CN102703701B - Method for treating cupric oxide or zinc oxide ores by adopting agitation ammonia leaching and infiltration basin ammonia leaching in combination - Google Patents

Method for treating cupric oxide or zinc oxide ores by adopting agitation ammonia leaching and infiltration basin ammonia leaching in combination Download PDF

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CN102703701B
CN102703701B CN201210204869.9A CN201210204869A CN102703701B CN 102703701 B CN102703701 B CN 102703701B CN 201210204869 A CN201210204869 A CN 201210204869A CN 102703701 B CN102703701 B CN 102703701B
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ammonia
ore
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immersion liquid
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CN102703701A (en
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周庆华
纪翠翠
马彩雯
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Industry Management Ltd., Kunming University of Science and Technology
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Kunming University of Science and Technology
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Abstract

The invention discloses a method for treating cupric oxide or zinc oxide ores by adopting agitation ammonia leaching and infiltration basin ammonia leaching in combination. The method is realized through the following steps: firstly fine crushing raw ores, and then dividing the materials into stream ores and fine ore pulp by adopting the combination screening method, wherein the stream ores undertake infiltration basin ammonia leaching by a thick ammonia leaching solution under the conditions of normal temperature, normal pressure and airtightness, and the fine ore pulp undertakes the first stage of agitation ammonia leaching by a mediate ammonia leaching solution under the conditions of normal temperature, normal pressure and airtightness; the fine ores and the stream ores after preliminary leaching undertake wet-type grinding and grading by a mediate ammonia leaching solution; and finally, the fine ore pulp undertakes the second stage of agitation ammonia leaching under the conditions of normal temperature, normal pressure and airtightness. The method has the advantages of improving the leaching efficiency of copper or zinc, reducing the solid-liquid separation ore amount of the fine ores, reducing the volatilization loss during repeated use of ammonia and improving the industrial health conditions; and further, the process has certain flexibility, so that the energy consumption for ore grinding is saved.

Description

Stir ammonia and soak the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia
Technical field
The present invention relates to a kind of method that leaches material with ammonia, particularly relate to a kind of ammonia that stirs and soak the method for soaking coupling with diffusion cell ammonia, for the treatment of containing high refractory oxidized copper ore or the zinc oxide ore of basic gangue, belong to mineral processing technical field.
Background technology
For containing high refractory oxidized copper ore and the zinc oxide ore of basic gangue, if use flotation process processing, can be subject to the interference of sludge, make reagent consumption large, the rate of recovery is low; If use pickling process processing, because acid will be reacted with basic gangue, acid consumption is too high, does not calculate economically; And with the processing of NPT ammonia leached method, thering is the selectivity of leaching good, gangue does not consume medicament, the feature that leach liquor impurity is few.
For containing the high refractory oxidized copper ore of basic gangue, adopt the direct ammonia of normal temperature and pressure to soak the free cupric oxide that can first reclaim in raw ore, existing description in this normal temperature normal pressure ammonia infusion-extraction-electrodeposition-slag infusion flotation that is CN200510010932.5 at application number, this method has obtained industrial application and has created economic benefit, the Xuan Ye factory of successively having different scales at Dongchuan District, Yunnan Province, its Leaching way is after wet grinding, to stir ammonia to soak, and returns not ammonia still process of liquid to leaching.
For containing the high difficult dressing zinc oxide ore of basic gangue, adopt NPT ammonia leached, can effectively leach the zinc oxide in ore, existing description in the method for this combined treatment of high calcium and magnesium low-grade oxidized lead zinc ore by means of concentration that is CN200910094204.5 at application number, its Leaching way is after wet grinding, to stir ammonia to soak.
Compare mutually, ammonia leaching process, for the treatment of the reducing roasting sand of red soil nickel ore, needs to heat to 50~60 DEG C, and need fill atmospheric oxidation, adds gentle inflation and makes to give vent to anger and take ammonia out of.Ammonia leaching process, for the treatment of high-alkali cupric oxide ore and high-alkali zinc oxide ore, can leach at normal temperatures and pressures, does not need to fill atmospheric oxidation, and this is convenient to live in leaching Working Procedure Controlling the volatilization of ammonia.
Leach the valuable metal of oxidized ore with ammonia, although the selectivity of its leaching is good, again discharged again after extraction or displacement by the ammonia of complexing; But under the condition of normal temperature and pressure, by forming [Cu (NH 3) 4] 2+count the carrying out of accelerating this reaction with the ammonia that exceeds 10~20 times of complex reactions; By forming [[Zn (NH 3) 4] 2+count the carrying out of accelerating this reaction with the ammonia that exceeds 4~8 times of complex reactions.After metal in leach liquor is extracted, ammonia wherein must be returned use.The ammonia that recycling is returned in liquid has two kinds of modes, and one is to carry out ammonia still process to returning liquid containing ammonia, and its energy consumption of heating is higher, should need not as far as possible; Another kind is directly to use suitable place by returning liquid containing ammonia, should avoid the volatilization loss of ammonia for this reason as far as possible.
