CN103276215A - Method for recovering noble metal from waste catalyst - Google Patents
Method for recovering noble metal from waste catalyst Download PDFInfo
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- CN103276215A CN103276215A CN2013102148704A CN201310214870A CN103276215A CN 103276215 A CN103276215 A CN 103276215A CN 2013102148704 A CN2013102148704 A CN 2013102148704A CN 201310214870 A CN201310214870 A CN 201310214870A CN 103276215 A CN103276215 A CN 103276215A
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Abstract
The invention discloses a method for recovering noble metal from a waste catalyst, which is technically characterized by comprising the following steps: dissolving a waste catalyst carrier with sulfuric acid while pressurizing, and adding a TiCl3 solution to prevent the dispersion of noble metal so as to increase the recovery rate of the noble metal, wherein the dissolved carrier obtains a relatively pure aluminum sulfate solution which can be used as a raw material for the manufacturing of a water purifying agent, thus realizing the comprehensive utilization of the waste catalyst. The method disclosed by the invention comprises the following specific technical process and reaction conditions: (1) incinerating the waste catalyst at 400-800 DEG C, and performing carbon removal; (2) dissolving the carrier while pressurizing: placing the waste catalyst subjected to carbon removal into a polytetrafluoroethylene lined high-pressure reaction kettle containing the dilute sulfuric acid and the TiCl3 solution, wherein the concentration of the sulfuric acid is 15-60%, the solid-to-liquid ratio is 1:(4-10), the mass concentration of the TiCl3 is 76.0-78.5%, the ratio of the added TiCl3 to the noble metal is (0.01-0.85):1, the working temperature is 105-230 DEG C, the reaction time is 1-6 hours, and the pressure is 1.1-28.0 Kg/cm<2>; (3) filtering, and washing; and (4) separating and purifying the noble metal in enriched slag.
Description
Technical field
The present invention relates to from the catalyzer that lost efficacy, reclaim the method for metal component, especially from the alumina base spent catalyst, reclaim the method for precious metal.
Background technology
The platinum metals has been widely used in catalyst for reaction such as hydrogenation, dehydrogenation, reformation, oxidation, isomerization, disproportionation, cracking, deaminizating, because factors such as poisoning, carbon deposit, carrier structure variation, metal grain gathering or loss cause catalyzer to lose activity, catalyzer needs periodic replacement.These catalyst value are huge, and when catalyzer finished work-ing life, the platinum metals must be recycled.
Because γ-Al
2O
3Surface-area big, good at the temperature range internal stability of most of catalyzed reactions, as γ-Al
2O
3When being used as carrier, except the effect that can play dispersion and stabilizing active component, also can provide acid, basic active center, play synergy with catalytic active component, so γ-Al
2O
3Purposes the widest, current main as various support of the catalyst.
Sulfuric acid can dissolve γ-Al
2O
3, from γ-Al
2O
3Reclaiming platinum metals and valuable metal in the base spent catalyst generally adopts wet method to extract.Wet method is used more is acid-soluble method.Acid-soluble method has selects to dissolve support methods, selection dissolving precious metal method and CL method, and selecting the generation of dissolving precious metal method and CL method to obtain by product can not direct production water purification agent Al
2(SO
4)
3, waste water comprehensive utilization cost height.
Patent CN101036889 discloses the method that a kind of catalyst made from platonic reclaims platinum, and operation divides 4 steps: (1) is according to the color of spent catalyst and contain the classification of charcoal number, batching by a certain percentage; (2) sulfuric acid dissolution carrier without burning carbon deposit, directly adopts sulfuric acid dissolution Al
2O
3Carrier, platinum does not dissolve, and adds a small amount of formic acid reduction after reaction finishes and is dispersed in a spot of platinum in the solution; (3) analyzing and testing platinum, insoluble filter residue are put into roasting kiln roasting charcoal, organism and water directly with behind the drying with steam, and fired slags is through the content of ball milling, weighing, sampling analysis measuring platinum; (4) platinum refining, fired slags is the sponge platina through aqua regia dissolution, chloride precipitation, hydrazine hydrate reduction ammonium chloroplatinate, platina passes through aqua regia dissolution, ion-exchange, chloride precipitation, hydrazine hydrate again, and 1100 ℃ of calcinings obtain 99.95% spongy platinum product, and the platinum rate of recovery is greater than 98%.
