CN107841635A - A kind of friendly process of argentiferous dead catalyst synthetical recovery - Google Patents
A kind of friendly process of argentiferous dead catalyst synthetical recovery Download PDFInfo
- Publication number
- CN107841635A CN107841635A CN201711104014.8A CN201711104014A CN107841635A CN 107841635 A CN107841635 A CN 107841635A CN 201711104014 A CN201711104014 A CN 201711104014A CN 107841635 A CN107841635 A CN 107841635A
- Authority
- CN
- China
- Prior art keywords
- silver
- colored
- friendly process
- catalyst
- leaching
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet processes
- C22B11/042—Recovery of noble metals from waste materials
- C22B11/048—Recovery of noble metals from waste materials from spent catalysts
-
- 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
Abstract
The present invention discloses a kind of friendly process for handling argentiferous dead catalyst, belongs to recovery technology field；Using a kind of argentiferous dead catalyst as raw material, insoluble silver therein is first reduced to silver soluble, then with dust technology and M preparations Selectively leaching silver, silver is set to be transferred to solution, separated with undissolved carrier, carrier is not destroyed, once purged to return factory's reuse or utilized as aluminium silicon resource；Liquid adds the heavy silver of hydrochloric acid after leaching, and silver is converted into silver nitride precipitation, and the silver-colored mother liquor that sinks returns to leaching after processing and recycled；Precipitate it is scrubbed after reduced to obtain pure sponge silver in the basic conditions with hydrogen peroxide；Reduction tail washings obtains sodium chloride product after multiple-effect evaporation.The silver-colored high income of the present invention, exhaust gas production is few, and reagent consumption is reduced, and cost recovery is low, and comprehensive resource utilization rate is high, non-wastewater discharge, is truly realized the purpose of pollution-free synthetical recovery, is a kind of new green environment protection metallurgical technology.
Description
Technical field
The invention belongs to chemical industry recovery technology field, is related to a kind of friendly process of argentiferous dead catalyst synthetical recovery.
Background technology
Silver catalyst is one of important petrochemical catalyst, with industrial expansion, the shortage of resource, dead catalyst
Secondary resource of the middle silver as preciousness, there is very big recovery value.
The carrier of silver catalyst is mainly the method for aluminum oxide or silica, at present domestic recovery argentiferous dead catalyst, greatly
More recovery silver therein, and wherein carrier is not utilized.And the method for reclaiming silver, typically there are two kinds of pyrogenic process or wet method,
The usual high energy consumption of pyrogenic process, pollution is big, the rate of recovery is low, so at present use wet method more.Wet method is mostly first will using appropriate method
Silver-colored dissolution, is transferred in solution from solid-state, then extracts again.The dissolving method of usual argentiferous dead catalyst has sulfuric acid high pressure dissolution method
With nitric acid dissolution method.Sulfuric acid high pressure dissolution method is high to equipment requirement, and base metal sulphates content is high in solution, is unfavorable for follow-up
Silver-colored recovery in solution；Nitric acid dissolution method is that the common method of silver is dissolved from argentiferous dead catalyst, and solvability is strong, leaching rate
Height, but dissolving can produce substantial amounts of oxides of nitrogen gas, and operating environment is poor.It is and main for the method for elemental silver from silver ion reduction
Reducing process, the most common method of domestic reduction silver is ammonia-hydrazine reducing process at present, i.e., by silver chlorate with ammoniacal liquor adjust pH value to
It is silver-colored with hydrazine hydrate reduction after alkalescence, and ammonia-hydrazine reducing process introduces NH4 +, problem be present in wastewater treatment.
The Exemplary patents CN 19979961A of presently relevant argentiferous waste catalyst recovery disclose a kind of from the useless catalysis of argentiferous
The method of electrodeposition recovery silver, is leached to obtain silver nitrate solution with concentrated nitric acid, is filtered by precision filtration equipment in agent, obtained filter
Liquid passes through the swirl flow electrolytic deposition desilverization, and obtained silver powder is collected into trap by the collector of bottom, with pure water,
Dry, founding obtains the silver that purity is 99.99%, the rate of recovery 98.8%.The advantages of method is that obtained silver purity is high,
The rate of recovery is high, and shortcoming is that concentrated nitric acid produces substantial amounts of nitrogen dioxide waste gas, environmental pollution weight when leaching.