Consider containing ammoniacal liquor return to place time, should analyze the water situation of An Jin factory.In the time that whole system water reaches balance, main water should be the ammoniacal liquor that contains recycling, need not return liquid and use instead and add new water containing ammonia in some link if wanted, its amount of water only can with leach after the water yield taken away of filter residue suitable, if new water is added too much, will cause system to occur that water expands, and haves no alternative but to arrange containing ammoniacal liquor thus outward, so just have outer row's loss of ammonia, this also should be avoided as far as possible.
By existing wet grinding mode, its wet grinding system and slurry preparing system are integrated, if not to returning liquid ammonia still process, avoid again system to occur that water expands and causes the outer row of ammonia to lose, just the dense ammonia that is applicable to leaching needs must be entered to immersion liquid joins in wet grinding system, but it is airtight that the wet grinding equipment of this system and screw classifying equipment are all difficult to, and ammonia is wanted volatilization loss; Wet grinding also makes ore pulp heat up, and this has aggravated again the volatilization of ammonia.So, before not only leaching, need to add more ammonia, production cost is raise, and the stimulation ammonia odor volatilizing has also worsened the industrial hygiene condition of production plant.The way of improving is, classifier for milling ore is covered, more separately establishes blower fan tail gas is evacuated to absorption tower, but ammonia by Dilution air after, its assimilated efficiency is not high.
Soak for ammonia, agitation leach is the technology of existing application, lump ore dump leaching required time is long and be difficult to airtight, placer diffusion cell leaching required time is suitable and be easy to airtight, therefore, soak by stirring ammonia that to soak in conjunction with application with placer diffusion cell ammonia be a new technology that needs development, this technology need solve the problem that the placer of ammonia before soaking and particulate ore deposit separate, so that placer heap has good perviousness, making to stir ore pulp does not have placer deep gouge phenomenon yet.
Summary of the invention
The invention provides a kind of ammonia that stirs and soak the method for soaking coupling with diffusion cell ammonia, for the treatment of containing high refractory oxidized copper ore or the zinc oxide ore of basic gangue, main purpose be for industrializing implementation not only improved copper or zinc leaching yield, but also reduce the volatilization loss of circulation ammonia and reduce the solid-liquid separation ore deposit amount to particulate ore deposit.
The present invention realizes by following technical proposal: a kind of ammonia that stirs soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, comprise that ultrafine grinding, combination screening, placer diffusion cell ammonia soak, first paragraph stirs that ammonia soaks, placer latter stage ore grinding and second segment stir ammonia and soak, and specifically passes through following each step:
(1) ultrafine grinding: be 2~3mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 3~5%;
(2) combination screening: to the material of processing through step (1), first carry out dry screen and be divided into that upper strata contains mud medium sand containing mud xalsonte, middle level and lower floor's particulate is done ore deposit; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out in confined conditions leading portion wet screening to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, is that 3 ︰ 1~5 ︰ 1 calculate by the mass ratio of the particulate ore pulp II of itself and output;
(3) placer diffusion cell ammonia soaks: in step (2) gained placer, be that 2 ︰ 1~3 ︰ 1 add dense ammonia to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 18~36h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion is washed ore body, and carry out respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer;
(4) first paragraph stir ammonia soak: step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 1.5~2.5h at normal temperature and pressure air tight condition, then after solid-liquid separation obtains dense ammonia leaching solution II and just soaks particulate ore deposit;
(5) placer latter stage ore grinding: add middle ammonia to enter immersion liquid in step (4) gained first soaked rear particulate ore deposit and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its fineness is that the powder quality that is less than 74 μ m accounts for 75~85%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that 2 ︰ 1~3 ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) second segment stirring ammonia soaks: the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation; To treat that again washery slag is that 3 ︰ 1 use washing lotions are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation, and complete the stirring ammonia of cupric oxide or zinc oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
The raw ore of described step (1) is the raw ore through front fragmentation, comprises the refractory oxidized copper ore high containing basic gangue, contains the high difficult dressing zinc oxide ore of basic gangue.
The dry screen of described step (2) is divided into bilayer, and the screen-aperture of upper sieve is 0.8~1.2mm, and the screen-aperture of lower screen is 0.3~0.5mm; The screen-aperture of leading portion wet screening is 0.5~0.8mm; The screen-aperture of back segment wet screening is 0.3~0.5mm.