Patent CN201210073205.3 discloses a kind of method that reclaims precious metal and prepare high purity aluminium oxide from aluminium scrap is catalyst based, reclaim precious metal and mainly comprise 3 steps: (1) roasting: aluminium scrap catalyst based (~ 40 μ m) and ammonium sulfate are mixed in proportion, at 300 ~ 500 ℃ of roasting temperature 2 ~ 4 h; (2) product of roasting leaches 2 h dealuminzations with dilute sulphuric acid (1 mol/L); (3) dealuminzation pulp water chloride solution reclaims precious metal, and noble metal recovery rate is greater than 99%.
Summary of the invention
Main purpose of the present invention provides a kind of method that reclaims precious metal from the alumina base spent catalyst.This method also by the sulfuric acid dissolution alumina catalyst support, obtains purer alum liquor in the efficient recovery precious metal, can be used as the raw material of making water purification agent, has realized the comprehensive utilization of spent catalyst.
Technical problem to be solved by this invention is to adopt sulfuric acid that used catalyst support is carried out dissolved under pressure, and sulfuric acid is being selected dissolving γ-Al
2O
3In the time of carrier, a spot of precious metal also can be dissolved, causes the dispersion of precious metal, and then reduce noble metal recovery rate, and the present invention is by adding TiCl
3Solution prevents the dispersion of precious metal, reaches the purpose that reclaims precious metal.
Embodiment of the present invention are pressed following design:
(1) burns: spent catalyst is poured in the Stainless Steel Disc, put into retort furnace, in 400 ~ 800 ℃ of calcining 1 ~ 6 h carbon removal;
(2) dissolved under pressure: the spent catalyst after will calcining is put into and is filled sulfuric acid and TiCl
3In the autoclave of solution, the dissolved under pressure used catalyst support;
(3) filter: the spent catalyst solution after will dissolving filters, washing, and filter residue is thick precious metal;
(4) purify: the enrichment slag that contains precious metal is transferred to solution separate purification.
Above-mentioned, the thickness of spent catalyst in Stainless Steel Disc should be even in the step (1), and control is at 1 ~ 10 cm, and the volume of spent catalyst should not surpass 2/3rds of Stainless Steel Disc.
TiCl described in the step (2)
3Solution is chemical pure, mass concentration: 76.0% ~ 78.5%, and add-on is 0.01 ~ 0.85:1 with the ratio of noble metal amount.
Sulfuric acid described in the step (2) is technical pure, and its mass concentration remains on 15% ~ 60%, and it is 1:4 ~ 10 that add-on keeps solid-to-liquid ratio.
Autoclave described in the step (2) adopts lining tetrafluoro autoclave, 105 ~ 230 ℃ of working temperatures, mixing speed 20 ~ 380 r/min.
The dissolved under pressure reaction times described in the step (2) should be controlled at 1 ~ 6 hour, and the pressure of dissolved under pressure used catalyst support should be controlled at 1.1 Kg/cm
2~ 28.0 Kg/cm
2
Filter described in the step (3) and should also carry out after the cooling fully for 3 ~ 10 times at solution dilution.
Described in the step (4) the enrichment slag that contains precious metal being transferred to solution separates to purify and be: the precious metal that will contain in the enrichment slag of precious metal leaches in the solution, and separates purification with the method for chloride precipitation or ammoniacal liquor complexing.
It is described that precious metal is leached into leach liquor used in the solution is HCl+HNO
3, HCl+NaClO
3, HCl+Cl
2
The described spent catalyst that contains precious metal is that alumina base is carrier, and the noble metal component on the described precious metal spent catalyst is one or both in platinum, the palladium.
The present invention adopts sulfuric acid that used catalyst support is carried out dissolved under pressure, and following advantage is compared with prior art arranged: (1) can improve sulfuric acid dissolution efficient, reduces the acid consumption, reduces the slag rate, shortens the reaction times; (2) by adding TiCl
3Solution can effectively prevent the dispersion of precious metal, improves noble metal recovery rate; (3) by the sulfuric acid dissolution alumina catalyst support, obtain purer Tai-Ace S 150, as the raw material of making water purification agent, realized the comprehensive utilization of spent catalyst.Cost of the present invention is low, it is little to pollute, precious metal rate of recovery height, be easy to realize industrialization.
Description of drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
The present invention is described in further detail and verifies its effect below in conjunction with the drawings and specific embodiments.
