CN103451431B - A kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts - Google Patents
A kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts Download PDFInfo
- Publication number
- CN103451431B CN103451431B CN201310379603.2A CN201310379603A CN103451431B CN 103451431 B CN103451431 B CN 103451431B CN 201310379603 A CN201310379603 A CN 201310379603A CN 103451431 B CN103451431 B CN 103451431B
- Authority
- CN
- China
- Prior art keywords
- add
- solid
- reaction
- arsenic
- filter residue
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
Landscapes
- Catalysts (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention provides a kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts, the method presses step of acid dipping, alkali lixiviate arsenic step by pre-treatment step, oxygen, the step of noble metal separation step and Recover palladium powder and platinum powder formed.Oxygen presses acidleach to combine with concentration of precious metal technique by the method, the base metal in spent catalyst can be removed, reclaim heavy metal element arsenic, and to precious metal element, there is the features such as reaction process selectivity is strong, the rate of recovery is high, easy and simple to handle, energy consumption is little, the noble metal nano powder of output is impure few, quality is good, is directly used in the field of catalyzer, medicine etc. as product.
Description
Technical field
The present invention relates to the field of extracting metal from spent catalyst, specifically, relate to a kind of method extracting nano-noble metal powder from spent noble metals bearing catalysts.
Background technology
At present, global all trades and professions are produced every year and are used brought spent catalyst about to have 200 ~ 2,500,000 tons, and these catalyzer itself just consume a large amount of manpower and materials in the fabrication process.Wherein, with regard to raw metal, mainly consume a large amount of precious metals, non-ferrous metal or its oxide compound.In the catalyst, the content of valuable metal is also not less than the content of respective metal in ore, and owing to manufacturing the impact of the course of processing, the enrichment degree of some metal even can higher than the ore of occurring in nature.Therefore, countries in the world government and enterprise notice the recycling of spent noble metals bearing catalysts for a long time, and such as, the Japan of scarcity of resources more payes attention to.In spent catalyst, whether institute's metallic components is recycled, and this depends on the number of valency metallic element contained by it and is worth height.
Catalyzer containing precious metal is widely used in the fields such as hydrogenation, oxidation, dehydrogenation, organic synthesis, formolation, carbonylation, and the precious metal kind mainly comprised in this spent catalyst has silver, platinum, rhodium, iridium, ruthenium, palladium etc.In addition, due to the demand of product itself or the impact of Working environment, the valuable metals such as nickel, cobalt, arsenic, antimony, copper also often appear at containing in noble metal catalyst.And scrap metal catalyst recovery is subject to puzzlement technically and economically, current recovery utilization rate is not high, and be confined to the rare precious metal that minority content is higher, value is larger, for and the effective recycling of the spent noble metals bearing catalysts of complicated components low containing valency amount of metal, also there is a lot of difficulty.
In addition, waste catalyst recovery technique main at present comprises pyrogenic process and reclaims and hydrometallurgic recovery two kinds, and the power consumption that pyrogenic process reclaims is high, pollution is large, and the acid consumption of hydrometallurgic recovery is large, solution ion concentration is high, tail washings complex disposal process.Therefore, the efficiency improving spent noble metals bearing catalysts removal process is also problem demanding prompt solution.
Summary of the invention
In order to solve the problems of the technologies described above, the invention provides a kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts, use the method can enrichment the precious metal element extracted in spent noble metals bearing catalysts and heavy metal arsenic, and directly prepare nano-noble metal powder.
The technical solution used in the present invention is: a kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts, it is characterized in that: described spent noble metals bearing catalysts contains the component of following weight per-cent: the Fe of 10 ~ 15%, the Zn of 10% ~ 20%, the Ni of 15% ~ 20%, the Pt of 15 ~ 25%, the As of 10 ~ 20%, the Pd of 0.1 ~ 1%, the Cu of 10 ~ 15%, and inevitable impurity, the method presses step of acid dipping, alkali lixiviate arsenic step by pre-treatment step, oxygen, the step of noble metal separation step and Recover palladium powder and platinum powder formed.