The content of the invention
The purpose of the present invention is to leach that nitrogen oxides is more, reagent disappears for existing argentiferous waste catalyst recovery technique is existing
Consumption is big, high energy consumption, the shortcomings of waste liquid is more, pollution is heavy, silver raising recovery rate is low, carrier does not reclaim, there is provided a kind of silver-colored spent catalyst is comprehensive
The friendly process of recovery is closed, present invention process is simple, pollution is small, cost is low, high income and noble silver, carrier, waste water obtain
It is green with comprehensive utilization.
The purpose of the present invention is achieved through the following technical solutions, a kind of green work of silver-colored spent catalyst synthetical recovery
Skill, using a kind of argentiferous dead catalyst as raw material, under certain condition, insoluble silver therein is first reduced to silver soluble, so
Afterwards with dust technology and M preparations Selectively leaching silver, silver is transferred to solution, separated with undissolved carrier, carrier is not destroyed, warp
Clean Hou Fan factory's reuses or utilized as aluminium silicon resource；Liquid adds the heavy silver of hydrochloric acid after leaching, and silver is converted into silver nitride precipitation, sinks silver-colored
Mother liquor returns to leaching after processing and recycled；Precipitate it is scrubbed after reduced to obtain pure sponge in the basic conditions with hydrogen peroxide
Silver；Reduction tail washings obtains sodium chloride product after multiple-effect evaporation；Specifically include following steps：
(1) silver-colored spent catalyst is subjected to reduction treatment, insoluble silver therein is reduced to silver soluble, reduced
Silver catalyst afterwards；
(2) to the leachate Selectively leaching silver of the silver-containing catalyst after reduction, silver is made to be transferred to solution；
(3) the heavy silver of leachate, silver are converted into silver nitride precipitation, and the silver-colored mother liquor that sinks returns to leaching after processing and recycled；Chlorine
Change silver-colored refining reduction, silver nitride precipitation is filtered, adjusts pH to alkalescence with sodium hydroxide after washing, is then reduced with hydrogen peroxide,
Generate pure silver powder product.
Preferably, the step (1) by insoluble silver chlorate be converted into silver reaction condition be：Raw material weight proportioning of soup processed is：
Silver-colored spent catalyst：Water：Reducing agent=1:(1~2)：(0.001~0.002), wherein, reducing agent is formic acid or hydrazine hydrate, instead
Answer 50~70 DEG C of temperature, reaction time 0.5h.
Preferably, the liquid-solid ratio of the Leach reaction of the step (2) is 1:1, " liquid " refers to leachate, dust technology and M preparations
Mixture, " Gu " refer to silver-colored spent catalyst, Leach reaction is carried out at normal temperatures, and the reaction time is 0.5~1h, dust technology and M
The proportioning of preparation is 1:(0.3~0.7)；The M preparations be at 0~30 DEG C, under 0~0.4MPa, the oxide or salt of iron with
Oxidant is by weight 1:100~200 are formulated mixture.
Preferably, the leaching in the step (2), leachate is gone out under by circulating sprayer it is enterprising by the way of
Circulation spraying is carried out, caused nitrogen oxides is preferably adsorbed by M preparations and resolves into nitrogen and oxygen during making, and solution follows
Circular rector is 0.1~0.2 times of liquor capacity/min.
Preferably, the oxidant in the M preparations is hydrogen peroxide or Ozone Water.
Preferably, the precipitating reagent of heavy silver is using hydrochloric acid, the heavy silver-colored mother liquid disposal in the step (3)：Heavy silver
Return to leach after mother liquor, soluble silver salt, the allotment of M preparations and recycle, heavy silver-colored mother liquor, soluble silver salt, M weight of formulation proportioning
For 1:0.003:(0.1~0.5).
