CN100400684C - Method for recovering noble-metal from waste catalyst - Google Patents
Method for recovering noble-metal from waste catalyst Download PDFInfo
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- CN100400684C CN100400684C CNB2006100466346A CN200610046634A CN100400684C CN 100400684 C CN100400684 C CN 100400684C CN B2006100466346 A CNB2006100466346 A CN B2006100466346A CN 200610046634 A CN200610046634 A CN 200610046634A CN 100400684 C CN100400684 C CN 100400684C
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
A method for recovering noble metal from waste catalysts containing noble metal is carried out by pre-treating for waste catalysts containing noble metal, stage roasting, leaching noble metal into solution, purifying and recovering noble metal from solution. The immersion liquid adopts mixed solution with sodium hypochlorite, hydrion and chlorine ion. It's cheap, safe, clean and complete. It has less pollution and higher recovery rate.
Description
1, technical field
The invention belongs to the method that from spent catalyst, reclaims metal component, specifically, relate to from the spent catalyst that contains precious metal, reclaim the method for precious metal.
2, background technology
Along with the progress of science and technology and becoming better and approaching perfection day by day of environmental legislation, precious metal has been not limited only to make ornament and play a role on economy and finance, and be applied in the Industrial processes, especially use widely having obtained aspect the used catalyzer of petrochemical process.
Precious metal such as palladium, platinum has important irreplaceable effect owing to have unique physics, chemical property in every field.Yet China's palladium and platinum resource are very deficient, and price is very expensive, and domestic needs increases year by year, needs import more than the 90w% of domestic needs.Simultaneously, annual China all has the waste material that contains palladium, platinum in a large number to produce.Since the secondary resource that contains precious metal with the first time resource compare, have the content height, form relative with technological process simple, advantage such as tooling cost is low, thereby each industrially developed country of the world all takes much count of the recycling of precious metal secondary resource.In conjunction with China's national situation, the meaning that the precious metal secondary resource is recycled is more great.
The method of precious metal from present recovery waste material mainly can be divided into: pyrogenic process and wet method two big classes.Pyrogenic process is to carry out high melt with containing the precious metal waste material, makes concentration of precious metal in common metal, reclaimed with traditional method, but this method complex operation, complex process, process cost height, precious metal yield is low again.Using at present is hydrometallurgic recovery more widely, and soon precious metal leaches into and forms ionic condition in the solution, extracts from solution then, has formed various extraction process thus.For example: U.S. Pat 5102632 proposes, and reclaims precious metal with two-stage method from the waste material that contains precious metal, at first carries out pyroprocessing, chlorination, leach with chloroazotic acid then, complex operation, expense height, dangerous big, environmental pollution is serious; All proposed from different raw materials, to reclaim the method for precious metal among US4331634, US 4578250, US 5045290, US 5324851, US 5302183, US 5654458, US 5503812, EP 0538168, EP 0585489 and the CN 85100109A separately, its process all is earlier waste material to be carried out pyroprocessing, carry out the routine dissolving through pretreated sample, reclaim precious metal with different organic solvent extractions then.In these methods, at first to carry out pyroprocessing to the waste material that contains precious metal, but catalyzer for the carbon distribution inactivation, especially the bigger spent catalyst of carbon deposition quantity, because heat release is concentrated in the high temperature roast process, temperature control is improper, can make the carbon distribution that adheres on the catalyzer be difficult to remove fully, carry out the routine leaching again, will certainly cause noble metal recovery rate low; Utilize hydrogen peroxide, chloroazotic acid etc. to carry out that routine is leached not only the expense height, environmental pollution is serious simultaneously and dangerous big.
3, summary of the invention
For solving above shortcoming, at the existing shortcoming of precious metal recovery technology in the existing noble metal catalyst, the present invention proposes a kind of method that reclaims precious metal from the precious metal spent catalyst, and this method has less investment, it is little to pollute, technology simple, need are short with the time, the rate of recovery is high and be easy to advantage such as industrialization.