Be specially, first described spent noble metals bearing catalysts passed through pulverizing, cleaning, dry and roasting pretreatment, then add strong acid and carry out acidleach under oxygen pressure, carry out heat filter and washing after the acidleach of oxygen pressure, in the filter residue after solid-liquid separation, add aqua regia dissolution, add ammonium chloride after catching up with nitre and form precipitation, add ammoniacal liquor again and carry out precious metal element separation, solution containing palladium adds reductive agent reaction and generates palladium powder, and the filter residue of platiniferous adds xitix and dispersion agent and passes into ammonia, finally obtains platinum powder.
In described pre-treatment step, first spent noble metals bearing catalysts is broken into fritter, again by levigate for the fritter after fragmentation to 3 ~ 5mm, use washed with de-ionized water, and dry 1 ~ 2 hour at 120 ~ 150 DEG C, then put into heat treatment furnace, roasting 1 ~ 2 hour at 200 ~ 300 DEG C, thus remove the organic substance in spent catalyst.
In described oxygen pressure step of acid dipping, to in the spent catalyst after described roasting, sulfuric acid is added according to solid-to-liquid ratio 1: 5 ~ 10, and put into enclosed high pressure reactor and carry out acid-leaching reaction, passing into oxygen and reaching oxygen partial pressure is 0.6 ~ 1.2MPa, temperature 150 ~ 180 DEG C, 1 ~ 2 hour reaction times, heat filter is carried out with the hot water of 80 ~ 90 DEG C after leaching, and with leached mud solid-to-liquid ratio be 1: 2 ~ 4 hot wash 2 ~ 3 times, solid-liquid separation makes arsenic and precious metal enter filter residue, and other metallic elements enter filtrate.
In described alkali lixiviate arsenic step, leach the filter residue after the acidleach of described oxygen pressure by the NaOH solution of 5mol/L, extraction time is 2 ~ 3 hours, solid-to-liquid ratio is 1: 5 ~ 10, and temperature is 50 ~ 80 DEG C, and reaction terminates rear filtering separation, make precious metal enter filter residue, and carry out electrolytic recovery arsenic containing arsenic filtrate.
In described noble metal separation step, chloroazotic acid is added according to solid-to-liquid ratio 1: 10 ~ 15 in the filter residue after solid-liquid separation, and add industrial hydrochloric acid and catch up with nitre, add the ammonium chloride of 70 ~ 90g/L afterwards, stop when the amount of precipitation no longer increases adding ammonium chloride, temperature of reaction is 60 ~ 80 DEG C, is less than 1.0 by the pH value continuing to add industrial hydrochloric acid control reaction soln; After described precipitation and solution separating, in described precipitation, add the ammoniacal liquor that mass concentration is 25 ~ 28%, add-on is 1.5 ~ 2 times of theoretical consumption, and after generating precipitation, solid-liquid separation obtains containing the filtrate of palladium and the filter residue of platiniferous again.
In the step of described Recover palladium powder, to slowly adding dispersion agent containing the filtrate of palladium and mass concentration is the hydrazine hydrate of 60 ~ 80%, add-on is theoretical consumption 1.5 ~ 2 times, controlling temperature of reaction is 45 ~ 55 DEG C, reaction generates palladium powder, it is neutral for cleaning to pH value with hot water after heat filter, dries 1 ~ 2 hour, finally obtain the palladium powder that granularity is 50 ~ 100nm at 120 ~ 150 DEG C.
In the step of described recovery platinum powder, the filter residue chloroazotic acid of platiniferous is dissolved completely, then add xitix and dispersion agent and pass into ammonia, xitix add-on is 1.0 ~ 1.5 times of theoretical consumption, and controlling temperature of reaction is 60 ~ 80 DEG C, and pH value is less than 1.0, reaction generates palladium powder, it is neutral for cleaning to pH value with hot water after heat filter, dries 1 ~ 2 hour, finally obtain the nanometer platinum powder that granularity is 10 ~ 100nm at 120 ~ 150 DEG C.
