carried out in the tank diameter of three series connection, be filled with air from trench bottom, the aeration quantity of three grooves is controlled as
12、10、6Nm3/ ㎡ h, ore pulp add from No.1 groove, flow automatically to No. three grooves by groove, Oxidation Leaching liquid 6 divides multiple spot from No.1 groove
Distribution adds, and the addition of Oxidation Leaching liquid 6 presses V=980 ω/CH2SO4+2.625CFe3+=4.18m3/ t is added, by micro-
The addition flow of Oxidation Leaching liquid 6 is adjusted, the exit pH of one, two, No. three groove ore pulp of control is respectively 1.5,2.2,2.5.
(3) ore pulp 1 after the acidifying after step A decomposing carbonates is transported into concentrator from No. three grooves to be settled, acid
Change liquid 3 to go to neutralize removal of impurities, concentration enters autoclave for the acidifying ore pulp of solid masses 45% underflow 2 and carries out pressure oxidation, oxidizing temperature
218 DEG C, partial pressure of oxygen 0.8MPa, residence time 100min, rear oxidation leachate 6 directly returns to step after aoxidizing the solid-liquor separation of ore pulp 4
Suddenly A three-levels stir acidifying replacement sulfuric acid and the dense rear neutralizations of step B are removed and used mixedly.
This example can reach system acid balance, and additional sulfuric acid, acidifying solution open circuit neutralization do not remove decomposing carbonate process after startup
Miscellaneous consumption lime is reduced to 115kg/t.
Embodiment 2
Certain aurin (in) ore deposit sulfur-bearing 12.3%, iron content 19.1%, containing arsenic 1.6%, carbonate containing (with calcium carbonate)
30.06%, pressure oxidation rear oxidation liquid produces sour 150kg/t, starts by 144kg/t elder generations enriching sulfuric acid, after by the oxygen of solid-liquor separation
Change leachate 6 and return to stirring acidifying decomposing carbonate, acidifying solution 3 first adds lime to start to removal of impurities is neutralized by 165kg/t, after by liquid
Admittedly the remaining Oxidation Leaching liquid 6 separated is returned to neutralize to remove and used mixedly.
Using the method for the present invention, concrete operation step and technological parameter are as follows：
(1) Oxidation Leaching liquid 6 contains H2SO434g/L, containing Fe3+19.1g/L。
(2) enter before autoclave aurin (in) ore deposit and step D Oxidation Leaching liquid 6 is stirred acidification reaction, decompose
Carbonate, react and carried out in the tank diameter of three series connection, be filled with air from trench bottom, ore pulp adds from No. 1 groove, flows automatically to 3
The outflow of number groove, leachate divide multiple spot is distributed to add from No. 1 groove, and the addition of Oxidation Leaching liquid 6 presses V=980 ω/CH2SO4+
2.625CFe3+=3.5m3/ t is added, and by finely tuning the addition flow of Oxidation Leaching liquid 6, one, two, No. three groove ore pulp of control goes out
Mouth pH value range is respectively 2.1,2.4,3.1.
(3) ore pulp 1 after the acidifying after step A decomposing carbonates is transported to concentrator from No. three grooves and settled, concentration
Ore pulp underflow 2 is acidified for solid masses 45-50% and enters autoclave pressurization oxidation, 210 DEG C of oxidizing temperature, partial pressure of oxygen 0.6MPa, is stopped
Time 80min is stayed, aoxidizes the direct return to step A three-levels stirring acidifying replacement sulfuric acid of rear oxidation leachate 6 after the solid-liquor separation of ore pulp 4
Remove and use mixedly with the dense rear neutralizations of step B.
This example can reach system acid balance, decomposing carbonate process not additional sulfuric acid after startup, during Oxidation Leaching liquid 6 is opened a way
95kg/t is reduced to removal of impurities consumption lime.
Embodiment 3
Certain aurin (in) ore deposit sulfur-bearing 10.8%, iron content 14.4%, containing arsenic 0.9%, carbonate containing (with calcium carbonate)
25.04%, pressure oxidation rear oxidation liquid produces sour 132kg/t, starts by 113kg/t elder generations enriching sulfuric acid, after by the oxygen of solid-liquor separation
Change leachate 6 and return to stirring acidifying decomposing carbonate, acidifying solution 3 first adds lime to start to removal of impurities is neutralized by 132kg/t, after by liquid
Admittedly the remaining Oxidation Leaching liquid 6 separated is returned to neutralize to remove and used mixedly.
Using the method for the present invention, concrete operation step and technological parameter are as follows：
(1) pressureleaching solution contains H2SO431g/L, containing Fe3+18.2g/L。
(2) the aurin ore pulp and step D Oxidation Leaching liquid 6 entered before autoclave is stirred acidification reaction, decomposes carbon
Hydrochlorate, react and carried out in the tank diameter of three series connection, be filled with air from trench bottom, the aeration quantity of three grooves is controlled as
10、8.5、5.5Nm3/ (㎡ h), ore pulp adds from No.1 groove, flows automatically to No. three grooves by groove, leachate divides multiple spot from No.1 groove
Distribution adds, and Oxidation Leaching liquid 6 presses V=980 ω/CH2SO4+2.625CFe3+=3.12m3/ t is added, and is aoxidized by finely tuning
The addition flow of leachate 6, the exit pH scope of one, two, No. three groove ore pulp of control is respectively 1.8,2.3,2.8.