The dense ammonia of described step (2) and (3) enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ 4~1 ︰ 3, its total ammonia concentration is 2~4mol/L to cupric oxide ore, is 3~6mol/L to zinc oxide ore; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form.
Total ammonia concentration that the middle ammonia of described step (3) and (5) enters immersion liquid is 1~2mol/L to cupric oxide ore, is 1.5~3mol/L to zinc oxide ore; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form.
Rare ammonia elutant II of the middle ammonia leaching solution of the dense ammonia leaching solution I of described step (3) gained, the dense ammonia leaching solution II of step (4) gained, step (6) gained, rare ammonia elutant I of step (3) gained, step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, be re-used as dense ammonia and enter immersion liquid or middle ammonia and enter that step (2) is returned in immersion liquid, (3) and (5) recycle.
The washing lotion of described step (3) and (6) is clear water.
Described rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
The sand liquid of described step (3), (4) and (6) separates and solid-liquid separation is all carried out in confined conditions.
The small ammonia of high-alkali cupric oxide ore or high-alkali zinc oxide ore is soaked to experimental study to be shown: under normal temperature and pressure air tight condition, only depend on single hop ammonia to soak to levigate ore pulp, owing to being subject to leach the obstruction of metal ion, even total strengthen into the ammonia concentration of immersion liquid and be also not enough to improve by a relatively large margin leaching yield; And adopt two sections of ammonia to soak, second segment wherein leaches, with in ammonia enter immersion liquid just can be larger to the increase rate of leaching yield.This is because first enter immersion liquid with dense ammonia and leach more valuable metal, and solid-liquid separation makes the metal ion leaching separate with leached mud, and second segment leaches the concentration of metal ions reduction of required dissolving afterwards, just can use middle ammonia instead and enter immersion liquid and improve leaching yield.
Further comparative experimental research shows: in two sections of ammonia soak, change first paragraph leach for p-3mm~
The placer of+0.5mm enters immersion liquid with dense ammonia and leaches, second segment leach still for to levigate ore pulp with in ammonia enter immersion liquid and leach, also can reach to ore first levigate, two sections of ammonia soak suitable leaching effect again.Although this is can accelerate the speed of Leaching reaction, make most valuable minerals expose the carrying out that just can contact to facilitate with leaching agent reaction in muck mode because valuable mineral is attenuated with grinding mode.
To stirring after whole ore wet grindings compared with the technology that ammonia soaks, the present invention has following advantage with existing:
1, be ultrafine grinding to the final stage muck of ore, this is because this class ore contains more basic gangue and sludge, enbrittle, ultrafine grinding had both been suitable for existing muck equipment to be realized cost-effectively, be conducive to again improve the leaching velocity that soak placer diffusion cell, be also conducive to how broken few mill to save energy consumption;
2, arrange at the screen-aperture of combination screening, suitably put slightly the screening separation size in placer and particulate ore deposit, this is convenient to reduce fluid volume in the process of screening and reduces ammonia volatilization, and to sieving fine sand part thicker in lower particulate ore pulp, also have classification-rear means of grind-soaking again to strengthen leaching;
3, dense ammonia enters that immersion liquid flows through that easily airtight wet screening, placer diffusion cell ammonia soak, first paragraph stirs that ammonia soaks, need in the link of liquid storage between solid-liquid separation operation and operation, do not flow through in difficult airtight wet grinding graded operation, this firmly volatilization loss of ammonia more easy to control, can improve industrial hygiene condition;
4, placer is carried out to diffusion cell ammonia and soak, sand liquid wherein separates more easier than the solid-liquid separation in particulate ore deposit, only need allow liquid self-flowing ooze out, and just can separate with placer, and this is convenient to control the volatilization loss of ammonia, can improve industrial hygiene condition;
5, reduce the Fine fraction of ore amount that enters two sections of ammonia and soak middle first paragraph, to avoid the capacious solid-liquid separating equipment of excessive use, saved investment;
6, flow process has certain handiness, can accept or reject according to the characteristic of just soaking rear placer; If there is not much left for placer, set it as thick tailings, this has just saved power consume; If placer is last available, latter stage ore grinding and two sections of ammonia are soaked and use, this is conducive to improve leaching yield;
7, can return liquid with middle ammonia because second segment leaches, so be added to grinding classification system, to return the ammonia content of liquid lower, and this has just reduced the volatilization loss of ammonia in grinding classification system.
Brief description of the drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
Further illustrate content of the present invention below in conjunction with embodiment, but these examples do not limit the scope of the invention.
