CN1733949A - Zinc oxide raw ore fluidization leaching process - Google Patents
Zinc oxide raw ore fluidization leaching process Download PDFInfo
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- CN1733949A CN1733949A CNA2004100404389A CN200410040438A CN1733949A CN 1733949 A CN1733949 A CN 1733949A CN A2004100404389 A CNA2004100404389 A CN A2004100404389A CN 200410040438 A CN200410040438 A CN 200410040438A CN 1733949 A CN1733949 A CN 1733949A
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- ore pulp
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- fluidization
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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Abstract
The invention relates to fluidization technique for zinc oxide crude ore, which comprises: breaking and grinding the crude ore, conditioning; pumping the top of cone-shaped reactor and acid liquid from bottom of reactor; leaching out; neutralizing the leached liquid in container; condensing in device; cleansing the supernatant to enter another reactor for further acid fluidization; filter-pressing the acid-leached pulp; conveying the filter liquid to ball grinding for conditioning; stacking the slag. Third invention decreases in-tank time of slag and zinc loss, increases zinc leaching efficiency, and cuts cost.
Description
Technical field
The invention belongs to the smelting technology method, particularly the wet process smelting technique of zinc oxide raw ore.
Technical background
Domestic and international 85% zinc is that electrodeposition method adopts zinc baking sand to produce.It is one critical process of zinc hydrometallurgy that the zinc oxide raw ore leaches.At present, the leaching plant that electric zinc factory generally adopts is mechanical agitating tank or pneumatic blending groove, agitator and airduct, steam heating tube etc. is housed in the groove inserts appurtenant in the infusion solutions.Because it is higher to contain acid in the solution, therefore higher to the requirement for anticorrosion of equipment, maintenance capacity is big, and the investment of leaching vat and auxiliary facility is corresponding increases.The zinc oxide raw ore is produced primary ore by the mine, directly enter crushing system and carry out electric zinc production operation, the ore composition mainly comprises grey lithotype oxidized ore, quartz sand lithotype and breccia type, they all are easy to be dissolved in the acid solution, ore has the characteristic of high silicon again simultaneously, adopt mechanical stirring to leach when producing, the leaching yield of silicon is higher, causes ore pulp solution clarification, filtration difficulty to occur in liquid-solid separation circuit; The throughput of conventional equipment is low, and the time that ore pulp stops in groove is long, leaches operation and is difficult to strengthen, thereby influence leaching effect.Owing to above reason, existing zinc smelting technology has caused production cost high, and the zinc metal loss is bigger.
Summary of the invention
Technical problem to be solved by this invention provides a kind of processing method of carrying out the fluidization leaching from the zinc oxide raw ore.Its technology is simple, and production cost is low, the leaching rate height of zinc, and the rate of loss of zinc is little, level of automation is high.
Solving the scheme that technical problem of the present invention adopts is:
(1) raw ore is gone into ball milling and is carried out fine grinding and size mixing through fragmentation is laggard, and ore pulp enters pre-immersion trough and adds auxiliary material, evenly puts into medial launder from the bottom, ore pulp is pumped into the top of the fluidizing reactor of taper with pump;
(2) utilizing pump that acid solution is pumped into the formation fluidize bed from the fluidizing reactor bottom leaches, reacted leach liquor overflows from the overflow port on fluidizing reactor top, the neutralization of inflow neutralizer when the pH value of leach liquor reaches 4.5～5.4, is sent to thickener and is concentrated;
(3) supernatant liquor that overflows from thickener top send cleaning section to carry out operation, and underflow enters another group fluidizing reactor again to carry out acid fluidization once more and leach, and acid leaching ore pulp carries out full ore pulp press filtration, and filtrate is sent to ball milling and is done and size mixing, and filter residue is stored up.
Technical scheme of the present invention also comprises: the auxiliary material that ore pulp enters pre-immersion trough adding is Manganse Dioxide, sulfuric acid and waste electrolyte, and the extraction temperature of fluidizing reactor is 50 ℃～95 ℃.
Technique scheme of the present invention can reach following effect:
(1) production cost is low.Just can replace six φ 3400 * 4600 mechanical agitating tanks of the prior art with two cover fluidizing reactors, and can save wherein mechanism, airduct, steam heating tube etc., the investment of minimizing equipment.