Preferably, the refining reduction condition of silver chlorate is controlled 10~14 for pH value in the step (3), and reduction temperature exists
60~80 DEG C, reduction silver powder purity is more than more than 99.95%.
Preferably, the tail washings after the silver chlorate refining reduction is sodium chloride crystal through multiple-effect evaporation condensing crystallizing.
Compared with prior art, the beneficial effects of the invention are as follows：
First, the participation of M preparations of the present invention, during making caused nitrogen oxides adsorbed rapidly and resolve into nitrogen and
Oxygen, the effusion of system nitrogen oxides is avoided, reduce exhaust gas production from source, it is environmentally friendly；Meanwhile M preparations
Participate in, accelerate reaction process, shorten the reaction time, reaction can be carried out at normal temperatures.
Second, liquid circulating leaching after the heavy silver of leachate, nitron consumption reduces more than 40%, realizes production process and subtract
Quantify；Sodium chloride product, non-wastewater discharge is made in reduction tail washings；Leaching process is circulated using solution, makes nitrogen oxide absorbent point
Solution is more thorough, and does not destroy carrier, carrier can reuse or as bauxite resource utilize, reduce waste sludge discharge.
3rd, whole technique is carried out under the conditions of totally-enclosed, and flow is succinct, science, and production cost is low, and silver raising recovery rate is high,
The purpose of pollution-free synthetical recovery is truly realized, is a kind of new green environment protection metallurgical technology.
4th, the present invention not only discharge by extract technology nitrogenfree oxide, and reducing process produces without waste water, and middle interstitial fluid can follow
Ring uses, and the few cost of reagent dosage is low, and silver raising recovery rate is high, and carrier, waste water, which are obtained for, to be made full use of, and energy consumption is low, environment-friendly.
Brief description of the drawings
Fig. 1 is present invention process flow chart.
Embodiment
Below with reference to specific embodiment, the method for conventional method and the present invention is contrasted, and the present invention is retouched
State, it is necessary to illustrate, these embodiments are only descriptive, without limiting the invention in any way.
Embodiment 1 (conventional method)
(1) take certain argentiferous dead catalyst 1000g to be put into 2000mL reactor (raw material argentiferous 11.5%), add and prepare
Good 2.0mol/L salpeter solution 1500mL, reactor top have slight tobacco to occur, 60~80 DEG C of controlling reaction temperature, leaching
Go out to react 45min, pour out leachate；The 2.0mol/L prepared salpeter solution 1000mL is added, second is carried out and leaches,
60~80 DEG C of controlling reaction temperature, Leach reaction 30min, pours out leachate, and two-stage leaching liquid is merged and filtered, and by insoluble load
Body is washed with water to neutrality, and wash water merges mixing with leachate, and it is 37.40g/L to survey silver concentration in solution, and overall solution volume is
3000L, silver leaching rate 97.57%, it is 3073ppm to detect silver content in carrier；
(2) above-mentioned filtrate is generated into silver nitride precipitation, precipitation filtering, washing with the heavy silver of hydrochloric acid, silver；
(3) silver chlorate ammoniacal liquor-hydrazine hydrate reduction after washing, it is silver powder to silver-colored Restore All, filtered, washing is dried
It is dry to obtain silver powder 111.68g, silver powder purity 99.96%, silver raising recovery rate 97.11%.
