CN101591733A - Precipitating alum and removing iron method in the high-iron zinc sulfide concentrate pressurized acid leaching still - Google Patents
Precipitating alum and removing iron method in the high-iron zinc sulfide concentrate pressurized acid leaching still Download PDFInfo
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- CN101591733A CN101591733A CNA2009100946239A CN200910094623A CN101591733A CN 101591733 A CN101591733 A CN 101591733A CN A2009100946239 A CNA2009100946239 A CN A2009100946239A CN 200910094623 A CN200910094623 A CN 200910094623A CN 101591733 A CN101591733 A CN 101591733A
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Abstract
Precipitating alum and removing iron in a kind of high-iron zinc sulfide concentrate pressurized acid leaching still, high-iron zinc sulfide concentrate mixes in proportion with zinc oxide ore and is conveyed in the autoclave at 23: 1, controlling acidity makes the iron major part transfer the slag phase in zinc leaching process, a small amount of iron that leaches transfers water in leaching liquid by solid phase, leach liquor enters in the regulating tank and to add low-grade zinc oxide ore or heavy cadmia and neutralize and make iron generation hydrolytic precipitation enter the slag phase, drain with slag through press filtration iron, the supernatant liquor that output is qualified directly enters purifying treatment, this method is because deironing is finished in still, and it is short to have flow process, easy and simple to handle, processing cost is low, deironing rate height, it is low that slag contains zinc, advantages such as zinc recovery height.Zinc leaches up to more than 98%, leaches iron content Fe≤20mg/l in the liquid.
Description
Technical field
The present invention relates to Zinc Hydrometallurgy Technology, precipitating alum and removing iron method in especially a kind of high-iron zinc sulfide concentrate pressurized acid leaching still.
Background technology
For the processing of this class material of high-iron zinc sulfide concentrate, adopt the pressurized acid leaching art breading at present, in zinc leaching process, about 30% iron is leached, and iron removes that adopting drops and soaks---pre-neutralization---precipitating alum and removing iron operation and just can remove in the pressurization leach liquor.As seen, there is long flow path in above-mentioned technology, complex operation, processing cost height, shortcoming the such as especially zinc of Jin Chuing is lost to again in the scum, has reduced the rate of recovery of zinc, and the wasting of resources is big.
Summary of the invention
The purpose of this invention is to provide precipitating alum and removing iron in a kind of high-iron zinc sulfide concentrate pressurized acid leaching still, in high ferro vulcanised ore concentrate pressurized acid leaching process, zinc leaches up to more than 98%, leaches iron content Fe≤20mg/l in the liquid.
The present invention reaches the ball milling fineness at one 400 orders and accounts for high-iron zinc sulfide concentrate and zinc oxide ore more than 95% and mixed in 23: 1 by weight proportion and be transported to surge tank and size mixing, adding tensio-active agent xylogen is sized mixing into finite concentration with ore pulp and is pumped in the autoclave, and deployed acid concentration of while is that the dilute sulphuric acid of 1.3～1.7mol/L pumps in the still; 130～160 ℃ of temperature in the kettle of control enter in the still feeding 99.5% industrial pure oxygen, and control still internal pressure is 1.2Mpa, utilize high temperature, high pressure and have to leach under the condition of dilute sulphuric acid and handle zinc sulfide concentrates; The whole acid concentration of the leaching ore pulp that obtains is controlled at 0.15～0.2mol/L, the leach liquor that contains small amounts of iron enters and slowly adds neutralizing agent in the regulating tank to pH5.0～5.2, make the iron generation hydrolysis in the leach liquor change the slag phase over to, drain with slag through press filtration iron, the supernatant liquor that output is qualified directly enters purifying treatment.
Said tensio-active agent xylogen add-on is 0.2% of high-iron zinc sulfide concentrate amount by weight.
The liquid-solid ratio that said ore pulp pumps into autoclave is 7～4.5: 1.
Said ore pulp extraction time in autoclave is 90～120min; Stirring velocity is 500r/min.
Said neutralizing agent is zinc oxide or heavy cadmia.
Said leach liquor enters 80～90 ℃ of controlling reaction time 30～45min behind the regulating tank, terminal temperatures.