The method that reclaims precious metal from contain the precious metal spent catalyst provided by the present invention mainly may further comprise the steps: the spent catalyst that contains precious metal is carried out pre-treatment, precious metal is leached in the solution, purifies and reclaim precious metal from solution, wherein saidly the spent catalyst that contains precious metal is carried out preprocessing process divide four-stage to carry out:
Fs: at 50-100 ℃, constant temperature is 1-3 hour in the time of best 60-70 ℃, and oxygen level is adjusted to 0.5v%-10.0v%, is preferably 2.0v%～7.0v%;
Subordinate phase: at 200-300 ℃, constant temperature is 1-3 hour in the time of best 240-260 ℃, oxygen level is increased be 8.0v%-15.0v%, is preferably 10.0v%～13.0v%;
Phase III: at 400-500 ℃, constant temperature is 1-3 hour in the time of best 430-450 ℃, oxygen level is increased be 13.0v%-19.0v%, is preferably 15.0v%～18.0v%;
The quadravalence section: at 700-800 ℃, constant temperature is 1-2 hour in the time of best 740-760 ℃, oxygen level is increased be 18v%～21v%, is preferably 19.0v%～21.0v%.
Heat-up rate between above-mentioned each stage is 1 ℃～10 ℃ of per minutes.
Described precious metal is leached can adopt immersion liquid commonly used in the prior art to leach in the solution, the preferred solution that contains clorox, hydrogen ion and chlorion that adopts; The clorox volumetric molar concentration is generally 0.1～20mol/L in the described immersion liquid, is preferably 0.2～10mol/L; The hydrogen ion volumetric molar concentration is generally 0.1～20mol/L, is preferably 0.2～10mol/L; The chlorion volumetric molar concentration is generally 0.1～20mol/L, is preferably 0.2～10mol/L.Generally can adopt and contain clorox, hydrochloric acid and/or muriatic mixing solutions.The condition of leaching is generally: leaching solution is 1: 1～1000: 1 with the solid volume ratio, is preferably 10: 1～100: 1, and leaching temperature is generally 0 ℃～300 ℃, is preferably 50 ℃～200 ℃, and leaching time is generally 1h～48h, is preferably 5h～10h.
The spent catalyst that contains precious metal of the present invention is that to be often referred to the precious metal be the activity of such catalysts component, and noble metal component is supported on certain supported catalyst, its carrier can be inorganic materials and/or organic materials, is generally aluminum oxide and/or molecular sieve.Described precious metal is meant group VIII noble metals component in the periodic table of elements, one or more in palladium, platinum, rhodium, the iridium for example, palladium commonly used, in the platinum one or both.
Describedly from solution, purify and reclaim precious metal and can adopt the whole bag of tricks commonly used in the prior art,, preferably adopt step-by-step precipitation method as solvent extration, step-by-step precipitation method, exchange resin method etc.Promptly at first regulate pH value to 4～5 of the solution that contains precious metal, remove precipitation with alkali; Add alkali regulator solution pH value to 8～9 again, remove post precipitation, get precious metal with hydrazine hydrate reduction, wherein used alkali is this area various alkaline matters commonly used, is preferably alkali-metal oxyhydroxide such as sodium hydroxide, potassium hydroxide.
Method of the present invention be applicable to the catalyzer that contains precious metal, the especially carbon deposition quantity of carbon distribution inactivation bigger contain noble metal catalyst.
Compared with prior art, the inventive method adopts the useless noble metal catalyst of the method pre-treatment of segmentation roasting, make carbon distribution on the spent catalyst burn totallyer, more thorough, help in the subsequent step recovery of precious metal is improved noble metal recovery rate.The mixing solutions that contains clorox, hydrogen ion and chlorion is adopted in used immersion liquid, and cost is low, pollution is little, danger is little, is easy to industrialization.Employing step-by-step precipitation method cost is low, pollution is little, retrieving arrangement is required simply, and shortened return period widely, is easier to industrialization.