In addition, the commercial sulphuric acid used in oxygen pressure step of acid dipping.Described solid-to-liquid ratio is solid masses and the ratio of liquid volume, and mass unit is g, and volume unit is L.Further, adopt method of the present invention that the rate of recovery of platinum palladium can be made all to reach more than 98%.
Advantage of the present invention is: pressed by oxygen the method for acidleach to combine with heavy metal and concentration of precious metal technique, the base metal elements in spent catalyst can be removed, after heavy metal is separated with precious metal element, directly obtain nano level noble metal powder by hydrazine hydrate and xitix, have the advantages that reaction process selectivity is strong, the rate of recovery is high, easy and simple to handle, energy consumption is little to precious metal element.The noble metal nano powder of output of the present invention is impure few, and quality is good, is directly used in the field of catalyzer, medicine etc. as product.Liquid and waste slag produced after conventional treatment process qualified discharge, secondary pollution can not be caused to environment.
Embodiment
Below in conjunction with embodiment and comparative example, the present invention is described in more detail.
Embodiment 1:
This spent noble metals bearing catalysts contains the component of following weight per-cent: the Fe of 14%, the Zn of 15%, the Ni of 15%, the Pt of 25%, the As of 15%, the Pd of 1%, the Cu of 15%, and inevitable impurity.First spent noble metals bearing catalysts is broken into fritter, then by levigate for the fritter after fragmentation to 3mm, uses washed with de-ionized water, and dry 2 hours at 120 DEG C, then put into heat treatment furnace, roasting 2 hours at 200 DEG C, thus remove the organic substance in spent catalyst.To in the spent catalyst after described roasting, sulfuric acid is added according to solid-to-liquid ratio 1: 5, and put into enclosed high pressure reactor and carry out acid-leaching reaction, passing into oxygen and reaching oxygen partial pressure is 0.8MPa, temperature 150 DEG C, 2 hours reaction times, heat filter is carried out with the hot water of 80 DEG C after leaching, and with leached mud solid-to-liquid ratio be 1: 2 hot wash 3 times, solid-liquid separation makes arsenic and precious metal enter filter residue, and other metallic elements enter filtrate.Then, leach the filter residue after the acidleach of described oxygen pressure by the NaOH solution of 5mol/L, extraction time is 2 hours, and solid-to-liquid ratio is 1: 5, and temperature is 50 DEG C, and reaction terminates rear filtering separation, makes precious metal enter filter residue, and carries out electrolytic recovery arsenic containing arsenic filtrate.Chloroazotic acid is added according to solid-to-liquid ratio 1: 10 in the filter residue after solid-liquid separation, and add industrial hydrochloric acid and catch up with nitre, add the ammonium chloride of 70g/L afterwards, stop when the amount of precipitation no longer increases adding ammonium chloride, temperature of reaction is 60 DEG C, is less than 1.0 by the pH value continuing to add industrial hydrochloric acid control reaction soln; After described precipitation and solution separating, in described precipitation, add the ammoniacal liquor that mass concentration is 25%, add-on is 2 times of theoretical consumption, and after generating precipitation, solid-liquid separation obtains containing the filtrate of palladium and the filter residue of platiniferous again.To slowly adding dispersion agent containing the filtrate of palladium and mass concentration is the hydrazine hydrate of 60%, add-on is theoretical consumption 1.5 times, controlling temperature of reaction is 45 DEG C, reaction generates palladium powder, it is neutral for cleaning to pH value with hot water after heat filter, dry 2 hours at 120 DEG C, finally obtain the palladium powder that granularity is 50 ~ 100nm.The filter residue chloroazotic acid of platiniferous is dissolved completely, then add xitix and dispersion agent and pass into ammonia, xitix add-on is 1.0 times of theoretical consumption, controlling temperature of reaction is 60 DEG C, pH value is less than 1.0, and reaction generates palladium powder, and it is neutral for cleaning to pH value with hot water after heat filter, dry 2 hours at 120 DEG C, finally obtain the nanometer platinum powder that granularity is 10 ~ 100nm.