(2) the leaching rate height of zinc.Ore pulp is adverse current with the flow direction of acid in fluidizing reactor, and formed weak, in, three zones of strong acid, the coarse particles ore deposit falls into the strong acid district, and middle particle ore deposit falls into the acid district, and the fine particle ore deposit falls into the weak acid district, make reaction more complete, because the reaction times is shorter, so the high silicon composition in the ore deposit leaches seldom, also just solved the problem of clarification, liquid-solid separation difficulty, improve the leaching rate of zinc, reduced the loss of zinc.
(3) easily realize production process serialization, automatization.
Embodiment
Embodiment 1
Crushing raw ore is become particle diameter 0.5mm～20mm, enter ball mill and size mixing, ore pulp enters pre-immersion trough and adds auxiliary material Manganse Dioxide, sulfuric acid and waste electrolyte, give soak 30 minutes after, ore pulp is evenly put into medial launder from the bottom.With pump ore pulp is pumped into the top of the fluidizing reactor of taper again, simultaneously, with pump acid solution is pumped into the formation fluidize bed from the fluidizing reactor bottom and leach, in leaching process, the reaction heat that utilizes reaction to produce is heated with the steam in the pre-immersion trough and is replenished mutually, guarantees that extraction temperature is at 60 ℃.The reaction leach liquor directly overflows from the overflow port on fluidizing reactor top, flows into the neutralizer neutralization, when the pH value of leach liquor reaches 4.5, is sent to thickener and concentrates.The supernatant liquor that overflows from thickener top send cleaning section to carry out operation, and underflow enters another group fluidizing reactor again and carries out acid fluidization leaching once more, and acid leaching ore pulp carries out the press filtration of gold mine slurry, and filtrate is sent to ball milling and is sized mixing, and filter residue is stored up.
Embodiment 2
Crushing raw ore is become particle diameter 0.5mm～20mm, enter ball mill and size mixing, ore pulp enters pre-immersion trough and adds auxiliary material Manganse Dioxide, sulfuric acid and waste electrolyte, give soak 40 minutes after, ore pulp is evenly put into medial launder from the bottom.With pump ore pulp is pumped into the top of the fluidizing reactor of taper again, simultaneously, with pump acid solution is pumped into the formation fluidize bed from the fluidizing reactor bottom and leach, in leaching process, the reaction heat that utilizes reaction to produce is heated with the steam in the pre-immersion trough and is replenished mutually, guarantees that extraction temperature is at 70 ℃.The reaction leach liquor directly overflows from the overflow port on fluidizing reactor top, pumps into the neutralizer neutralization, when the pH value of leach liquor reaches 5.0, is sent to thickener and concentrates.The supernatant liquor that overflows from thickener top send cleaning section to carry out operation, and underflow enters another group fluidizing reactor again and carries out acid fluidization leaching once more, and acid leaching ore pulp carries out full ore pulp press filtration, and filtrate is sent to ball milling and is sized mixing, and filter residue is stored up.
Embodiment 3
Crushing raw ore is become particle diameter 0.5mm～20mm, enter ball mill and size mixing, ore pulp enters pre-immersion trough and adds auxiliary material Manganse Dioxide, sulfuric acid and waste electrolyte, give soak 45 minutes after, ore pulp is evenly put into medial launder from the bottom.With pump ore pulp is pumped into the top of the fluidizing reactor of taper again, simultaneously, with pump acid solution is pumped into the formation fluidize bed from the fluidizing reactor bottom and leach, in leaching process, the reaction heat that utilizes reaction to produce is heated with the steam in the pre-immersion trough and is replenished mutually, guarantees that extraction temperature is at 82 ℃.The reaction leach liquor directly overflows from the overflow port on fluidizing reactor top, pumps into the neutralizer neutralization, when the pH value of leach liquor reaches 5.2, is sent to thickener and concentrates.The supernatant liquor that overflows from thickener top send cleaning section to carry out operation, and underflow enters another group fluidizing reactor again and carries out acid fluidization leaching once more, and acid leaching ore pulp carries out full ore pulp press filtration, and filtrate is sent to ball milling and is sized mixing, and filter residue is stored up.
Be the contrast of several indexs of the present invention and mechanical mixing method below, the raw ore that is utilized is quartz sand lithotype zinc oxide ore.
1, productive capacity contrast
| Classification | Leaching yield % | Leach rate of recovery % | Slag contains zinc % |
| The fluidization method | 93.35 | 84.16 | 5.3 |
| Mechanical mixing method | 92.25 | 82.34 | 6.54 |
2, concentrate the quality contrast
| Classification | The supernatant liquor quality | Filter effect |
| The fluidization method | Limpid | Better |
| Mechanical mixing method | Sometimes muddy, limpid sometimes | Generally |
3, cost contrast
| Classification | The capital construction cost | Production cost | Maintenance cost |
| The fluidization method | 300,000 yuan | Low | 30,000 yuan/year |
| Mechanical mixing method | 5,000,000 yuan | High | 450,000 yuan/year |
Annotate: the two all is 20,000 tons/year a industrial scale in the above contrast, and original 6 agitator motors in the mechanical stirring production, every power 22kw, and move 24 hours every day continuously, and year production was by 300 days, but brownout in every year 950400kw.h of the present invention.