Method provided by the invention, make full use of high temperature and oxidizing atmosphere condition in the autoclave, after iron in the high-iron zinc sulfide concentrate leaches, transform out a large amount of ferric ions, controlling acidity makes the iron major part transfer the slag phase in zinc leaching process, make ferric ion change the slag phase over to, thereby reduce the iron-holder in the leach liquor with the form that generates rhombohedral iron ore or siderotil.A small amount of iron that leaches transfers water in leaching liquid by solid phase, leach liquor enters in the regulating tank and to add low-grade zinc oxide ore or heavy cadmia and neutralize and make iron generation hydrolytic precipitation enter the slag phase, drain with slag through press filtration iron, the supernatant liquor that output is qualified directly enters purifying treatment, has cancelled leach liquor through low---pre-neutralization---precipitating alum and removing iron operation of soaking.
In the subtractive process of iron, impurity element As, the Sd in the leach liquor, Ge also follow the hydrolysis of iron to enter the slag phase together in leaching liquid, low-gradely contain the zinc zinc oxide ore or heavy cadmia is made neutralizing agent because of using, and it is big to produce the quantity of slag, the good filtration.So that the iron generation hydrolysis in the leach liquor can not have influence on the strainability of slag.Therefore can shorten one section pressurization with precipitating alum and removing iron in the still and leach the last part technology flow process, the energy consumption in the minimizing process and the loss of metallic zinc, thus reach the effect that reduces production costs.
This method has the flow process weak point because deironing is finished in still, easy and simple to handle, processing cost is low, deironing rate height, and it is low that slag contains zinc, advantages such as zinc recovery height.
Embodiment:
1, raw material
High ferro zinc sulphide essence is taken from certain and is selected factory, and the per-cent of its composition and weight: Zn43.7%, Fe28.67%, S28.29% are with levigate 95% above mistake-400 mesh sieve that reaches of high-iron zinc sulfide concentrate;
2, zincic acid leaches
Leach zinc with the dilute sulphuric acid of concentration 1.3～1.7mol/L, high-iron zinc sulfide concentrate and zinc oxide ore are to pump in the autoclave after being mixed at 23: 1 by weight, go into the still liquid-solid ratio 5: 1, mix total amount 240 and restrain.Leaching condition is: 150 ± 5 ℃ of temperature in the kettle, mixing speed 500r/min, extraction time 120min, still internal pressure 1.2Mpa.The add-on of tensio-active agent xylogen is 0.2% of high-iron zinc sulfide concentrate amount by weight, and with this understanding, the leaching yield of zinc is 98.23%.Whole acid concentration: the 0.15～0.2mol/L of leach liquor; In the leach liquor and terminal point pH:5.0～5.2, temperature: 80～90 ℃.Leach liquid and enter adding neutralizing agent zinc oxide ore in the regulating tank, make the iron generation hydrolysis in the leach liquor change the slag phase over to, be removed the reaction times through the liquid-solid separation of iron of press filtration: 30～45min; The supernatant solution that output is qualified enters purifying treatment.
Claims (6)
1, precipitating alum and removing iron in a kind of high-iron zinc sulfide concentrate pressurized acid leaching still is characterized in that:
The ball milling fineness is reached-400 orders to be accounted for high-iron zinc sulfide concentrate and zinc oxide ore more than 95% and mixed in 23: 1 by weight proportion and be transported to surge tank and size mixing, adding tensio-active agent xylogen is sized mixing into finite concentration with ore pulp and is pumped in the autoclave, and deployed acid concentration of while is that the dilute sulphuric acid of 1.3～1.7mol/L pumps in the still; 130～160 ℃ of temperature in the kettle of control enter in the still feeding 99.5% industrial pure oxygen, and control still internal pressure is 1.2Mpa, utilize high temperature, high pressure and have to leach under the condition of dilute sulphuric acid and handle zinc sulfide concentrates; The whole acid concentration of the leaching ore pulp that obtains is controlled at 0.15～0.2mol/L, the leach liquor that contains small amounts of iron enters and slowly adds neutralizing agent in the regulating tank to pH5.0～5.2, make the iron generation hydrolysis in the leach liquor change the slag phase over to, drain with slag through press filtration iron, the supernatant liquor that output is qualified directly enters purifying treatment.
2, precipitating alum and removing iron in the high-iron zinc sulfide concentrate pressurized acid leaching still according to claim 1 is characterized in that said xylogen add-on is 0.2% of high-iron zinc sulfide concentrate amount by weight.
3, precipitating alum and removing iron in the high-iron zinc sulfide concentrate pressurized acid leaching still according to claim 1 is characterized in that the liquid-solid ratio that said ore pulp pumps into autoclave is 7～4.5: 1.
4, precipitating alum and removing iron in the high-iron zinc sulfide concentrate pressurized acid leaching still according to claim 1 is characterized in that said ore pulp extraction time in autoclave is 90～120min; Stirring velocity is 500r/min.