Embodiment 1
Contain the high refractory oxidized copper ore of basic gangue: cupric 1.65%, free cupric oxide distributive law is 70.30%, is 28.48% in conjunction with copper distributive law, cupric sulfide distributive law is 1.22%, CaO:28.12%, MgO:2.80%, Fe:7.97%, Al 2o 3: 0.90%, SiO 2: 9.28%(is quality percentage composition, for drying rear result of laboratory test, lower same).
By above-mentioned raw ore after front fragmentation, the processing step processing by following:
(1) ultrafine grinding: be 3mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 4%;
(2) combination screening: to the material of processing through step (1), first carry out dry screen and divide (screen-aperture of upper sieve is 1.0mm, and the screen-aperture of lower screen is 0.4mm) to do ore deposit containing mud xalsonte, middle level containing mud medium sand and lower floor's particulate to be divided into upper strata; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out leading portion wet screening in confined conditions (screen-aperture of leading portion wet screening is 0.7mm) to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening (screen-aperture of back segment wet screening is 0.4mm) to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, is that 3.5 ︰ 1 calculate by the mass ratio of the particulate ore pulp II of itself and output; Dense ammonia enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ 3, its total ammonia concentration is 3mol/L; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(3) placer diffusion cell ammonia soaks: in step (2) gained placer, be that 2.5 ︰ 1 add the dense ammonia identical with step (2) to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 30h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid in confined conditions again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion clear water washs ore body, and carry out in confined conditions respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer; Wherein, to enter total ammonia concentration of immersion liquid be 1.5mol/L to middle ammonia; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(4) first paragraph stirs ammonia and soaks: step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 2.0h at normal temperature and pressure air tight condition, then particulate ore deposit after solid-liquid separation obtains dense ammonia leaching solution II and just soaks in confined conditions;
(5) placer latter stage ore grinding: add the middle ammonia identical with step (3) to enter immersion liquid in step (4) gained first soaked rear particulate ore deposit and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its fineness is that the powder quality that is less than 74 μ m accounts for 85%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that 2 ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) second segment stirring ammonia soaks: the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation in confined conditions; To treat that again washery slag is that 3 ︰ 1 use washing lotion clear water are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation in confined conditions, and complete the stirring ammonia of cupric oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
Rare ammonia elutant II of the middle ammonia leaching solution of the dense ammonia leaching solution I of step (3) gained, the dense ammonia leaching solution II of step (4) gained, step (6) gained, rare ammonia elutant I of step (3) gained, step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, be re-used as dense ammonia and enter immersion liquid or middle ammonia and enter that step (2) is returned in immersion liquid, (3) and (5) recycle; Rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
Design calculation is taking small-scale test research as foundation, and lowering a little its total leaching yield design objective is 61.00%, and the free cupric oxide in ore is fully leached, and is leached in conjunction with copper-base is few, and cupric sulfide is partly leached.
The index of each product of described step (3), (4), (6) is in table 1 and table 2, and these indexs calculate out with leaching yield and complementary design index, and complementary design index comprises liquid-solid mass ratio, filter residue water ratio.
Each operation of table 1 embodiment 1 and the design objective of solid product
The liquid phase design objective of each product of table 2 embodiment 1
Embodiment 2
Contain the high difficult dressing zinc oxide ore of basic gangue: containing zinc 9.75%, the distributive law of carbonate and sulphate form zinc is 82.75%, and silicate form zinc distributive law is 14.87%, the distributive law of sulphided form zinc is 2.38%, Pb:1.86%, CaO:15.62%, Fe:l3.73%, MgO:1.84%, Al 2o 3: 2.90%, Si0 2: 13.76%.