Embodiment 2:
This spent noble metals bearing catalysts contains the component of following weight per-cent: the Fe of 12%, the Zn of 20%, the Ni of 18%, the Pt of 20%, the As of 14%, the Pd of 1%, the Cu of 15%, and inevitable impurity.First spent noble metals bearing catalysts is broken into fritter, then by levigate for the fritter after fragmentation to 4mm, uses washed with de-ionized water, and dry 1 hour at 130 DEG C, then put into heat treatment furnace, roasting 2 hours at 250 DEG C, thus remove the organic substance in spent catalyst.To in the spent catalyst after described roasting, sulfuric acid is added according to solid-to-liquid ratio 1: 8, and put into enclosed high pressure reactor and carry out acid-leaching reaction, passing into oxygen and reaching oxygen partial pressure is 1MPa, temperature 160 DEG C, 2 hours reaction times, heat filter is carried out with the hot water of 85 DEG C after leaching, and with leached mud solid-to-liquid ratio be 1: 3 hot wash 2 times, solid-liquid separation makes arsenic and precious metal enter filter residue, and other metallic elements enter filtrate.Then, leach the filter residue after the acidleach of described oxygen pressure by the NaOH solution of 5mol/L, extraction time is 3 hours, and solid-to-liquid ratio is 1: 8, and temperature is 60 DEG C, and reaction terminates rear filtering separation, makes precious metal enter filter residue, and carries out electrolytic recovery arsenic containing arsenic filtrate.Chloroazotic acid is added according to solid-to-liquid ratio 1: 12 in the filter residue after solid-liquid separation, and add industrial hydrochloric acid and catch up with nitre, add the ammonium chloride of 80g/L afterwards, stop when the amount of precipitation no longer increases adding ammonium chloride, temperature of reaction is 70 DEG C, is less than 1.0 by the pH value continuing to add industrial hydrochloric acid control reaction soln; After described precipitation and solution separating, in described precipitation, add the ammoniacal liquor that mass concentration is 28%, add-on is 1.5 times of theoretical consumption, and after generating precipitation, solid-liquid separation obtains containing the filtrate of palladium and the filter residue of platiniferous again.To slowly adding dispersion agent containing the filtrate of palladium and mass concentration is the hydrazine hydrate of 80%, add-on is theoretical consumption 1.5 times, controlling temperature of reaction is 50 DEG C, reaction generates palladium powder, it is neutral for cleaning to pH value with hot water after heat filter, dry 1 hour at 130 DEG C, finally obtain the palladium powder that granularity is 50 ~ 100nm.The filter residue chloroazotic acid of platiniferous is dissolved completely, then add xitix and dispersion agent and pass into ammonia, xitix add-on is 1.2 times of theoretical consumption, controlling temperature of reaction is 70 DEG C, pH value is less than 1.0, and reaction generates palladium powder, and it is neutral for cleaning to pH value with hot water after heat filter, dry 2 hours at 130 DEG C, finally obtain the nanometer platinum powder that granularity is 10 ~ 100nm.