Embodiment one
The spent catalyst that takes by weighing 4 Kg platiniferous, 3036 g/T is poured in the Stainless Steel Disc, and thickness is 5 cm, puts into retort furnace, in 600 ℃ of calcining 3 h carbon removal; Spent catalyst after the calcining is put into the lining tetrafluoro autoclave that fills 30% sulfuric acid, add 4.5g TiCl
3Solution, the dissolved under pressure used catalyst support, solid-to-liquid ratio 1:6,130 ℃ of working temperatures, in 4 hours reaction times, pressure is 2.5 Kg/cm
2, stir speed (S.S.) 80 r/min; With 6 times of the spent catalyst solution dilutions after the dissolving and cooled and filtered, washing, calcining fully, obtain 177 g filter residues, filter residue is platina; Platina in the enrichment slag is leached in the solution with chloroazotic acid, catch up with behind the nitre and purify with the ammonium chloride repeated precipitation, and obtain 11.92 g spongy platinums in 800 ℃ of calcining ammonium chloroplatinates, purity is greater than 99.95%, and the rate of recovery is greater than 98.1%.
Embodiment two
Take by weighing the spent catalyst that 5 Kg contain palladium 2850 g/T and pour in the Stainless Steel Disc, thickness is 7 cm, puts into retort furnace, in 600 ℃ of calcining 4 h carbon removal; Spent catalyst after the calcining is put into the lining tetrafluoro autoclave that fills 30% sulfuric acid, add 5.5g TiCl
3Solution, the dissolved under pressure used catalyst support, solid-to-liquid ratio 1:6,140 ℃ of working temperatures, in 5 hours reaction times, pressure is 3.5 Kg/cm
2, stir speed (S.S.) 80 r/min; With 7 times of the spent catalyst solution dilutions after the dissolving and cooled and filtered, washing, calcining fully, obtain 148 g filter residues, filter residue is thick palladium; Thick palladium formic acid reduction back in the enrichment slag is leached in the solution with chloroazotic acid, and use chloride precipitation, the complexing repeatedly of ammoniacal liquor, hydrochloric acid, acidifying obtain 14.01 g palladium sponges with hydrazine hydrate reduction then, and purity is greater than 99.95%, and the rate of recovery is greater than 98.3%.
Embodiment three
The spent catalyst that takes by weighing 6 Kg platiniferous, 1428 g/T, palladium 2274 g/T is poured in the Stainless Steel Disc, and thickness is 8 cm, puts into retort furnace, in 650 ℃ of calcining 5 h carbon removal; Spent catalyst after the calcining is put into the lining tetrafluoro autoclave that fills 35% sulfuric acid, add 8.5g TiCl
3Solution, the dissolved under pressure used catalyst support, solid-to-liquid ratio 1:6,150 ℃ of working temperatures, in 4 hours reaction times, pressure is 4.5 Kg/cm
2, stir speed (S.S.) is 80 r/min; With 8 times of the spent catalyst solution dilutions after the dissolving and cooled and filtered, washing, calcining fully, obtain 182 g filter residues, filter residue is platina, thick palladium; Platina in the enrichment slag, thick palladium formic acid reduction back are leached in the solution with hydrochloric acid and sodium chlorate, adding saturated sodium hydroxide solution then transfers about pH=1, to the neutralization after solution in add ammonium chloride, form ammonium chloroplatinate, palladium remains in the solution, platinum is purified with the ammonium chloride repeated precipitation, and in 800 ℃ the calcining ammonium chloroplatinates obtain 8.21 g spongy platinums, palladium solution ammoniacal liquor, hydrochloric acid complexing repeatedly, acidifying, obtain 13.18 g palladium sponges with hydrazine hydrate reduction then, the purity of gained spongy platinum, palladium sponge is greater than 99.95%, and the rate of recovery is greater than 96.2%.
Embodiment four
The spent catalyst that takes by weighing 6 Kg platiniferous, 4277 g/T is poured in the Stainless Steel Disc, and thickness is 8 cm, puts into retort furnace, in 600 ℃ of calcining 5 h carbon removal; Spent catalyst after the calcining is put into the lining tetrafluoro autoclave that fills 30% sulfuric acid, add 9.0g TiCl
3Solution, the dissolved under pressure used catalyst support, solid-to-liquid ratio 1:6,150 ℃ of working temperatures, in 5 hours reaction times, pressure is 4.5 Kg/cm
2, stir speed (S.S.) 80 r/min; With 8 times of the spent catalyst solution dilutions after the dissolving and cooled and filtered, washing, calcining fully, obtain 206 g filter residues, filter residue is platina; Platina in the enrichment slag is leached in the solution with chloroazotic acid, catch up with behind the nitre and purify with the ammonium chloride repeated precipitation, and obtain 25.35 g spongy platinums in 800 ℃ of calcining ammonium chloroplatinates, purity is greater than 99.95%, and the rate of recovery is greater than 98.7%.