By above-mentioned raw ore after front fragmentation, the processing step processing by following:
(1) ultrafine grinding: be 3mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 4%;
(2) combination screening: to the material of processing through step (1), first carry out dry screen and divide (screen-aperture of upper sieve is 1.0mm, and the screen-aperture of lower screen is 0.4mm) to do ore deposit containing mud xalsonte, middle level containing mud medium sand and lower floor's particulate to be divided into upper strata; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out leading portion wet screening in confined conditions (screen-aperture of leading portion wet screening is 0.7mm) to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening (screen-aperture of back segment wet screening is 0.4mm) to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, is that 4 ︰ 1 calculate by the mass ratio of the particulate ore pulp II of itself and output; Dense ammonia enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ 3, its total ammonia concentration is 4.5mol/L; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(3) placer diffusion cell ammonia soaks: in step (2) gained placer, be that 3 ︰ 1 add the dense ammonia identical with step (2) to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 24h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid in confined conditions again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion clear water washs ore body, and carry out in confined conditions respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer; Wherein, to enter total ammonia concentration of immersion liquid be 2mol/L to middle ammonia; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(4) first paragraph stirs ammonia and soaks: step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 2h at normal temperature and pressure air tight condition, then particulate ore deposit after solid-liquid separation obtains dense ammonia leaching solution II and just soaks in confined conditions;
(5) placer latter stage ore grinding: add the middle ammonia identical with step (3) to enter immersion liquid in step (4) gained first soaked rear particulate ore deposit and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its fineness is that the powder quality that is less than 74 μ m accounts for 80%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that 3 ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) second segment stirring ammonia soaks: the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation in confined conditions; To treat that again washery slag is that 3 ︰ 1 use washing lotion clear water are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation in confined conditions, and complete the stirring ammonia of zinc oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
Rare ammonia elutant II of the middle ammonia leaching solution of the dense ammonia leaching solution I of step (3) gained, the dense ammonia leaching solution II of step (4) gained, step (6) gained, rare ammonia elutant I of step (3) gained, step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, be re-used as dense ammonia and enter immersion liquid or middle ammonia and enter that step (2) is returned in immersion liquid, (3) and (5) recycle; Rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
Design calculation is taking small-scale test research as foundation, and lowering a little its total leaching yield design objective is 77.00%, and the carbonate in ore and the zinc of sulphate form are fully leached, and is leached but the zincode of silicate and sulphided form is few.The index of each product of described step (3), (4), (6) is in table 3 and table 4.
Each operation of table 3 embodiment 2 and the design objective of solid product
The liquid phase design objective of each product of table 4 embodiment 2
Embodiment 3
Contain the high refractory oxidized copper ore of basic gangue: cupric 0.78%, free cupric oxide distributive law is 79.82%, and copper combination rate is 8.27%, and cupric sulfide distributive law is 11.91%, CaO:16.42%, MgO:7.74%, Al 2o 3: 6.87%, SiO 2: 18.37%, Fe 2o 3: 5.33%.
By above-mentioned raw ore after front fragmentation, the processing step processing by following:
(1) ultrafine grinding: be 3mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 5%;
(2) combination screening: to the material of processing through step (1), first carry out dry screen and divide (screen-aperture of upper sieve is 1.2mm, and the screen-aperture of lower screen is 0.5mm) to do ore deposit containing mud xalsonte, middle level containing mud medium sand and lower floor's particulate to be divided into upper strata; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out leading portion wet screening in confined conditions (screen-aperture of leading portion wet screening is 0.8mm) to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening (screen-aperture of back segment wet screening is 0.5mm) to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, is that 3 ︰ 1 calculate by the mass ratio of the particulate ore pulp II of itself and output; Dense ammonia enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ 3, its total ammonia concentration is 2mol/L; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(3) placer diffusion cell ammonia soaks: in step (2) gained placer, be that 2 ︰ 1 add the dense ammonia identical with step (2) to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 20h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid in confined conditions again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion clear water washs ore body, and carry out in confined conditions respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer; Wherein, total ammonia concentration that middle ammonia enters immersion liquid is 1mol/L, and employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and forms;
(4) first paragraph stirs ammonia and soaks: step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 1.5h at normal temperature and pressure air tight condition, then particulate ore deposit after solid-liquid separation obtains dense ammonia leaching solution II and just soaks in confined conditions;
(5) placer latter stage ore grinding: add the middle ammonia identical with step (3) to enter immersion liquid in step (4) gained first soaked rear particulate ore deposit and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its fineness is that the powder quality that is less than 74 μ m accounts for 75%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that 2 ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) second segment stirring ammonia soaks: the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation in confined conditions; To treat that again washery slag is that 3 ︰ 1 use washing lotion clear water are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation in confined conditions, and complete the stirring ammonia of cupric oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
Rare ammonia elutant II of the middle ammonia leaching solution of the dense ammonia leaching solution I of step (3) gained, the dense ammonia leaching solution II of step (4) gained, step (6) gained, rare ammonia elutant I of step (3) gained, step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, be re-used as dense ammonia and enter immersion liquid or middle ammonia and enter that step (2) is returned in immersion liquid, (3) and (5) recycle; Rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
Small-scale test research shows: its total leaching yield is 71.24%, and the free cupric oxide in ore is fully leached, and is leached in conjunction with copper-base is few, and cupric sulfide is partly leached.
Embodiment 4
Contain the high difficult dressing zinc oxide ore of basic gangue: containing zinc 4.86%, the distributive law of carbonate and sulphate form zinc is 92.24%, and silicate form zinc distributive law is 4.54%, the distributive law of sulphided form zinc is 3.22%, Pb:0.78%, CaO:17.35%, Fe:8.84%, MgO:2.97%, Al 2o 3: 3.69%, Si0 2: 15.57%.