(3) ore pulp 1 after the acidifying after step A decomposing carbonates is transported to concentrator from No. three grooves and settled, dense
Spend and be acidified ore pulp underflow 2 for solid masses 45-50% and enter autoclave pressurization oxidation, 205 DEG C, partial pressure of oxygen 0.5MPa of oxidizing temperature,
Residence time 60min, aoxidize the direct return to step A three-levels stirring acidifying replacement sulfur of rear oxidation leachate 6 after the solid-liquor separation of ore pulp 4
Neutralize to remove after acid and step B are dense and use mixedly.
This example can reach system acid balance, decomposing carbonate process not additional sulfuric acid after startup, during Oxidation Leaching liquid 6 is opened a way
75kg/t is reduced to removal of impurities consumption lime.
As described above, the present invention can be better realized.Above-described embodiment is only the optimal embodiment of the present invention, but this
The embodiment of invention is simultaneously not restricted to the described embodiments, and other are done under Spirit Essence and principle without departing from the present invention
Change, modify, replace, combine, simplify, should be equivalent substitute mode, be included in protection scope of the present invention.
Claims (3)
1. the method for comprehensive utilization of iron ion in a kind of arsenic-containing gold ore pressureleaching solution, applicable object are sulfur-bearing 10-16%, arsenic
0.8-3.5%, with calcium carbonate carbonate 25-45% aurin (in) the Oxidation Leaching liquid of ore deposit, concrete technology step and condition
It is as follows：
A. three-level stirring acidifying：By aurin (in) ore deposit stirs with using the Oxidation Leaching liquid (6) that step D is obtained after first being started with sulfuric acid instead
Slurry and acidification reaction are mixed, decomposing carbonate, reacts and is carried out in one to No. three tank diameter of series connection, from the bottom of three tank diameters
Portion is filled with air, and ore pulp adds from No.1 groove, and No. three grooves, sulfuric acid or even Oxidation Leaching liquid (6) are flowed automatically to from No.1 groove point by groove
Multiple spot is distributed to be added, and addition presses formula V=980 ω/CH2SO4+2.625CFe3+Calculate, in formula：
V(m3/ t) --- the Oxidation Leaching liquid product that ore per ton adds, it is allowed to departure ± 10%
ω (%) --- with calcium carbonate carbonate content in ore
CH2SO4(kg/m3) --- H in leachate2SO4Concentration
CFe3+(kg/m3) --- Fe in leachate3+Concentration
The exit pH scope for controlling one, two, No. three tank diameter ore pulp is respectively 1.5-2.2,2.2-2.5,2.5-3.2, obtains three
Ore pulp (1) after the acidifying of number tank diameter.
B. it is dense：The ore pulp (1) after acidifying is transported into concentrator from No. three tank diameters to be settled, obtains acidifying solution (3) and concentration
For the acidifying ore pulp underflow (2) of solid masses 45~50%, then first add to acidifying solution (3) and to use step D instead after alkali starts and obtain
Remaining Oxidation Leaching liquid (6) carry out neutralization removal of impurities, slag (7) must be neutralized and enter Tailings Dam；
C. pressure oxidation：Acidifying ore pulp underflow (2) is entered into autoclave and carries out pressure oxidation, 200-220 DEG C of oxidizing temperature, partial pressure of oxygen
0.4-1.0MPa, residence time 50-100min, ore pulp (4) must be aoxidized；
D. solid-liquor separation：Ore pulp (4) solid-liquor separation will be aoxidized, H must be contained2SO430-50g/L、Fe3+18-25g/L Oxidation Leaching
Liquid (6) and oxidizing slag (5), Oxidation Leaching liquid (6) are stored in that solution tank is stand-by or the stirring acidifying of direct return to step A three-levels substitutes
Neutralized after sulfuric acid and step B are dense except using mixedly, other process otherwise processeds can be entered by obtaining oxidizing slag (5).
2. according to the method for claim 1, it is characterized in that the aeration quantity of tri- tank diameters of step A be respectively 10-12,
8-10、4-6Nm3/㎡·h。
3. according to the method for claim 1, it is characterized in that the alkali of the neutralization removal of impurities in the step B is lime.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109932268A (en) * | 2019-02-14 | 2019-06-25 | 紫金矿业集团股份有限公司 | Siderotil content assaying method in the slugging of gold mine pressurised oxygen and cyanide residue |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106119566A (en) * | 2016-08-18 | 2016-11-16 | 紫金矿业集团股份有限公司 | A kind of hot pressing recovery method of the difficult gold mine of arsenic-containing sulphur-containing |
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- 2017-10-27 CN CN201711020686.0A patent/CN107881342B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106119566A (en) * | 2016-08-18 | 2016-11-16 | 紫金矿业集团股份有限公司 | A kind of hot pressing recovery method of the difficult gold mine of arsenic-containing sulphur-containing |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109932268A (en) * | 2019-02-14 | 2019-06-25 | 紫金矿业集团股份有限公司 | Siderotil content assaying method in the slugging of gold mine pressurised oxygen and cyanide residue |
| CN109932268B (en) * | 2019-02-14 | 2021-06-08 | 紫金矿业集团股份有限公司 | Method for measuring content of iron vitriol in gold ore pressure oxidation slag and cyaniding slag |
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