Claims (10)
1. method that reclaims precious metal from spent catalyst is characterized in that carrying out successively as follows:
(1) burns: spent catalyst is poured in the Stainless Steel Disc, put into retort furnace, in 400 ~ 800 ℃ of calcining 1 ~ 6 h carbon removal;
(2) dissolved under pressure: the spent catalyst after will calcining is put into and is filled sulfuric acid and TiCl
3In the autoclave of solution, the dissolved under pressure used catalyst support;
(3) filter: the spent catalyst solution after will dissolving filters, washing, and filter residue is thick precious metal;
(4) purify: the enrichment slag that contains precious metal is transferred to solution separate purification.
2. recovery method according to claim 1 is characterized in that the thickness of spent catalyst in Stainless Steel Disc should be even in the step (1), and control is at 1 ~ 10 cm, and the volume of spent catalyst should not surpass 2/3rds of Stainless Steel Disc.
3. recovery method according to claim 1 is characterized in that TiCl described in the step (2)
3Solution is chemical pure, mass concentration: 76.0% ~ 78.5%, and add-on is 0.01 ~ 0.85:1 with the ratio of noble metal amount.
4. recovery method according to claim 1 is characterized in that the sulfuric acid described in the step (2) is technical pure, and its mass concentration remains on 15% ~ 60%, and it is 1:4 ~ 10 that add-on keeps solid-to-liquid ratio.
5. recovery method according to claim 1 is characterized in that autoclave described in the step (2) adopts lining tetrafluoro autoclave, 105 ~ 230 ℃ of working temperatures, mixing speed 20 ~ 380 r/min.
6. recovery method according to claim 1 is characterized in that the dissolved under pressure reaction times described in the step (2) should control at 1 ~ 6 hour, and the pressure of dissolved under pressure used catalyst support should be controlled at 1.1 Kg/cm
2~ 28.0 Kg/cm
2
7. recovery method according to claim 1 is characterized in that filtering described in the step (3) and should also carry out after the cooling fully for 3 ~ 10 times at solution dilution.
8. recovery method according to claim 1, it is characterized in that described in the step (4) that the enrichment slag that contains precious metal is transferred to solution to be separated to purify and be: the precious metal that will contain in the enrichment slag of precious metal leaches in the solution, and separates purification with the method for chloride precipitation or ammoniacal liquor complexing.
9. recovery method according to claim 8 is characterized in that described precious metal is leached into leach liquor used in the solution is HCl+HNO
3, HCl+NaClO
3, HCl+Cl
2
10. the method that reclaims precious metal from spent catalyst according to claim 1 is characterized in that the described spent catalyst that contains precious metal is that alumina base is carrier, and the noble metal component on the described precious metal spent catalyst is one or both in platinum, the palladium.
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103981363A (en) * | 2014-06-04 | 2014-08-13 | 沈少波 | Device and method for extracting rare noble metals by adopting wet process |
| CN104342558A (en) * | 2014-05-12 | 2015-02-11 | 上海派特贵金属环保科技有限公司 | A method for recycling palladium from a spent precious metal catalyst |
| CN104480312A (en) * | 2014-11-23 | 2015-04-01 | 北京科技大学 | Method for recycling noble metal from automobile exhaust catalyst |
| CN104745836A (en) * | 2015-04-21 | 2015-07-01 | 昆山鸿福泰环保科技有限公司 | Platinum recovery refining process |
| CN104831071A (en) * | 2015-04-08 | 2015-08-12 | 昆明理工大学 | Method for recovering platinum and palladium from waste carrier catalyst by hydrothermal method |
| CN104975182A (en) * | 2015-07-14 | 2015-10-14 | 河南中原黄金冶炼厂有限责任公司 | Pretreatment method for recovering gold and silver from waste water adsorbing gold-carried carbon for precious metal refining |
| CN105603206A (en) * | 2016-01-12 | 2016-05-25 | 贵研资源（易门）有限公司 | Pretreatment method of plasma furnace aggregate before recycling noble metals |
| CN106222440A (en) * | 2016-08-31 | 2016-12-14 | 陕西瑞科新材料股份有限公司 | The recovery method of palladium metal in a kind of useless palladium carbon catalyst |
| CN106319224A (en) * | 2016-08-08 | 2017-01-11 | 广东先导稀材股份有限公司 | Indium recovery method |
| CN108315564A (en) * | 2017-12-28 | 2018-07-24 | 核工业北京化工冶金研究院 | The method that a kind of molten carrier recycles platinum from aluminium-based catalyst |
| CN112047400A (en) * | 2020-09-28 | 2020-12-08 | 山东泰和水处理科技股份有限公司 | Waste activated carbon disposal device and disposal method thereof |
| CN114107663A (en) * | 2021-10-12 | 2022-03-01 | 安徽元琛环保科技股份有限公司 | Method for extracting noble metal from waste noble metal catalyst |
| CN114836629A (en) * | 2022-05-05 | 2022-08-02 | 昆明贵研新材料科技有限公司 | Enrichment method of waste silicon dioxide carrier noble metal catalyst |
| CN114892015A (en) * | 2022-05-05 | 2022-08-12 | 昆明贵研新材料科技有限公司 | From useless Al 2 O 3 Method for enriching and recovering precious metals in base precious metal catalyst |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1123843A (en) * | 1994-11-30 | 1996-06-05 | 核工业北京化工冶金研究院 | Recovery of platinum family elements from waste catalysts |
| RU2138568C1 (en) * | 1998-07-13 | 1999-09-27 | Парецкий Валерий Михайлович | Method of processing exhausted catalysts containing platinum-group metals |
| CN1472346A (en) * | 2003-06-30 | 2004-02-04 | 黎明化工研究院 | Recovery of palladium metal from waste palladium/aluminium oxide catalyst |
| CN100419101C (en) * | 2003-10-14 | 2008-09-17 | 秦仁洙 | Recovery of precious metals from waste catalysts |
| CN101376923A (en) * | 2007-08-27 | 2009-03-04 | 中国石油化工股份有限公司 | Method for recycling noble metal from spent catalyst |
| CN101575674A (en) * | 2001-06-28 | 2009-11-11 | 贵研铂业股份有限公司 | Method for recovering platinum metal from melting trapped material |
-
2013
- 2013-06-03 CN CN201310214870.4A patent/CN103276215B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1123843A (en) * | 1994-11-30 | 1996-06-05 | 核工业北京化工冶金研究院 | Recovery of platinum family elements from waste catalysts |
| RU2138568C1 (en) * | 1998-07-13 | 1999-09-27 | Парецкий Валерий Михайлович | Method of processing exhausted catalysts containing platinum-group metals |
| CN101575674A (en) * | 2001-06-28 | 2009-11-11 | 贵研铂业股份有限公司 | Method for recovering platinum metal from melting trapped material |
| CN1472346A (en) * | 2003-06-30 | 2004-02-04 | 黎明化工研究院 | Recovery of palladium metal from waste palladium/aluminium oxide catalyst |
| CN100419101C (en) * | 2003-10-14 | 2008-09-17 | 秦仁洙 | Recovery of precious metals from waste catalysts |
| CN101376923A (en) * | 2007-08-27 | 2009-03-04 | 中国石油化工股份有限公司 | Method for recycling noble metal from spent catalyst |
Non-Patent Citations (1)
| Title |
|---|
| 何云陔等: "铂、钯催化还原水产氢及光助作用的研究", 《催化学报》 * |
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| CN103981363A (en) * | 2014-06-04 | 2014-08-13 | 沈少波 | Device and method for extracting rare noble metals by adopting wet process |
| CN104480312A (en) * | 2014-11-23 | 2015-04-01 | 北京科技大学 | Method for recycling noble metal from automobile exhaust catalyst |
| CN104831071A (en) * | 2015-04-08 | 2015-08-12 | 昆明理工大学 | Method for recovering platinum and palladium from waste carrier catalyst by hydrothermal method |
| CN104745836A (en) * | 2015-04-21 | 2015-07-01 | 昆山鸿福泰环保科技有限公司 | Platinum recovery refining process |
| CN104975182A (en) * | 2015-07-14 | 2015-10-14 | 河南中原黄金冶炼厂有限责任公司 | Pretreatment method for recovering gold and silver from waste water adsorbing gold-carried carbon for precious metal refining |
| CN105603206A (en) * | 2016-01-12 | 2016-05-25 | 贵研资源（易门）有限公司 | Pretreatment method of plasma furnace aggregate before recycling noble metals |
| CN105603206B (en) * | 2016-01-12 | 2017-11-03 | 贵研资源（易门）有限公司 | Plasma heating furnace enrichment material reclaims the preprocess method before noble metal |
| CN106319224A (en) * | 2016-08-08 | 2017-01-11 | 广东先导稀材股份有限公司 | Indium recovery method |
| CN106319224B (en) * | 2016-08-08 | 2018-01-23 | 广东先导稀材股份有限公司 | The recovery method of indium |
| CN106222440A (en) * | 2016-08-31 | 2016-12-14 | 陕西瑞科新材料股份有限公司 | The recovery method of palladium metal in a kind of useless palladium carbon catalyst |
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