Embodiment 2 (the inventive method)
(1) take certain argentiferous dead catalyst 1000g to be put into 2000mL reactor (raw material argentiferous 11.5%), add and prepare
Good reducing solution 1500mL, 60 DEG C of circular response 30min, stop heating, extract supernatant out after static clarification；
(2) 2.0mol/L prepared salpeter solution 1000mL is added, is uniformly slowly added to M catalyst at room temperature, and
Go out under it is enterprising by the way of circulating leaching liquid, whole course of reaction without tobacco generate, Leach reaction 30min, leachate is fallen
Go out, and insoluble slag is washed with water to neutrality, wash water merges mixing with leachate, and it is 57.26g/L to survey silver concentration in solution, solution
Cumulative volume is 2000mL, and silver leaching rate 99.58%, it is 499.8ppm to detect silver content in carrier；
(2) above-mentioned filtrate is generated into silver nitride precipitation, precipitation filtering, washing with the heavy silver of hydrochloric acid, silver；
(3) silver chlorate after washing adjusts pH value to 10~14 with sodium hydroxide, is slowly added to hydrogen peroxide, extremely silver is whole also
Originally it was silver powder, filtered, washing and drying obtains silver powder 113.98g, silver powder purity 99.96%, the rate of recovery 99.11%；
(4) sodium chloride 61.54g is obtained after evaporation and concentration to reduction tail washings.
Embodiment 3 (the inventive method)
(1) by argentiferous dead catalyst, (carrier is α-Al2O3) 3000 grams (argentiferous 11.5wt%), it is divided into 3 parts, every part 1000
Gram, numbering is 1#, 2#, 3# respectively, is separately added into reducing solution 1500mL, the 60 DEG C of circular response 30min prepared, stops adding
Heat, supernatant is extracted out after static clarification；
(2) it is uniformly slow at room temperature to the salpeter solution 1000mL of addition 2.0mol/L in the 1# reactors after the completion of reduction
It is slow to add M catalyst, and go out under usinging it is enterprising by the way of circulating leaching liquid, whole course of reaction is without tobacco generation, Leach reaction
30min, silver are transferred to solution, obtain argentiferous leachate, are extracted out after standing clarification, and insoluble slag is washed with water to neutrality, wash water with
Leachate, which merges, to be mixed；
(3) the heavy silver processing of argentiferous leachate progress hydrochloric acid to obtaining, obtains silver salt and heavy silver-colored mother liquor；
(4) it is used to carry out leaching process to 2# after heavy silver-colored mother liquor is handled；
(5) aforesaid operations are repeated, 2#, 3# after reduction treatment are leached respectively successively, heavy silver processing, leaching process
It is middle to supplement appropriate salpeter solution to process ratio.Treat that 1~3# materials leach, after the completion of heavy silver, solution total amount is 4000mL, entirely
Process consumption 2.0mol/L nitric acid total amount is 1780mL；
(6) 1#~3# materials are leached, the carrier merging mixing that washing post processing obtains, sampling detection, silver contains in carrier
Measure as 167.6ppm；The total leaching rate of 1#~3# materials is 99.87%
(7) above-mentioned all silver salt are merged and carries out reduction treatment, adjusted pH value to 10~14 with sodium hydroxide, be slowly added to
Hydrogen peroxide, is silver powder to silver-colored Restore All, and filtered, washing and drying obtains silver powder 342.65g, silver powder purity 99.96%, recovery
Rate 99.32%；
(8) sodium chloride 185.18g is obtained after evaporation and concentration to last reduction tail washings.
Three kinds of embodiments leach and recovery Comparative result table
Claims (8)
1. a kind of friendly process of silver-colored spent catalyst synthetical recovery, it is characterised in that including lower step：
（1）Silver-colored spent catalyst is subjected to reduction treatment, insoluble silver therein is reduced to silver soluble, after being reduced
Silver-containing catalyst；
（2）To the leachate Selectively leaching silver of the silver-containing catalyst after reduction, silver is set to be transferred to solution；
（3）The heavy silver of leachate, silver are converted into silver nitride precipitation, and the silver-colored mother liquor that sinks returns to leaching after processing and recycled；Silver chlorate
Refining reduction, silver nitride precipitation is filtered, adjusts pH to alkalescence with sodium hydroxide after washing, is then reduced, generated with hydrogen peroxide
Pure silver powder product.