By above-mentioned raw ore after front fragmentation, the processing step processing by following:
(1) ultrafine grinding: be 3mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 4%;
(2) combination screening: to the material of processing through step (1), first carry out dry screen and divide (screen-aperture of upper sieve is 1.0mm, and the screen-aperture of lower screen is 0.4mm) to do ore deposit containing mud xalsonte, middle level containing mud medium sand and lower floor's particulate to be divided into upper strata; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out leading portion wet screening in confined conditions (screen-aperture of leading portion wet screening is 0.7mm) to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening (screen-aperture of back segment wet screening is 0.4mm) to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, is that 3.5 ︰ 1 calculate by the mass ratio of the particulate ore pulp II of itself and output; Dense ammonia enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ 4, its total ammonia concentration is 3mol/L; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(3) placer diffusion cell ammonia soaks: in step (2) gained placer, be that 2.5 ︰ 1 add the dense ammonia identical with step (2) to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 18h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid in confined conditions again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion clear water washs ore body, and carry out in confined conditions respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer; Wherein, to enter total ammonia concentration of immersion liquid be 1.5mol/L to middle ammonia; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(4) first paragraph stirs ammonia and soaks: step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 1.5h at normal temperature and pressure air tight condition, then particulate ore deposit after solid-liquid separation obtains dense ammonia leaching solution II and just soaks in confined conditions;
(5) placer latter stage ore grinding: add the middle ammonia identical with step (3) to enter immersion liquid in step (4) gained first soaked rear particulate ore deposit and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its fineness is that the powder quality that is less than 74 μ m accounts for 75%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that 3 ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) second segment stirring ammonia soaks: the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation in confined conditions; To treat that again washery slag is that 3 ︰ 1 use washing lotion clear water are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation in confined conditions, and complete the stirring ammonia of zinc oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
Rare ammonia elutant II of the middle ammonia leaching solution of the dense ammonia leaching solution I of step (3) gained, the dense ammonia leaching solution II of step (4) gained, step (6) gained, rare ammonia elutant I of step (3) gained, step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, be re-used as dense ammonia and enter immersion liquid or middle ammonia and enter that step (2) is returned in immersion liquid, (3) and (5) recycle; Rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
Small-scale test research shows: its total leaching yield is 75.39%, and the zinc carbonate in ore and zinc sulfate are fully leached, and zinc silicate is seldom leached, and zinc sulphide is partly leached.
Embodiment 5
Contain the high refractory oxidized copper ore of basic gangue: cupric 2.26%, free cupric oxide distributive law is 76.64%, and copper combination rate is 19.34%, and cupric sulfide distributive law is 4.02%, CaO:24.15%, MgO:4.08%, Al 2o 3: 2.36%, SiO 2: 7.74%, Fe 2o 3: 12.61%.
By above-mentioned raw ore after front fragmentation, the processing step processing by following:
(1) ultrafine grinding: be 2mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 3%;
(2) combination screening: to the material of processing through step (1), first carry out dry screen and divide (screen-aperture of upper sieve is 0.8mm, and the screen-aperture of lower screen is 0.3mm) to do ore deposit containing mud xalsonte, middle level containing mud medium sand and lower floor's particulate to be divided into upper strata; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out leading portion wet screening in confined conditions (screen-aperture of leading portion wet screening is 0.5mm) to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening (screen-aperture of back segment wet screening is 0.3mm) to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, is that 4 ︰ 1 calculate by the mass ratio of the particulate ore pulp II of itself and output; Dense ammonia enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ 3, its total ammonia concentration is 4mol/L, adopts the allotment that adds water of strong aqua, volatile salt or bicarbonate of ammonia to form;
(3) placer diffusion cell ammonia soaks: in step (2) gained placer, be that 3 ︰ 1 add the dense ammonia identical with step (2) to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 36h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid in confined conditions again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion clear water washs ore body, and carry out in confined conditions respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer; Wherein, total ammonia concentration that middle ammonia enters immersion liquid is 2mol/L, and employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and forms;
(4) first paragraph stirs ammonia and soaks: step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 2h at normal temperature and pressure air tight condition, then particulate ore deposit after solid-liquid separation obtains dense ammonia leaching solution II and just soaks in confined conditions;
(5) placer latter stage ore grinding: add the middle ammonia identical with step (3) to enter immersion liquid in step (4) gained first soaked rear particulate ore deposit and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its fineness is that the powder quality that is less than 74 μ m accounts for 85%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that 2.5 ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) second segment stirring ammonia soaks: the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation in confined conditions; To treat that again washery slag is that 3 ︰ 1 use washing lotion clear water are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation in confined conditions, and complete the stirring ammonia of cupric oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
Rare ammonia elutant II of the middle ammonia leaching solution of the dense ammonia leaching solution I of step (3) gained, the dense ammonia leaching solution II of step (4) gained, step (6) gained, rare ammonia elutant I of step (3) gained, step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, be re-used as dense ammonia and enter immersion liquid or middle ammonia and enter that step (2) is returned in immersion liquid, (3) and (5) recycle; Rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
Small-scale test research shows: its total leaching yield is 69.57%, and the free cupric oxide in ore is fully leached, and is leached in conjunction with copper-base is few, and cupric sulfide is partly leached.