5, precipitating alum and removing iron in the high-iron zinc sulfide concentrate pressurized acid leaching still according to claim 1 is characterized in that said neutralizing agent is zinc oxide ore or sediment zinc.
6, precipitating alum and removing iron in the high-iron zinc sulfide concentrate pressurized acid leaching still according to claim 1 is characterized in that said leach liquor enters 80～90 ℃ of controlling reaction time 30～45min behind the regulating tank, terminal temperatures.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100946239A CN101591733B (en) | 2009-06-22 | 2009-06-22 | Method for jarosite precipitation and deironization by pressure acid leaching of high-iron zinc-sulphide concentrate in kettle |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100946239A CN101591733B (en) | 2009-06-22 | 2009-06-22 | Method for jarosite precipitation and deironization by pressure acid leaching of high-iron zinc-sulphide concentrate in kettle |
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| CN101591733A true CN101591733A (en) | 2009-12-02 |
| CN101591733B CN101591733B (en) | 2011-01-05 |
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| CN2009100946239A Active CN101591733B (en) | 2009-06-22 | 2009-06-22 | Method for jarosite precipitation and deironization by pressure acid leaching of high-iron zinc-sulphide concentrate in kettle |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101974683A (en) * | 2010-11-10 | 2011-02-16 | 云南永昌铅锌股份有限公司 | Method for producing middle supernatant solution by carrying out two-step pressure acid leaching on high-iron zinc sulfide concentrate |
| CN102002602A (en) * | 2010-11-10 | 2011-04-06 | 云南永昌铅锌股份有限公司 | Method for increasing recovery rates of lead and zinc during lead-zinc sulfide ore dressing-smelting joint application |
| CN102168181A (en) * | 2011-03-17 | 2011-08-31 | 云南永昌铅锌股份有限公司 | Horizontal type pressure leaching kettle and zinc sulfide concentrate leaching method using same |
| CN102586601A (en) * | 2012-03-09 | 2012-07-18 | 大兴安岭云冶矿业开发有限公司 | Method for removing iron by utilizing autoclave during zinc hydrometallurgy production |
| CN102605180A (en) * | 2012-04-23 | 2012-07-25 | 云南冶金集团股份有限公司 | Method for treating zinc sulfide concentrate powder |
| CN102614979A (en) * | 2012-03-29 | 2012-08-01 | 中南大学 | Method for recycling iron in multilevel magnetic separation mode from zinc hydrometallurgy process |
| CN102676805A (en) * | 2012-05-30 | 2012-09-19 | 巴彦淖尔紫金有色金属有限公司 | Low grade zinc concentrate associated lead and silver recovery process |
| CN102925716A (en) * | 2012-11-26 | 2013-02-13 | 云南黄金矿业集团股份有限公司 | Pressurization, water immersion and oxidation preprocessing cyaniding gold extraction method for difficult-processing gold concentrates |
| CN103233120A (en) * | 2013-04-27 | 2013-08-07 | 湖南水口山有色金属集团有限公司 | Method for improving surface activity of floatation silver concentrates during oxygen pressure acid leaching process |
| CN103627911A (en) * | 2013-12-09 | 2014-03-12 | 株洲冶炼集团股份有限公司 | Treatment process for high-iron zinc oxide |
| CN105002354A (en) * | 2015-07-28 | 2015-10-28 | 昆明理工大学 | Method for leaching zinc and other valuable metal in zinc sulfide ore through medium-and-low-pressure oxygen enrichment |
| CN105296755A (en) * | 2015-11-20 | 2016-02-03 | 金川集团股份有限公司 | Method for removing iron in nonmetal high nickel matte pressure leachate |
| CN105734290A (en) * | 2016-03-29 | 2016-07-06 | 湖北大江环保科技股份有限公司 | Arsenic removing technology for zinc hydrometallurgy |
| CN116287713A (en) * | 2022-09-08 | 2023-06-23 | 西部矿业股份有限公司 | Treatment method of zinc hydrometallurgy de-ironing slag |
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| JP3911536B2 (en) * | 2000-01-31 | 2007-05-09 | Ｄｏｗａメタルマイン株式会社 | Zinc concentrate leaching method |
| AU6722001A (en) * | 2000-07-14 | 2002-01-30 | Noranda Inc | Production of zinc oxide from acid soluble ore using precipitation method |