4, embodiment
Comparative example
10.0g contain the industrial Pt/ molecular sieve spent catalyst of 0.330w%Pt, through high-temperature roasting 4h in 650 ℃ of air, the cooling back adds 100ml
Chloroazotic acidLeach, 60 ℃ are stirred 2h, filter and the thorough washing precipitation, obtain containing the solution 162g of platinic compound, the mass percent concentration that records Pt in the solution through atomic absorption spectrum is 0.017w%, calculates wherein Pt content 0.0275g, and the leaching rate of Pt is 83.3w%.
Below according to U.S. Patent No. 5,797,977 methods that reclaim about platinum: at first regulate pH value to 5.5～7 of the solution that contains platinum, remove precipitation with alkali; Add alkali regulator solution pH value to 9.5～10.5 again, remove post precipitation and add ammonium chloride in filtrate, produce the ammonium chloroplatinate precipitation, the ammonium chloroplatinate high-temperature roasting is obtained the high purity spongy platinum, yield is 92.3w%, and the total yield of Pt is 76w%.
Embodiment 1
10.0g contain the industrial Pt/ molecular sieve spent catalyst of 0.350w%Pt, constant temperature is 2 hours in the time of 70 ℃, oxygen level is adjusted to 5.0v%; Constant temperature is 2 hours in the time of 240 ℃, oxygen level is progressively increased be 12.0v%, and constant temperature is 2 hours in the time of 430 ℃, oxygen level is progressively increased be 18.0v%; Constant temperature is 2 hours in the time of 740 ℃, oxygen level is progressively increased be 21v%, and wherein every intersegmental heat-up rate is 5 ℃ of per minutes.(wherein the volumetric molar concentration of clorox is 5mol/L with adding 100ml leaching solution in the above-mentioned sample, the hydrochloric acid volumetric molar concentration is 10mol/L), 200 ℃ are stirred 2h, filter and the thorough washing precipitation, with the pH value to 4 that sodium hydroxide is regulated the solution that contains platinum, remove precipitation; Add sodium hydrate regulator solution pH value to 8 again, remove post precipitation, get the platinum metals product with hydrazine hydrate reduction, high-temperature roasting obtains high purity platinum, calculates wherein Pt content 0.0335g, and the total yield of Pt is 95.7w%.
Embodiment 2
10.0g contain the industrial Pt/ aluminum oxide spent catalyst of 0.250w%Pt, constant temperature is 1 hour in the time of 70 ℃, oxygen level is adjusted to 5.0v%; Constant temperature is 2 hours in the time of 250 ℃, oxygen level is progressively increased be 12.0v%, and constant temperature is 2 hours in the time of 450 ℃, oxygen level is progressively increased be 18.0v%; Constant temperature is 3 hours in the time of 760 ℃, oxygen level is progressively increased be 21v%, and wherein every intersegmental heat-up rate is 6 ℃ of per minutes.Above-mentioned sample is added 150ml leaching solution (wherein the clorox volumetric molar concentration is 5mol/L, and sour volumetric molar concentration is 5mol/L, and the sodium-chlor volumetric molar concentration is 5mol/L), 150 ℃ are stirred 3h, filter and the thorough washing precipitation,, remove precipitation with the pH value to 5 that sodium hydroxide is regulated the solution that contains platinum; Add sodium hydrate regulator solution pH value to 9 again, remove post precipitation, get the platinum metals product with hydrazine hydrate reduction, high-temperature roasting obtains high purity platinum, calculates wherein Pt content 0.024g, and the total yield of Pt is 96.0w%.