Claims (2)
1, a kind of zinc oxide raw ore fluidization extract technology is characterized in that:
(1) raw ore is gone into ball milling and is carried out fine grinding and size mixing through fragmentation is laggard, and ore pulp enters pre-immersion trough and adds auxiliary material, evenly puts into medial launder from the bottom, ore pulp is pumped into the top of the fluidizing reactor of taper with pump;
(2) utilizing pump that acid solution is pumped into the formation fluidize bed from the fluidizing reactor bottom leaches, reacted leach liquor overflows from the overflow port on fluidizing reactor top, the neutralization of inflow neutralizer when the pH value of leach liquor reaches 4.5～5.4, is sent to thickener and is concentrated;
(3) supernatant liquor that overflows from thickener top send cleaning section to carry out operation, and underflow enters another group fluidizing reactor again to carry out acid fluidization once more and leach, and acid leaching ore pulp carries out full ore pulp press filtration, and filtrate is sent to ball milling and is done and size mixing, and filter residue is stored up.
2, by the described zinc oxide raw ore of claim 1 fluidization extract technology, it is characterized in that: the auxiliary material that ore pulp enters pre-immersion trough adding is Manganse Dioxide, sulfuric acid and waste electrolyte, and the extraction temperature of fluidizing reactor is 50 ℃～95 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100404389A CN1303232C (en) | 2004-08-10 | 2004-08-10 | Zinc oxide raw ore fluidization leaching process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100404389A CN1303232C (en) | 2004-08-10 | 2004-08-10 | Zinc oxide raw ore fluidization leaching process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1733949A true CN1733949A (en) | 2006-02-15 |
| CN1303232C CN1303232C (en) | 2007-03-07 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100404389A Expired - Fee Related CN1303232C (en) | 2004-08-10 | 2004-08-10 | Zinc oxide raw ore fluidization leaching process |
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| Country | Link |
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| CN (1) | CN1303232C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101748289B (en) * | 2008-12-15 | 2012-04-18 | 汉中八一锌业有限责任公司 | Neutral leaching method of zinc metallurgy in wet method |
| CN103627899A (en) * | 2013-12-09 | 2014-03-12 | 株洲冶炼集团股份有限公司 | Device for clearing accumulated dregs in pipelines without disassembly in zinc hydrometallurgy |
| CN113174496A (en) * | 2021-04-22 | 2021-07-27 | 甘肃厂坝有色金属有限责任公司 | Method and system for supplementing manganese in zinc hydrometallurgy |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3911536B2 (en) * | 2000-01-31 | 2007-05-09 | Ｄｏｗａメタルマイン株式会社 | Zinc concentrate leaching method |
| CN1303231C (en) * | 2002-08-24 | 2007-03-07 | 祥云县飞龙实业有限责任公司 | Zinc sulfide concentrate calcines and zinc ide ore combined leaching process |
| CN1414121A (en) * | 2002-09-17 | 2003-04-30 | 昆明冶研新材料股份有限公司 | Method of treating low grade zinc oxide ore |
-
2004
- 2004-08-10 CN CNB2004100404389A patent/CN1303232C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101748289B (en) * | 2008-12-15 | 2012-04-18 | 汉中八一锌业有限责任公司 | Neutral leaching method of zinc metallurgy in wet method |
| CN103627899A (en) * | 2013-12-09 | 2014-03-12 | 株洲冶炼集团股份有限公司 | Device for clearing accumulated dregs in pipelines without disassembly in zinc hydrometallurgy |
| CN103627899B (en) * | 2013-12-09 | 2015-04-22 | 株洲冶炼集团股份有限公司 | Device for clearing accumulated dregs in pipelines without disassembly in zinc hydrometallurgy |
| CN113174496A (en) * | 2021-04-22 | 2021-07-27 | 甘肃厂坝有色金属有限责任公司 | Method and system for supplementing manganese in zinc hydrometallurgy |
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| Publication number | Publication date |
|---|---|
| CN1303232C (en) | 2007-03-07 |
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Granted publication date: 20070307 Termination date: 20100810 |