Embodiment 6
Contain the high difficult dressing zinc oxide ore of basic gangue: containing zinc 12.66%, the distributive law of carbonate and sulphate form zinc is 77.57%, and silicate form zinc distributive law is 21.35%, the distributive law of sulphided form zinc is 1.08%, Pb:2.36%, CaO:13.75%, Fe:11.66%, MgO:2.84%, Al 2o 3: 7.90%, Si0 2: 12.76%.
By above-mentioned raw ore after front fragmentation, the processing step processing by following:
(1) ultrafine grinding: be 3mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 5%;
(2) combination screening: to the material of processing through step (1), first carry out dry screen and divide (screen-aperture of upper sieve is 1.2mm, and the screen-aperture of lower screen is 0.5mm) to do ore deposit containing mud xalsonte, middle level containing mud medium sand and lower floor's particulate to be divided into upper strata; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out leading portion wet screening in confined conditions (screen-aperture of leading portion wet screening is 0.8mm) to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening (screen-aperture of back segment wet screening is 0.5mm) to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, is that 5 ︰ 1 calculate by the mass ratio of the particulate ore pulp II of itself and output; Dense ammonia enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ 4, its total ammonia concentration is 6mol/L; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(3) placer diffusion cell ammonia soaks: in step (2) gained placer, be that 3 ︰ 1 add the dense ammonia identical with step (2) to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 30h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid in confined conditions again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion clear water washs ore body, and carry out in confined conditions respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer; Wherein, to enter total ammonia concentration of immersion liquid be 3mol/L to middle ammonia; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form;
(4) first paragraph stirs ammonia and soaks: step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 2.5h at normal temperature and pressure air tight condition, then particulate ore deposit after solid-liquid separation obtains dense ammonia leaching solution II and just soaks in confined conditions;
(5) placer latter stage ore grinding: add the middle ammonia identical with step (3) to enter immersion liquid in step (4) gained first soaked rear particulate ore deposit and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its fineness is that the powder quality that is less than 74 μ m accounts for 85%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that 3 ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) second segment stirring ammonia soaks: the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation in confined conditions; To treat that again washery slag is that 3 ︰ 1 use washing lotion clear water are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation in confined conditions, complete the stirring ammonia of cupric oxide or zinc oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
Rare ammonia elutant II of the middle ammonia leaching solution of the dense ammonia leaching solution I of step (3) gained, the dense ammonia leaching solution II of step (4) gained, step (6) gained, rare ammonia elutant I of step (3) gained, step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, be re-used as dense ammonia and enter immersion liquid or middle ammonia and enter that step (2) is returned in immersion liquid, (3) and (5) recycle; Rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
Small-scale test research shows: its total leaching yield is 72.28%, and the zinc carbonate in ore and zinc sulfate are fully leached, and zinc silicate is seldom leached, and zinc sulphide is partly leached.