Embodiment 3:
This spent noble metals bearing catalysts contains the component of following weight per-cent: the Fe of 15%, the Zn of 10%, the Ni of 15%, the Pt of 25%, the As of 20%, the Pd of 1%, the Cu of 14%, and inevitable impurity.First spent noble metals bearing catalysts is broken into fritter, then by levigate for the fritter after fragmentation to 5mm, uses washed with de-ionized water, and dry 1 hour at 140 DEG C, then put into heat treatment furnace, roasting 1 hour at 300 DEG C, thus remove the organic substance in spent catalyst.To in the spent catalyst after described roasting, sulfuric acid is added according to solid-to-liquid ratio 1: 10, and put into enclosed high pressure reactor and carry out acid-leaching reaction, passing into oxygen and reaching oxygen partial pressure is 1.2MPa, temperature 180 DEG C, 1 hour reaction times, heat filter is carried out with the hot water of 90 DEG C after leaching, and with leached mud solid-to-liquid ratio be 1: 4 hot wash 2 times, solid-liquid separation makes arsenic and precious metal enter filter residue, and other metallic elements enter filtrate.Then, leach the filter residue after the acidleach of described oxygen pressure by the NaOH solution of 5mol/L, extraction time is 3 hours, and solid-to-liquid ratio is 1: 10, and temperature is 80 DEG C, and reaction terminates rear filtering separation, makes precious metal enter filter residue, and carries out electrolytic recovery arsenic containing arsenic filtrate.Chloroazotic acid is added according to solid-to-liquid ratio 1: 15 in the filter residue after solid-liquid separation, and add industrial hydrochloric acid and catch up with nitre, add the ammonium chloride of 90g/L afterwards, stop when the amount of precipitation no longer increases adding ammonium chloride, temperature of reaction is 80 DEG C, is less than 1.0 by the pH value continuing to add industrial hydrochloric acid control reaction soln; After described precipitation and solution separating, in described precipitation, add the ammoniacal liquor that mass concentration is 28%, add-on is 2 times of theoretical consumption, and after generating precipitation, solid-liquid separation obtains containing the filtrate of palladium and the filter residue of platiniferous again.To slowly adding dispersion agent containing the filtrate of palladium and mass concentration is the hydrazine hydrate of 80%, add-on is theoretical consumption 1.5 times, controlling temperature of reaction is 55 DEG C, reaction generates palladium powder, it is neutral for cleaning to pH value with hot water after heat filter, dry 1 hour at 150 DEG C, finally obtain the palladium powder that granularity is 50 ~ 100nm.The filter residue chloroazotic acid of platiniferous is dissolved completely, then add xitix and dispersion agent and pass into ammonia, xitix add-on is 1.5 times of theoretical consumption, controlling temperature of reaction is 80 DEG C, pH value is less than 1.0, and reaction generates palladium powder, and it is neutral for cleaning to pH value with hot water after heat filter, dry 1 hour at 150 DEG C, finally obtain the nanometer platinum powder that granularity is 10 ~ 100nm.
Comparative example:
First spent noble metals bearing catalysts is broken into fritter, again by levigate for the fritter after fragmentation to 5mm, use washed with de-ionized water, and dry 1 hour at 140 DEG C, then heat treatment furnace is put into, roasting 1 hour at 300 DEG C, thus the organic substance in removal spent catalyst, then the sulfuric acid of 5mol/L is adopted to leach at ambient pressure, filter residue after solid-liquid separation adopts alkali lixiviate arsenic, then electrolytic recovery arsenic, and the filter residue containing precious metal adds aqua regia dissolution, adopt ammonium chloride to be separated by platinum palladium, and prepare ultrafine palladium powder and Ultrafine Platinum Powder by hydrazine hydrate reduction.In comparative example, the metallic arsenic obtained and noble metal powder composition all wayward, the fluctuation of Pt, Pd composition is comparatively large, and residual element As, Cu content is high, and noble metal powder granularity is also all at more than 200mn.
As can be seen from embodiment 1-3 and comparative example, by utilizing the treatment process extracting arsenic and precious metal from spent noble metals bearing catalysts according to the embodiment of the present invention, impurity content can be reduced widely, industrial practice is convenient to control to utilize, and reclaim and obtain nano level superfine noble metal powder, directly can supply the field such as Precious Metal, catalyzer manufacturer and use.
Although illustrate and describe embodiments of the invention, those having ordinary skill in the art will appreciate that: can carry out multiple change, amendment, replacement and modification to these embodiments when not departing from principle of the present invention and aim, scope of the present invention is by claim and equivalents thereof.