2. the friendly process of silver-colored spent catalyst synthetical recovery according to claim 1, it is characterised in that the step
（1）Insoluble silver chlorate is converted into silver-colored reaction condition is：Raw material weight proportioning of soup processed is：Silver-colored spent catalyst：Water：Reducing agent=
1:（1~2）：（0.001~0.002）, wherein, reducing agent is formic acid or hydrazine hydrate, 50 ~ 70 DEG C of reaction temperature, and the reaction time is
0.5h。
3. the friendly process of silver-colored spent catalyst synthetical recovery according to claim 1, it is characterised in that the step
（2）Leach reaction liquid-solid ratio be 1:1, " liquid " refers to leachate, is the mixture of dust technology and M preparations, " Gu " refer to silver-colored failure
Catalyst, Leach reaction are carried out at normal temperatures, and the reaction time is 0.5 ~ 1h, dust technology:The proportioning of M preparations is 1:（0.3~0.7）；
The M preparations are at 0 ~ 30 DEG C, and under 0 ~ 0.4MPa, the oxide or salt and oxidant of iron are by weight 1:100 ~ 200 prepare
And resulting mixture.
4. the friendly process of silver-colored spent catalyst synthetical recovery according to claim 3, it is characterised in that the step
（2）In leaching, leachate is gone out under by circulating sprayer it is enterprising by the way of carry out circulation spraying, produced during making
Raw nitrogen oxides is adsorbed by M preparations and resolves into nitrogen and oxygen, and solution internal circulating load is 0.1 ~ 0.2 times of liquor capacity/min.
5. the friendly process of silver-colored spent catalyst synthetical recovery according to claim 4, it is characterised in that the M preparations
In oxidant be hydrogen peroxide or Ozone Water.
6. the friendly process of silver-colored spent catalyst synthetical recovery according to claim 1, it is characterised in that the step
（3）In sink silver precipitating reagent be using hydrochloric acid, the heavy silver-colored mother liquid disposal：Heavy silver-colored mother liquor, soluble silver salt, M preparations are adjusted
Return to leach after matching somebody with somebody and recycle, heavy silver-colored mother liquor, soluble silver salt, M weight of formulation proportioning are 1:0.003:（0.1~0.5）.
7. the friendly process of silver-colored spent catalyst synthetical recovery according to claim 1, it is characterised in that the step
（3）The refining reduction condition of middle silver chlorate is that pH value is controlled 10 ~ 14, and at 60 ~ 80 DEG C, reduction silver powder purity is more than reduction temperature
More than 99.95%.
8. according to the friendly process of claim 1 argentiferous dead catalyst synthetical recovery, it is characterised in that the silver chlorate refining is also
Tail washings after original is sodium chloride crystal through multiple-effect evaporation condensing crystallizing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711104014.8A CN107841635A (en) | 2017-11-10 | 2017-11-10 | A kind of friendly process of argentiferous dead catalyst synthetical recovery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711104014.8A CN107841635A (en) | 2017-11-10 | 2017-11-10 | A kind of friendly process of argentiferous dead catalyst synthetical recovery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107841635A true CN107841635A (en) | 2018-03-27 |
Family
ID=61682601
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711104014.8A Pending CN107841635A (en) | 2017-11-10 | 2017-11-10 | A kind of friendly process of argentiferous dead catalyst synthetical recovery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107841635A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108588429A (en) * | 2018-06-01 | 2018-09-28 | 贵研资源（易门）有限公司 | The method that gold and silver is recycled from sandblasting waste material and failure silver catalyst for ethylene oxide |