Claims (9)

1. stir ammonia and soak a method of soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that through following each step:
(1) be 2~3mm by raw ore ultrafine grinding to granularity, the mass percent of controlling moisture is 3~5%;
(2) to the material of processing through step (1), first carry out dry screen be divided into upper strata containing mud xalsonte, middle level containing mud medium sand and the dry ore deposit of lower floor's particulate; Again containing adding dense ammonia to enter immersion liquid in mud xalsonte, and carry out in confined conditions leading portion wet screening to be divided into xalsonte and cement mortar; Then add containing mud medium sand and carry out in confined conditions back segment wet screening to be divided into medium sand and particulate ore pulp I with this cement mortar; Finally xalsonte and medium sand are merged into placer, the dry ore deposit of particulate and particulate ore pulp I are merged into particulate ore pulp II; In this step, dense ammonia enters the add-on of immersion liquid, by the mass ratio of the particulate ore pulp II of itself and output for (3~5) ︰ 1 calculate;
(3) in step (2) gained placer, be that (2~3) ︰ 1 add dense ammonia to enter immersion liquid by liquid-solid mass ratio, the mode leaching with counter flow in series under normal temperature and pressure air tight condition is carried out diffusion cell and is leached 18~36h, separate and obtain dense ammonia leaching solution I and treat washed-out sand through sand liquid again, then by liquid-solid mass ratio be 1 ︰ 1 successively with in ammonia enter immersion liquid, washing lotion is treated washed-out sand and is washed, and carry out respectively sand liquid separate obtain in ammonia elutant, rare ammonia elutant I and just soak rear placer;
(4) step (2) gained particulate ore pulp II is carried out to first paragraph agitation leach 1.5~2.5h at normal temperature and pressure air tight condition, then after solid-liquid separation obtains dense ammonia leaching solution II and just soaks particulate ore deposit;
(5) in step (4) gained first soaked rear particulate ore deposit, add middle ammonia to enter immersion liquid and carry out pre-classification, its classification sand setting and step (3) gained just soak after rear placer merging, the middle ammonia elutant that adds again middle ammonia to enter immersion liquid and step (3) gained is carried out wet grinding and Inspection graduation, the Grading Overflow of pre-classification and Inspection graduation is levigate ore pulp, and its granularity is that the powder quality that is less than 74 μ m accounts for 75~85%; In in this step, ammonia enters the add-on of immersion liquid or middle ammonia and enters the add-on of immersion liquid and middle ammonia elutant, is that (2~3) ︰ 1 calculate by the mass ratio of the levigate ore pulp of itself and output;
(6) the levigate ore pulp of step (5) gained is entered to second segment agitation leach 2.0h under normal temperature and pressure air tight condition, then obtain middle ammonia leaching solution and treat washery slag through solid-liquid separation; To treat that again washery slag is that 3 ︰ 1 use washing lotions are sized mixing and wash by liquid-solid mass ratio, then obtain rare ammonia elutant II and thin tailings through solid-liquid separation, and complete the stirring ammonia of cupric oxide or zinc oxide ore is soaked with diffusion cell ammonia and soaks coupling processing.
2. stirring ammonia according to claim 1 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: the raw ore of described step (1) is the raw ore through front fragmentation, comprise the refractory oxidized copper ore high containing basic gangue or contain the high difficult dressing zinc oxide ore of basic gangue.
3. stirring ammonia according to claim 1 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: the dry screen of described step (2) is divided into bilayer, the screen-aperture of upper sieve is 0.8~1.2mm, and the screen-aperture of lower screen is 0.3~0.5mm; The screen-aperture of leading portion wet screening is 0.5~0.8mm; The screen-aperture of back segment wet screening is 0.3~0.5mm.
4. stirring ammonia according to claim 1 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: the dense ammonia of described step (2) and (3) enters [CO in immersion liquid 2] and [NH 3] the ratio of volumetric molar concentration be 1 ︰ (4~3), its total ammonia concentration is 2~4mol/L to cupric oxide ore, is 3~6mol/L to zinc oxide ore; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form.
5. stirring ammonia according to claim 1 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: total ammonia concentration that the middle ammonia of described step (3) and (5) enters immersion liquid is 1~2mol/L to cupric oxide ore, is 1.5~3mol/L to zinc oxide ore; Employing strong aqua, volatile salt or bicarbonate of ammonia add water to allocate and form.
6. stirring ammonia according to claim 1 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: the dense ammonia leaching solution I of described step (3) gained, the dense ammonia leaching solution II of step (4) gained, the middle ammonia leaching solution of step (6) gained, rare ammonia elutant I of step (3) gained, rare ammonia elutant II of step (6) gained extracts respectively extracts copper or zinc, and obtain respectively dense ammonia raffinate, middle ammonia raffinate and rare ammonia raffinate, after mixing or adding reagent, be deployed into qualified solution, being re-used as dense ammonia enters immersion liquid or middle ammonia and enters immersion liquid and return to step (2), (3) and (5) recycle.
7. stirring ammonia according to claim 1 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: the washing lotion of described step (3) and (6) is clear water.
8. stirring ammonia according to claim 6 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: described rare ammonia raffinate returns to step (3) as washing lotion and (6) recycle.
9. stirring ammonia according to claim 1 soaks the method for soaking coupling processing cupric oxide or zinc oxide ore with diffusion cell ammonia, it is characterized in that: the sand liquid of described step (3), (4) and (6) separates and solid-liquid separation is all carried out in confined conditions.
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* Cited by examiner, † Cited by third party
Title
氧化铜矿常温常压两段氨浸试验研究;纪翠翠等;《有色金属》;20110531;第63卷(第2期);152-154 *
纪翠翠等.氧化铜矿常温常压两段氨浸试验研究.《有色金属》.2011,第63卷(第2期),

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