| CN1400321A (en) * | 2002-05-29 | 2003-03-05 | 云南冶金集团总公司 | Zinc sulfide preparation concentrate compression 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 |
| CN1584072A (en) * | 2004-05-25 | 2005-02-23 | 云南冶金集团总公司 | Pressurizer self-catalytic selective leaching-out method for ferric zinc sulfide refining mine |
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- 2009-06-22 CN CN2009100946239A patent/CN101591733B/en active Active
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| CN102002602B (en) * | 2010-11-10 | 2013-01-23 | 云南永昌铅锌股份有限公司 | Method for increasing recovery rates of lead and zinc during lead-zinc sulfide ore dressing-smelting joint application |
| CN102002602A (en) * | 2010-11-10 | 2011-04-06 | 云南永昌铅锌股份有限公司 | Method for increasing recovery rates of lead and zinc during lead-zinc sulfide ore dressing-smelting joint application |
| CN101974683B (en) * | 2010-11-10 | 2012-05-23 | 云南永昌铅锌股份有限公司 | Method for producing middle supernatant solution by carrying out two-step pressure acid leaching on high-iron zinc sulfide concentrate |
| CN101974683A (en) * | 2010-11-10 | 2011-02-16 | 云南永昌铅锌股份有限公司 | Method for producing middle supernatant solution by carrying out two-step pressure acid leaching on high-iron zinc sulfide concentrate |
| CN102168181A (en) * | 2011-03-17 | 2011-08-31 | 云南永昌铅锌股份有限公司 | Horizontal type pressure leaching kettle and zinc sulfide concentrate leaching method using same |
| CN102168181B (en) * | 2011-03-17 | 2013-02-20 | 云南永昌铅锌股份有限公司 | Horizontal type pressure leaching kettle and zinc sulfide concentrate leaching method using same |
| CN102586601A (en) * | 2012-03-09 | 2012-07-18 | 大兴安岭云冶矿业开发有限公司 | Method for removing iron by utilizing autoclave during zinc hydrometallurgy production |
| CN102614979A (en) * | 2012-03-29 | 2012-08-01 | 中南大学 | Method for recycling iron in multilevel magnetic separation mode from zinc hydrometallurgy process |
| CN102605180A (en) * | 2012-04-23 | 2012-07-25 | 云南冶金集团股份有限公司 | Method for treating zinc sulfide concentrate powder |
| CN102676805A (en) * | 2012-05-30 | 2012-09-19 | 巴彦淖尔紫金有色金属有限公司 | Low grade zinc concentrate associated lead and silver recovery process |
| CN102676805B (en) * | 2012-05-30 | 2013-05-01 | 巴彦淖尔紫金有色金属有限公司 | Low grade zinc concentrate associated lead and silver recovery process |
| CN102925716A (en) * | 2012-11-26 | 2013-02-13 | 云南黄金矿业集团股份有限公司 | Pressurization, water immersion and oxidation preprocessing cyaniding gold extraction method for difficult-processing gold concentrates |
| CN103233120A (en) * | 2013-04-27 | 2013-08-07 | 湖南水口山有色金属集团有限公司 | Method for improving surface activity of floatation silver concentrates during oxygen pressure acid leaching process |
| CN103233120B (en) * | 2013-04-27 | 2016-01-20 | 湖南水口山有色金属集团有限公司 | Improve flotation of silver concentrate surface-active method in oxygen pressure acidleach process |
| CN103627911A (en) * | 2013-12-09 | 2014-03-12 | 株洲冶炼集团股份有限公司 | Treatment process for high-iron zinc oxide |
| CN103627911B (en) * | 2013-12-09 | 2015-01-14 | 株洲冶炼集团股份有限公司 | Treatment process for high-iron zinc oxide |
| CN105002354A (en) * | 2015-07-28 | 2015-10-28 | 昆明理工大学 | Method for leaching zinc and other valuable metal in zinc sulfide ore through medium-and-low-pressure oxygen enrichment |
| CN105296755A (en) * | 2015-11-20 | 2016-02-03 | 金川集团股份有限公司 | Method for removing iron in nonmetal high nickel matte pressure leachate |
| CN105296755B (en) * | 2015-11-20 | 2018-06-08 | 金川集团股份有限公司 | A kind of method that non-metallic high nickel matte pressureleaching solution removes iron |
| CN105734290A (en) * | 2016-03-29 | 2016-07-06 | 湖北大江环保科技股份有限公司 | Arsenic removing technology for zinc hydrometallurgy |
| CN116287713A (en) * | 2022-09-08 | 2023-06-23 | 西部矿业股份有限公司 | Treatment method of zinc hydrometallurgy de-ironing slag |
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