| CN109516599A (en) * | 2018-12-19 | 2019-03-26 | 河北德龙环境工程股份有限公司 | The polymorphic silver separation sub-prime device of one kind and sewage water treatment method |
| CN110735041A (en) * | 2019-08-28 | 2020-01-31 | 广西银亿高新技术研发有限公司 | process method for leaching insoluble metal waste by cyclic catalytic oxidation acid leaching |
| CN111321307A (en) * | 2020-03-07 | 2020-06-23 | 江苏北矿金属循环利用科技有限公司 | Process for efficiently recovering palladium from palladium-containing waste catalyst |
| CN111364060A (en) * | 2020-04-07 | 2020-07-03 | 昆明寰世科技开发有限公司 | Method for producing pure silver and co-producing metal aluminum from waste silver catalyst with alumina as carrier |
| CN113308609A (en) * | 2021-05-26 | 2021-08-27 | 江苏北矿金属循环利用科技有限公司 | Method for clean recovery and resource utilization of spent silver-containing waste catalyst |
| CN114807605A (en) * | 2022-03-09 | 2022-07-29 | 金川集团股份有限公司 | Method for updating silver electrolyte by hydrogen peroxide |
| CN115747503A (en) * | 2022-12-27 | 2023-03-07 | 江苏电科环保有限公司 | Improved recovery method of waste film |
| CN115852158A (en) * | 2022-12-14 | 2023-03-28 | 核工业北京化工冶金研究院 | Method for recovering silver from silver-containing waste catalyst |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070098609A1 (en) * | 2005-10-29 | 2007-05-03 | Mcconnell Brian | Hydrometallurgical process for the treatment of metal-bearing sulfide mineral concentrates |
| EP2123341A2 (en) * | 2008-05-21 | 2009-11-25 | W.C. Heraeus GmbH | Recycling method for catalytic mould |
| CN103074500A (en) * | 2012-12-27 | 2013-05-01 | 徐州浩通新材料科技股份有限公司 | Method for producing high-purity silver powder by using silver-containing dead catalyst |
| CN103526034A (en) * | 2013-10-21 | 2014-01-22 | 昆明贵研催化剂有限责任公司 | Method for activating and leaching platinum group metals from automobile spent catalysts by wet method |
| CN105886785A (en) * | 2015-01-25 | 2016-08-24 | 昆明冶金高等专科学校 | Method for preparing high-purity silver powder from silver-rich residue containing high selenium and tellurium |
| CN106474893A (en) * | 2016-12-15 | 2017-03-08 | 中国科学院过程工程研究所 | The flue gas desulfurization and denitration technique that a kind of ozone oxidization combination slag absorbs |
-
2017
- 2017-11-10 CN CN201711104014.8A patent/CN107841635A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070098609A1 (en) * | 2005-10-29 | 2007-05-03 | Mcconnell Brian | Hydrometallurgical process for the treatment of metal-bearing sulfide mineral concentrates |
| EP2123341A2 (en) * | 2008-05-21 | 2009-11-25 | W.C. Heraeus GmbH | Recycling method for catalytic mould |
| CN103074500A (en) * | 2012-12-27 | 2013-05-01 | 徐州浩通新材料科技股份有限公司 | Method for producing high-purity silver powder by using silver-containing dead catalyst |
| CN103526034A (en) * | 2013-10-21 | 2014-01-22 | 昆明贵研催化剂有限责任公司 | Method for activating and leaching platinum group metals from automobile spent catalysts by wet method |
| CN105886785A (en) * | 2015-01-25 | 2016-08-24 | 昆明冶金高等专科学校 | Method for preparing high-purity silver powder from silver-rich residue containing high selenium and tellurium |
| CN106474893A (en) * | 2016-12-15 | 2017-03-08 | 中国科学院过程工程研究所 | The flue gas desulfurization and denitration technique that a kind of ozone oxidization combination slag absorbs |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108588429A (en) * | 2018-06-01 | 2018-09-28 | 贵研资源（易门）有限公司 | The method that gold and silver is recycled from sandblasting waste material and failure silver catalyst for ethylene oxide |
| CN109516599A (en) * | 2018-12-19 | 2019-03-26 | 河北德龙环境工程股份有限公司 | The polymorphic silver separation sub-prime device of one kind and sewage water treatment method |
| CN110735041A (en) * | 2019-08-28 | 2020-01-31 | 广西银亿高新技术研发有限公司 | process method for leaching insoluble metal waste by cyclic catalytic oxidation acid leaching |
| CN111321307A (en) * | 2020-03-07 | 2020-06-23 | 江苏北矿金属循环利用科技有限公司 | Process for efficiently recovering palladium from palladium-containing waste catalyst |