Claims (1)
1. one kind is extracted the method for arsenic and precious metal from spent noble metals bearing catalysts, it is characterized in that: described spent noble metals bearing catalysts contains the component of following weight per-cent: the Fe of 10 ~ 15%, the Zn of 10% ~ 20%, the Ni of 15% ~ 20%, the Pt of 15 ~ 25%, the As of 10 ~ 20%, the Pd of 0.1 ~ 1%, the Cu of 10 ~ 15%, and inevitable impurity, the method presses step of acid dipping, alkali lixiviate arsenic step by pre-treatment step, oxygen, the step of noble metal separation step and Recover palladium powder and platinum powder formed; Be specially, first described spent noble metals bearing catalysts passed through pulverizing, cleaning, dry and roasting pretreatment, then add sulfuric acid and carry out acidleach under oxygen pressure, heat filter and washing is carried out after the acidleach of oxygen pressure, the filter residue after heat filter is leached and filtering separation with alkali, aqua regia dissolution is added in the filter residue after solid-liquid separation, add ammonium chloride after catching up with nitre and form precipitation, add ammoniacal liquor again and carry out precious metal element separation, solution containing palladium adds reductive agent reaction and generates nano Pd powder, the filter residue of platiniferous adds xitix and dispersion agent and passes into ammonia, finally obtains nanometer platinum powder; In described pre-treatment step, first spent noble metals bearing catalysts is broken into fritter, again by levigate for the fritter after fragmentation to 3 ~ 5mm, use washed with de-ionized water, and dry 1 ~ 2 hour at 120 ~ 150 DEG C, then put into heat treatment furnace, roasting 1 ~ 2 hour at 200 ~ 300 DEG C, thus remove the organic substance in spent catalyst; In described oxygen pressure step of acid dipping, to in the spent catalyst after described roasting, sulfuric acid is added according to solid-to-liquid ratio 1: 5 ~ 10, and put into enclosed high pressure reactor and carry out acid-leaching reaction, passing into oxygen and reaching oxygen partial pressure is 0.6 ~ 1.2MPa, temperature 150 ~ 180 DEG C, 1 ~ 2 hour reaction times, heat filter is carried out with the hot water of 80 ~ 90 DEG C after leaching, and with leached mud solid-to-liquid ratio be 1: 2 ~ 4 hot wash 2 ~ 3 times, solid-liquid separation makes arsenic and precious metal enter filter residue, and other metallic elements enter filtrate; In described alkali lixiviate arsenic step, leach the filter residue after the acidleach of described oxygen pressure by the NaOH solution of 5mol/L, extraction time is 2 ~ 3 hours, solid-to-liquid ratio is 1: 5 ~ 10, and temperature is 50 ~ 80 DEG C, and reaction terminates rear filtering separation, make precious metal enter filter residue, and carry out electrolytic recovery arsenic containing arsenic filtrate; In described noble metal separation step, chloroazotic acid is added according to solid-to-liquid ratio 1: 10 ~ 15 in the filter residue after solid-liquid separation, and add industrial hydrochloric acid and catch up with nitre, add the ammonium chloride of 70 ~ 90g/L afterwards, stop when the amount of precipitation no longer increases adding ammonium chloride, temperature of reaction is 60 ~ 80 DEG C, is less than 1.0 by the pH value continuing to add industrial hydrochloric acid control reaction soln; After described precipitation and solution separating, in described precipitation, add the ammoniacal liquor that mass concentration is 25 ~ 28%, add-on is 1.5 ~ 2 times of theoretical consumption, and after generating precipitation, solid-liquid separation obtains containing the filtrate of palladium and the filter residue of platiniferous again; In the step of described Recover palladium powder, to slowly adding dispersion agent containing the filtrate of palladium and mass concentration is the hydrazine hydrate of 60 ~ 80%, add-on is theoretical consumption 1.5 ~ 2 times, controlling temperature of reaction is 45 ~ 55 DEG C, reaction generates palladium powder, it is neutral for cleaning to pH value with hot water