Embodiment 3
10.0g contain the industrial Pd/ aluminum oxide spent catalyst of 0.30w%Pd, constant temperature is 2 hours in the time of 50 ℃, oxygen level is adjusted to 8.0v%; Constant temperature is 2 hours in the time of 230 ℃, oxygen level is progressively increased be 15.0v%, and constant temperature is 2 hours in the time of 420 ℃, oxygen level is progressively increased be 18.0v%; Constant temperature is 2 hours in the time of 700 ℃, oxygen level is progressively increased be 21v%, and wherein every intersegmental heat-up rate is 4 ℃ of per minutes.Above-mentioned sample is added 500ml leaching solution, and (wherein the clorox volumetric molar concentration is 10mol/L, the nitric acid volumetric molar concentration is 10mol/L, the sodium-chlor volumetric molar concentration is 5mol/L), 100 ℃ are stirred 5h, filter and the thorough washing precipitation, with the pH value to 5 that sodium hydroxide is regulated the solution that contains platinum, remove precipitation; Add sodium hydrate regulator solution pH value to 9 again, remove post precipitation, get the platinum metals product with hydrazine hydrate reduction, high-temperature roasting obtains high purity platinum, calculates wherein Pd content 0.0276g, and the total yield of Pd is 92.0w%.
Embodiment 4
10.0g contain the industrial Pt/ amorphous silicon aluminium spent catalyst of 0.60w%Pt, constant temperature is 2 hours in the time of 100 ℃, oxygen level is adjusted to 4.0v%; Constant temperature is 2 hours in the time of 300 ℃, oxygen level is progressively increased be 12.0v%, and constant temperature is 2 hours in the time of 480 ℃, oxygen level is progressively increased be 16.0v%; Constant temperature is 2 hours in the time of 700 ℃, oxygen level is progressively increased be 21v%, and wherein every intersegmental heat-up rate is 5 ℃ of per minutes.Above-mentioned sample is added 200ml leaching solution, and (wherein the clorox volumetric molar concentration is 10mol/L, the nitric acid volumetric molar concentration is 5mol/L, the sodium-chlor volumetric molar concentration is 5mol/L), 200 ℃ are stirred 2h, filter and the thorough washing precipitation, with the pH value to 5 that sodium hydroxide is regulated the solution that contains platinum, remove precipitation; Add sodium hydrate regulator solution pH value to 9 again, remove post precipitation, get the platinum metals product with hydrazine hydrate reduction, high-temperature roasting obtains high purity platinum, calculates wherein Pt content 0.027g, and the total yield of Pt is 96.6w%.
Claims (10)
1. method that from contain the precious metal spent catalyst, reclaims precious metal, mainly may further comprise the steps: the spent catalyst that contains precious metal is carried out pre-treatment, precious metal is leached in the solution, purifies from solution and reclaim precious metal, it is characterized in that describedly the spent catalyst that contains precious metal is carried out preprocessing process dividing four-stage to carry out:
Fs: at 50-100 ℃, constant temperature 1-3 hour, oxygen level was adjusted to 0.5v%-10.0v%;
Subordinate phase: at 200-300 ℃, constant temperature 1-3 hour, it was 8.0v%-15.0v% that oxygen level is increased;
Phase III: at 400-500 ℃, constant temperature 1-3 hour, it was 13.0v%-19.0v% that oxygen level is increased;
The quadravalence section: at 700-800 ℃, constant temperature 1-2 hour, it was 18v%～21v% that oxygen level is increased.
2. in accordance with the method for claim 1, it is characterized in that describedly the spent catalyst that contains precious metal is carried out preprocessing process dividing four-stage to carry out:
Fs: constant temperature is 1-3 hour in the time of 60-70 ℃, and oxygen level is adjusted to 2.0v%～7.0v%;
Subordinate phase: constant temperature is 1-3 hour in the time of 240-260 ℃, oxygen level is increased be 10.0v%～13.0v%;
Phase III: constant temperature is 1-3 hour in the time of 430-450 ℃, oxygen level is increased be 15.0v%～18.0v%;
The quadravalence section: constant temperature is 1-2 hour in the time of 740-760 ℃, oxygen level is increased be 19.0v%～21v%.
3. according to claim 1 or 2 described methods, it is characterized in that the heat-up rate between described each stage is 1～10 ℃ of a per minute.
4. in accordance with the method for claim 1, it is characterized in that described precious metal is leached immersion liquid used in the solution is the solution that contains clorox, hydrogen ion and chlorion.