| CN111364060A (en) * | 2020-04-07 | 2020-07-03 | 昆明寰世科技开发有限公司 | Method for producing pure silver and co-producing metal aluminum from waste silver catalyst with alumina as carrier |
| CN113308609A (en) * | 2021-05-26 | 2021-08-27 | 江苏北矿金属循环利用科技有限公司 | Method for clean recovery and resource utilization of spent silver-containing waste catalyst |
| CN114807605A (en) * | 2022-03-09 | 2022-07-29 | 金川集团股份有限公司 | Method for updating silver electrolyte by hydrogen peroxide |
| CN114807605B (en) * | 2022-03-09 | 2024-03-01 | 金川集团股份有限公司 | Method for updating silver electrolyte by hydrogen peroxide |
| CN115852158A (en) * | 2022-12-14 | 2023-03-28 | 核工业北京化工冶金研究院 | Method for recovering silver from silver-containing waste catalyst |
| CN115747503A (en) * | 2022-12-27 | 2023-03-07 | 江苏电科环保有限公司 | Improved recovery method of waste film |
| CN115747503B (en) * | 2022-12-27 | 2023-12-15 | 江苏电科环保有限公司 | Improved recovery method of waste film |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107841635A (en) | A kind of friendly process of argentiferous dead catalyst synthetical recovery | |
| CN102071319B (en) | Method for preparing high-purity silver from silver-containing waste liquid | |
| CN103526016B (en) | A kind of method of raw material containing lead hydrometallurgic recovery | |
| CN103789550B (en) | The recovery method of vanadium potassium silicon in spent vanadium catalyst | |
| CN112410556B (en) | Method for recovering waste lithium iron phosphate powder | |
| CN105969993A (en) | Comprehensive recycling method for high-arsenic soot | |
| CN106435197A (en) | Process and device for alkaline extraction and recovery from waste catalysts in SCR (selective catalytic reduction) denitrification | |
| WO2023246080A1 (en) | Method for recycling industrial waste salt and waste denitration catalyst | |
| CN109536726A (en) | A kind of recovery method of argentiferous dead catalyst | |
| CN105776333A (en) | Preparation method of vanadium pentoxide | |
| CN106111051A (en) | A kind of red mud extracts ferrum, aluminum for the method for adsorbent and application | |
| CN113336258A (en) | Method for preparing active copper oxide from sponge copper | |
| CN110510648A (en) | A method of separating and recovering aluminium, potassium and ammonium from the mixed solution of sulfur acid aluminium, potassium sulfate and ammonium sulfate | |
| CN106086417A (en) | A kind of method extracting copper and gold from waste mobile phone circuit board | |
| CN107022681A (en) | A kind of comprehensive recovering process of aluminium scrap silicon middle rare earth, aluminium and silicon | |
| CN105200248B (en) | A kind of step of utilization carbide slag one neutralizes the method that titanium white waste acid prepares high-purity scandium | |
| CN112591782B (en) | Conversion and purification method of low-consumption dihydrate phosphogypsum | |
| CN106542506A (en) | A kind of method that selenium is reclaimed from heavy tellurium waste liquid | |
| CN111304451B (en) | Method for recycling waste vanadium catalyst by using phosphoric acid solution | |
| CN116143174B (en) | Method for preparing ammonium paratungstate by scheelite short process | |
| CN108946795B (en) | Method for preparing high-purity basic lead carbonate by using lead-containing dedusting ash | |
| CN111268718A (en) | Method for directly preparing mercury oxide from mercury-containing organic sludge | |
| CN113234941B (en) | High-value utilization method of electrolytic manganese anode slime | |
| CN105983707A (en) | Method for preparing high-purity rhenium powder from rhenium-containing high-arsenic copper sulfide | |
| CN107619938B (en) | A method of silver-colored ruthenium being purified in ruthenium compound tail washings from preparing |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180327 |
|
| RJ01 | Rejection of invention patent application after publication |