after heat filter, dries 1 ~ 2 hour, finally obtain the palladium powder that granularity is 50 ~ 100nm at 120 ~ 150 DEG C; In the step of described recovery platinum powder, the filter residue chloroazotic acid of platiniferous is dissolved completely, then add xitix and dispersion agent and pass into ammonia, xitix add-on is 1.0 ~ 1.5 times of theoretical consumption, and controlling temperature of reaction is 60 ~ 80 DEG C, and pH value is less than 1.0, reaction generates palladium powder, it is neutral for cleaning to pH value with hot water after heat filter, dries 1 ~ 2 hour, finally obtain the nanometer platinum powder that granularity is 10 ~ 100nm at 120 ~ 150 DEG C; The sulfuric acid used in oxygen pressure step of acid dipping is commercial sulphuric acid; Described solid-to-liquid ratio is solid masses and the ratio of liquid volume, and mass unit is g, and volume unit is L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310379603.2A CN103451431B (en) | 2013-08-27 | 2013-08-27 | A kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310379603.2A CN103451431B (en) | 2013-08-27 | 2013-08-27 | A kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103451431A CN103451431A (en) | 2013-12-18 |
| CN103451431B true CN103451431B (en) | 2015-08-12 |
Family
ID=49734262
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310379603.2A Active CN103451431B (en) | 2013-08-27 | 2013-08-27 | A kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103451431B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112522514B (en) * | 2020-11-17 | 2022-05-03 | 陕西三秦环保科技股份有限公司 | Recycling treatment method for copper-containing etching solution |
| CN116065029A (en) * | 2023-02-02 | 2023-05-05 | 河北程睿环保集团有限公司 | Process for extracting noble metal from three-way catalyst |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60251233A (en) * | 1984-05-29 | 1985-12-11 | Nisso Bentoron Kk | Method for recovering platinium group element from waste catalyst |
| CN1067925A (en) * | 1991-06-24 | 1993-01-13 | 中国有色金属工业总公司昆明贵金属研究所 | Method for recovering palladium from waste palladium-carbon catalyst and incinerator system |
| CN1067926A (en) * | 1991-06-24 | 1993-01-13 | 中国有色金属工业总公司昆明贵金属研究所 | Method for recovering platinum from waste catalyst |
| CN1127304A (en) * | 1995-05-29 | 1996-07-24 | 国内贸易部物资再生利用研究所 | Palladium recovering method from waste palladium carbon catalyst |
| RU2081924C1 (en) * | 1995-08-23 | 1997-06-20 | Спиртус Марк Аврамович | Method arsenic removing from the noble metal concentrates |
| CN102181644A (en) * | 2011-04-13 | 2011-09-14 | 深圳市格林美高新技术股份有限公司 | Method for reclaiming rare noble metals from waste circuit board |
| CN102717090A (en) * | 2011-03-31 | 2012-10-10 | 北京有色金属研究总院 | Method for preparing ultrafine platinum powder by adopting liquid-phase reduction |
-
2013
- 2013-08-27 CN CN201310379603.2A patent/CN103451431B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60251233A (en) * | 1984-05-29 | 1985-12-11 | Nisso Bentoron Kk | Method for recovering platinium group element from waste catalyst |
| CN1067925A (en) * | 1991-06-24 | 1993-01-13 | 中国有色金属工业总公司昆明贵金属研究所 | Method for recovering palladium from waste palladium-carbon catalyst and incinerator system |
| CN1067926A (en) * | 1991-06-24 | 1993-01-13 | 中国有色金属工业总公司昆明贵金属研究所 | Method for recovering platinum from waste catalyst |
| CN1127304A (en) * | 1995-05-29 | 1996-07-24 | 国内贸易部物资再生利用研究所 | Palladium recovering method from waste palladium carbon catalyst |
| RU2081924C1 (en) * | 1995-08-23 | 1997-06-20 | Спиртус Марк Аврамович | Method arsenic removing from the noble metal concentrates |
| CN102717090A (en) * | 2011-03-31 | 2012-10-10 | 北京有色金属研究总院 | Method for preparing ultrafine platinum powder by adopting liquid-phase reduction |
| CN102181644A (en) * | 2011-04-13 | 2011-09-14 | 深圳市格林美高新技术股份有限公司 | Method for reclaiming rare noble metals from waste circuit board |
Non-Patent Citations (1)
| Title |
|---|
| 从铂钯精矿中回收贵金属工艺选择;王爱荣等;《安徽化工》;20021030(第5期);第11-12页第2-3节 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103451431A (en) | 2013-12-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103451433B (en) | A kind of method extracting precious metal from spent noble metals bearing catalysts | |