5. in accordance with the method for claim 4, it is characterized in that the clorox volumetric molar concentration is 0.1～20mol/L in the described immersion liquid; The hydrogen ion volumetric molar concentration is 0.1～20mol/L; The chlorion volumetric molar concentration is 0.1～20mol/L; The condition of leaching is: leaching solution is 1: 1～1000: 1 with the solid volume ratio, and leaching temperature is 0 ℃～300 ℃, and leaching time is 1h～48h.
6. in accordance with the method for claim 4, it is characterized in that the clorox volumetric molar concentration is 0.2～10mol/L in the described immersion liquid; The hydrogen ion volumetric molar concentration is 0.2～10mol/L; The chlorion volumetric molar concentration is 0.2～10mol/L; The condition of leaching is: leaching solution is 10: 1～100: 1 with the solid volume ratio, 50 ℃～200 ℃ of leaching temperatures, and leaching time is 5h～10h.
7. in accordance with the method for claim 4, it is characterized in that described immersion liquid employing contains clorox, hydrochloric acid and/or muriatic mixing solutions.
8. in accordance with the method for claim 1, it is characterized in that the described spent catalyst that contains precious metal is is carrier with aluminum oxide and/or molecular sieve, precious metal is one or more in palladium, platinum, rhodium and the iridium.
9. in accordance with the method for claim 1, it is characterized in that the described carrier that contains the spent catalyst of precious metal is an aluminum oxide, precious metal is a platinum.
10. in accordance with the method for claim 9, it is characterized in that described from solution, the purification and recovery precious metal employing step-by-step precipitation method, promptly at first regulate pH value to 4～5 of the solution that contains platinum, remove precipitation with alkali; Add alkali regulator solution pH value to 8～9 again, remove post precipitation, get metal platinum with hydrazine hydrate reduction.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85100109A (en) * | 1985-04-01 | 1986-07-16 | 清华大学 | With the platinum in the extraction process recovery spent catalyst |
| CN1024686C (en) * | 1991-06-24 | 1994-05-25 | 中国有色金属工业总公司昆明贵金属研究所 | Platinum recovery from waste catalyst |
| CN1038199C (en) * | 1994-11-30 | 1998-04-29 | 核工业北京化工冶金研究院 | Recovery of platinum family elements from waste catalysts |
| RU2111791C1 (en) * | 1997-06-17 | 1998-05-27 | Нижегородский нефтеперерабатывающий научно-исследовательский центр | Method for extraction of platinum of waste platinum-containing catalysts on the base of aluminium oxide |
| CN1385545A (en) * | 2002-05-24 | 2002-12-18 | 张方宇 | Method for recovering platinum, palladium and rhodium from waste catalyst in car tail gas |
| CN1205345C (en) * | 2002-04-04 | 2005-06-08 | 中国石油化工股份有限公司 | Method of recovering noble metal from spent catalyst containing noble metal |
-
2006
- 2006-05-19 CN CNB2006100466346A patent/CN100400684C/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85100109A (en) * | 1985-04-01 | 1986-07-16 | 清华大学 | With the platinum in the extraction process recovery spent catalyst |
| CN1024686C (en) * | 1991-06-24 | 1994-05-25 | 中国有色金属工业总公司昆明贵金属研究所 | Platinum recovery from waste catalyst |
| CN1038199C (en) * | 1994-11-30 | 1998-04-29 | 核工业北京化工冶金研究院 | Recovery of platinum family elements from waste catalysts |
| RU2111791C1 (en) * | 1997-06-17 | 1998-05-27 | Нижегородский нефтеперерабатывающий научно-исследовательский центр | Method for extraction of platinum of waste platinum-containing catalysts on the base of aluminium oxide |
| CN1205345C (en) * | 2002-04-04 | 2005-06-08 | 中国石油化工股份有限公司 | Method of recovering noble metal from spent catalyst containing noble metal |
| CN1385545A (en) * | 2002-05-24 | 2002-12-18 | 张方宇 | Method for recovering platinum, palladium and rhodium from waste catalyst in car tail gas |
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