| CN103451432B (en) | A kind of method extracting lead and precious metal from spent noble metals bearing catalysts | |
| CN102277497B (en) | Method of reclaiming gold, palladium, platinum and silver from waste circuit board | |
| CN102534226B (en) | Method for extracting precious metal from spent automobile catalyst by concentration smelting-wet separation process | |
| CN102952947B (en) | Comprehensive recovery method of rare metals in waste circuit boards | |
| CN102994771B (en) | Method for extracting palladium sponge from silver electrolysis anode slime parting liquid | |
| CN100400684C (en) | Method for recovering noble-metal from waste catalyst | |
| CN101942568B (en) | Method for recovering noble metal from waste computer and fittings thereof | |
| CN103131857B (en) | Method for purifying platinum group metal from waste three-way catalyst | |
| CN101476041B (en) | Method for separating and recycling copper, nickel and regenerative plastic from waste electroplating plastic | |
| CN104911359A (en) | Process method for extracting cobalt and nickel from manganese waste slag | |
| CN103397186A (en) | Regenerating method and process for recycling rare precious metals from electronic wastes | |
| CN102732728B (en) | Separation method of noble metals in scrapped auto-exhaust catalyst | |
| CN111793753A (en) | Process for extracting and separating platinum group metals from waste catalyst | |
| CN102796877A (en) | Method for enriching rhodium from rhodium-containing organic dead catalyst | |
| CN102560100A (en) | Process for preparing high-purity superfine cobalt powder from copper-cobalt-iron alloy | |
| CN113293301B (en) | Method for recovering platinum group metals from metal carrier waste automobile exhaust catalyst | |
| CN102643995A (en) | Method for separating and recovering copper from waste electronic appliances | |
| CN103834805A (en) | Method of leaching divalent cobalt from cobalt copper bidery metal | |
| CN109825707A (en) | A method of recycling gold from discarded circuit board | |
| CN103173619B (en) | Method for recovering nickel and tungsten by waste nickel and tungsten catalyst | |
| CN114134337B (en) | Low-cost and high-efficiency method for recovering noble metal in circuit board components | |
| CN116716484B (en) | Method for recovering palladium and dimethylglyoxime from palladium-refining palladium-removing slag | |
| CN103451431B (en) | A kind of method extracting arsenic and precious metal from spent noble metals bearing catalysts | |
| CN105886785A (en) | Method for preparing high-purity silver powder from silver-rich residue containing high selenium and tellurium |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: LI LUQING Free format text: FORMER OWNER: LUO ZHI Effective date: 20150616 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20150616 Address after: Yinzhou District Lianfeng road 315175 Zhejiang city of Ningbo Province, No. 886 Applicant after: Li Luqing Address before: Yinzhou District Heng Jie Heng Jie Zhen Road 315181 No. 50 Zhejiang city of Ningbo Province Applicant before: Luo Zhi |
|
| ASS | Succession or assignment of patent right |
Owner name: JIANGXI NANCHENG XINYE ENVIRONMENTAL PROTECTION DI Free format text: FORMER OWNER: LI LUQING Effective date: 20150701 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| C53 | Correction of patent for invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Zhou Meigen Inventor after: Zhang Zhiming Inventor before: Luo Zhi |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: INVENTOR; FROM: LUO ZHI TO: ZHOU MEIGEN ZHANG ZHIMING |
|
| TA01 | Transfer of patent application right |
Effective date of registration: 20150701 Address after: 344700, Jinshan Industrial Zone, Nancheng County, Jiangxi, Fuzhou (third issue) Applicant after: Jiangxi Nancheng Xinye Environmental Protection Disposal Co.,Ltd. Address before: Yinzhou District Lianfeng road 315175 Zhejiang city of Ningbo Province, No. 886 Applicant before: Li Luqing |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |