CN108067244A - A kind of spent catalyst recovery method - Google Patents
A kind of spent catalyst recovery method Download PDFInfo
- Publication number
- CN108067244A CN108067244A CN201611011393.1A CN201611011393A CN108067244A CN 108067244 A CN108067244 A CN 108067244A CN 201611011393 A CN201611011393 A CN 201611011393A CN 108067244 A CN108067244 A CN 108067244A
- Authority
- CN
- China
- Prior art keywords
- solution
- catalyst
- nickel
- molybdenum
- method described
- 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.)
- Granted
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/85—Chromium, molybdenum or tungsten
- B01J23/88—Molybdenum
- B01J23/883—Molybdenum and nickel
-
- 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
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/009—General processes for recovering metals or metallic compounds 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Environmental & Geological Engineering (AREA)
- Geology (AREA)
- Manufacturing & Machinery (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Life Sciences & Earth Sciences (AREA)
- Catalysts (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention discloses a kind of spent catalyst recovery method, including following content：（1）Molybdenum nickel system dead catalyst is stripped, is dried, microwave treatment, crushing；（2）Catalyst after crushing with alkali is mixed, then carries out high-temperature roasting；（3）Calcined catalyst is subjected to Hot water immersion, filtering, meta-aluminate filtrate and nickel oxide solid is made；（4）By step（3）Middle filtrate and aluminium salt acidity solution reaction filter, prepare boehmite, and boehmite kneading, shaping, roasting are made carrier；（5）By step（4）The solution filtered out carries out activated carbon adsorption molybdenum, is desorbed after absorption using ammonium hydroxide, and ammonium molybdate solution is made；（6）To step（3）Solid adds in acid after middle filter, then removes Fe and Al in solution using alkaline solution adjustment pH value, concentrates and nickel salt solution is made；（7）By step（6）In nickel nitrate solution be added to step（5）Solution in, molybdenum nickel ammonia solution is made；（8）Utilize step（4）Middle carrier and step（7）Middle solution is impregnated, dried, roasted, and catalyst is made.This method has the characteristics that simple for process, processing cost is low.
Description
Technical field
Present document relates to a kind of spent catalyst recovery methods, relate in particular to a kind of utilization molybdenum nickel system dead catalyst system
The method of standby hydrogenation catalyst, especially for distillate molybdenum nickel series hydrogenating catalyst.
Technical background
In modern times oil refining and chemical industry, realized by catalytic process during more than 90% chemical reaction, catalyst into
To realize that oil refining and the exploitation of the new process new product of chemical industry are crucial.But catalyst is when being changed into dead catalyst, to environment gesture
It must cause certain harm.When the residual oil hydrocatalyst basic service life is 8000 small at present, often covers residual hydrogenation equipment and every year
Hundreds of tons of dead catalyst is generated, domestic more than ten sets of residual hydrogenation equipment existing at present, country's residual oil dead catalyst is reachable every year
Tons up to ten thousand.Molybdenum nickel active metallic content is low with respect to other catalyst on residual oil hydrocatalyst, and catalyst returned enterprise is led at present
What is considered is metal recovery problem, is used for alumina support essentially as waste residue to cement or Ceramics Enterprises, carrier
Utilization rate is too low.Active metal and alumina support recycling become an important side of current hydrogenation catalyst research
To.
Technical comparing at present on aluminium base waste catalyst recovery metal is more.CN941106479.6 proposes that pyrogenic process recycling is useless
Ni in catalyst, this method need higher calcination temperature.CN200910020761.2 proposes to return from molybdenum-contained waste catalyst
The method for receiving metal, this method is to crush catalyst, then proposes Mo with soda ash hybrid reaction etc..CN200910020761.2
A kind of method that molybdenum is recycled in catalyst aluminium base dead catalyst is disclosed, this method is also to crush catalyst, mixes and forges with alkali
Burn etc., extract molybdenum.CN200410050503.6 discloses a kind of method using vanadium-containing wasting catalyst production vanadic anhydride, should
Method is that first removing deposition is oily, is crushed, and recycling sodium vanadate and the sodium molybdate, then roast successively such as leaching leach, secondary recovery vanadic acid
Vanadium pentoxide is finally made in sodium and sodium molybdate.US4544533 is disclosed recycles metal from waste loading type hydrotreating catalyst
Method, then this method leaches metal using roasting away coke and sulfur-containing slag from dead catalyst.US4514369 is public
The metal on the methods of being separated by liquid-liquid extraction acquisition dead catalyst is opened.Existing dead catalyst recycles, and mainly examines
Consider the recycling of metal or more changing device reuses, the simple recycling of metal, substantial amounts of alumina support is caused to waste, and give up
Catalyst change device is can not to meet all spent catalysts to recycle.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of method that molybdenum nickel waste catalyst recovery prepares raw catelyst, it is special
It is not distillate treating catalyst.This method has the features such as simple for process, processing cost is low.
A kind of spent catalyst recovery method, including following content：
（1）Molybdenum nickel system dead catalyst is stripped, is dried, microwave treatment, crushing；
（2）Catalyst after crushing with alkali is mixed, then carries out high-temperature roasting；
（3）Calcined catalyst is subjected to Hot water immersion, filtering, meta-aluminate filtrate and nickel oxide solid is made；
（4）By step（3）Middle filtrate and aluminium salt acidity solution reaction filter, prepare boehmite, and boehmite is mixed
It pinches, be molded, roasting obtained carrier；
（5）By step（4）The solution filtered out carries out activated carbon adsorption molybdenum, is desorbed after absorption using ammonium hydroxide, and it is molten that ammonium molybdate is made
Liquid；
（6）To step（3）Solid adds in acid after middle filter, then removes Fe and Al in solution using alkaline solution adjustment pH value, dense
Contraction obtains nickel salt solution；
（7）By step（6）In nickel nitrate solution be added to step（5）Solution in, molybdenum nickel ammonia solution is made；
（8）Utilize step（4）Middle carrier and step（7）Middle solution is impregnated, dried, roasted, and catalyst is made.
In the above method, step（1）The molybdenum nickel system hydrogenation catalyst content meter by weight that gives up contains catalyst solid
70 ~ 90%, petroleum distillate 10 ~ 30%, the weight content of nickel oxide is 3-10% in the catalyst after extracting, and the weight of molybdenum oxide contains
It measures as 10-25%.For the organic solvent used that extracts for toluene, petroleum ether, ethyl alcohol etc., extraction temperature is 80 ~ 110 DEG C.It is described
Microwave treatment microwave frequency is 915 ~ 2450 MHz, and processing time is 3 ~ 8h.The microwave treatment is preferably in gaseous methanol and nitrogen
It is carried out under the mixed atmosphere of gas, the volume ratio of gaseous methanol and nitrogen is 1:3-1:5.In gaseous methanol and the mixed atmosphere of nitrogen
Lower carry out microwave treatment is conducive to further reduce the active force between molybdenum nickel metal and alumina support, improves subsequent molybdenum
Nickel metal and aluminium oxide efficiently separate, and result of study shows that the process can also play the role of improving catalyst activity.It is described
It crushes as grinding particle size to 200 ~ 400 mesh, preferably 300 ~ 400 mesh.
In the above method, step（2）Described in alkali can be sodium hydroxide, sodium carbonate, one kind in potassium hydroxide or several
Kind, alkali and contained Al in dead catalyst2O3Molar ratio for 4 ~ 1, preferably 2.5 ~ 1.5；The high-temperature roasting temperature for 700 ~
1000 DEG C, preferably 850 ~ 950 DEG C, 2 ~ 6h of roasting time, preferably 3 ~ 5h.
In the above method, step（3）Described in hot water temperature be 85 ~ 110 DEG C, preferably 90-100 DEG C, liquid-solid ratio for 7 ~
3, preferably 6 ~ 4, extraction time are 0.2 ~ 2h, preferably 0.5 ~ 1h.
In the above method, step（4）Described in acid solution for aluminium chloride, aluminum nitrate or aluminum sulfate, acid solution
PH for 1 ~ 3, step（3）Middle filtrate and acid solution reaction controlling pH value 7 ~ 9, preferably 7 ~ 7.5, reaction temperature control are 50
~ 80 DEG C, 500 ~ 1000 DEG C of the carrier calcination temperature.
In the above method, step（5）Middle granularity of activated carbon is 20 ~ 200 mesh, preferably 40 ~ 80 mesh；Adsorption process can add
Enter complexing agent, such as：Hydrochloric acid, 8-hydroxyquinoline etc..
In the above method, step（6）Described in acid for sulfuric acid, the alkaline solution is sodium hydroxide solution, hydrogen-oxygen
It is 2 ~ 15% to change sodium solution mass concentration, preferably 4 ~ 10%；It is 5 ~ 6.5 to adjust pH value, preferably 5.5 ~ 6.2.
In the above method, step（8）Described in drying temperature be 100 ~ 180 DEG C, drying time is 2 ~ 5h, and calcination temperature is
400 ~ 600 DEG C, roasting time is 2 ~ 4h.
The method of the present invention can effectively recycle the active metal and aluminium oxide in molybdenum nickel system dead catalyst after industrial operation, be
A kind of environmental-friendly method for preparing catalyst.Compared with prior art, the thermal stress that microwave treatment generates being capable of molybdenum nickel metal
It is separated with aluminium oxide, improves the organic efficiency of metal and aluminium oxide；Dead catalyst can effectively recycle aluminium oxide and be prepared into hydrogenation
Catalyst carrier；Molybdenum nickel active metal can be recycled, and be re-prepared as metallic solution；This method enables to catalyst to follow
Ring economy uses, and improves environmental aspect, creates good economic benefit.
Specific embodiment
The functions and effects further illustrated the present invention with reference to embodiment.
Example 1
Molybdenum nickel catalyst is stripped de-oiling after taking industrial operation, dry, microwave treatment, processing time 5h；Weigh catalyst
100g is crushed to 300 mesh；Sodium carbonate 166g is weighed, is uniformly mixed with dead catalyst, 850 DEG C of roasting 4h;With 90 DEG C
500g hot water is leached, filtering, remaining filter residue 1.Solution and acid solution after filtering（Aluminum sulfate）In temperature 60 C, pH value is
Boehmite is prepared in the case of 7, filters, obtains filtrate 1；Boehmite with adhesive is mixed, is molded, at 700 DEG C
3h is roasted, obtains 86g carriers;Hydrochloric acid will be slowly added in filtrate 1, be adjusted to acid, be warming up to 60 DEG C, add in the 300g of 200 mesh
Activated carbon carries out activated carbon adsorption；Adsorb 3 it is small when after, desorbed using ammonium hydroxide, be configured to concentration be 0.55g/ml ammonium molybdate it is molten
Liquid；Filter residue 1 is added in into salpeter solution until being completely dissolved, pH value is slowly adjusted to 6.2 using ammonium hydroxide, is filtered, then
Nickel nitrate solution concentration is adjusted to 0.11g/mL；Nickel nitrate solution and ammonium molybdate solution are mixed, are immersed in 80g carriers
On, dry, 98g catalyst A are made in 470 DEG C of roasting 3h,
Example 2
Molybdenum nickel catalyst is stripped de-oiling after taking industrial operation, dry, microwave treatment, processing time 8h；Weigh catalyst
100g is crushed to 300 mesh；Sodium carbonate 166g is weighed, is uniformly mixed with dead catalyst, 850 DEG C of roasting 4h;With 90 DEG C
500g hot water is leached, filtering, remaining filter residue 1.Solution and acid solution after filtering（Aluminum sulfate）In temperature 60 C, pH value is
Boehmite is prepared in the case of 7, filters, obtains filtrate 1；Boehmite with adhesive is mixed, is molded, at 700 DEG C
3h is roasted, obtains 86g carriers;Hydrochloric acid will be slowly added in filtrate 1, be adjusted to acid, be warming up to 60 DEG C, add in the 300g of 100 mesh
Activated carbon carries out activated carbon adsorption；Adsorb 3 it is small when after, desorbed using ammonium hydroxide, be configured to concentration be 0.55g/ml ammonium molybdate it is molten
Liquid；Filter residue 1 is added in into salpeter solution until being completely dissolved, pH value is slowly adjusted to 6.2 using ammonium hydroxide, is filtered, then
Nickel nitrate solution concentration is adjusted to 0.11g/mL；Nickel nitrate solution and ammonium molybdate solution are mixed, are immersed in 80g carriers
On, dry, 98g catalyst B are made in 470 DEG C of roasting 3h,
Example 3
Molybdenum nickel catalyst is stripped de-oiling after taking industrial operation, dry, microwave treatment, processing time 5h；Weigh catalyst
100g is crushed to 300 mesh；Sodium carbonate 166g is weighed, is uniformly mixed with dead catalyst, 850 DEG C of roasting 4h;With 90 DEG C
500g hot water is leached, filtering, remaining filter residue 1.Solution and acid solution after filtering（Aluminum sulfate）In temperature 60 C, pH value is
Boehmite is prepared in the case of 7, filters, obtains filtrate 1；Boehmite with adhesive is mixed, is molded, at 700 DEG C
3h is roasted, obtains 86g carriers;Hydrochloric acid will be slowly added in filtrate 1, be adjusted to acid, be warming up to 60 DEG C, add in the 300g of 200 mesh
Activated carbon carries out activated carbon adsorption, and complexing agent 8-hydroxy-quinoline is added in during activated carbon adsorption；Adsorb 2 it is small when after, adopt solution with ammonia
It inhales, is configured to the ammonium molybdate solution that concentration is 0.55g/ml；Filter residue 1 is added in into salpeter solution until being completely dissolved, using ammonium hydroxide
PH value is slowly adjusted to 6.2, is filtered, nickel nitrate solution concentration is then adjusted to 0.11g/mL；By nickel nitrate solution
It is mixed, is immersed on 80g carriers with ammonium molybdate solution, dry, 98g catalyst C are made in 470 DEG C of roasting 3h,
Example 4
Molybdenum nickel catalyst is stripped de-oiling after taking industrial operation, dry, microwave treatment, processing time 5h, at the microwave
Reason carries out under the mixed atmosphere of gaseous methanol and nitrogen, and the volume ratio of gaseous methanol and nitrogen is 1:3.；Weigh catalyst
100g is crushed to 300 mesh；Sodium carbonate 166g is weighed, is uniformly mixed with dead catalyst, 850 DEG C of roasting 4h;With 90 DEG C
500g hot water is leached, filtering, remaining filter residue 1.Solution and acid solution after filtering（Aluminum sulfate）In temperature 60 C, pH value is
Boehmite is prepared in the case of 7, filters, obtains filtrate 1；Boehmite with adhesive is mixed, is molded, at 700 DEG C
3h is roasted, obtains 86g carriers;Hydrochloric acid will be slowly added in filtrate 1, be adjusted to acid, be warming up to 60 DEG C, add in the 300g of 200 mesh
Activated carbon carries out activated carbon adsorption；Adsorb 3 it is small when after, desorbed using ammonium hydroxide, be configured to concentration be 0.55g/ml ammonium molybdate it is molten
Liquid；Filter residue 1 is added in into salpeter solution until being completely dissolved, pH value is slowly adjusted to 6.5 using ammonium hydroxide, is filtered, then
Nickel nitrate solution concentration is adjusted to 0.11g/mL；Nickel nitrate solution and ammonium molybdate solution are mixed, are immersed in 80g carriers
On, dry, 98g catalyst D are made in 470 DEG C of roasting 3h,
Example 5
Molybdenum nickel catalyst is stripped de-oiling after taking industrial operation, dry, microwave treatment, processing time 5h, at the microwave
Reason carries out under the mixed atmosphere of gaseous methanol and nitrogen, and the volume ratio of gaseous methanol and nitrogen is 1:5.；Weigh catalyst
100g is crushed to 300 mesh；Sodium carbonate 166g is weighed, is uniformly mixed with dead catalyst, 850 DEG C of roasting 4h;With 90 DEG C
500g hot water is leached, filtering, remaining filter residue 1.Solution and acid solution after filtering（Aluminum sulfate）In temperature 60 C, pH value is
Boehmite is prepared in the case of 7, filters, obtains filtrate 1；Boehmite with adhesive is mixed, is molded, at 700 DEG C
3h is roasted, obtains 86g carriers;Hydrochloric acid will be slowly added in filtrate 1, be adjusted to acid, be warming up to 60 DEG C, add in the 300g of 200 mesh
Activated carbon carries out activated carbon adsorption, and complexing agent 8-hydroxy-quinoline is added in during activated carbon adsorption；Adsorb 2 it is small when after, adopt solution with ammonia
It inhales, is configured to the ammonium molybdate solution that concentration is 0.55g/ml；Filter residue 1 is added in into salpeter solution until being completely dissolved, using ammonium hydroxide
PH value is slowly adjusted to 6.5, is filtered, nickel nitrate solution concentration is then adjusted to 0.11g/mL；By nickel nitrate solution
It is mixed, is immersed on 80g carriers with ammonium molybdate solution, dry, 98g catalyst E are made in 470 DEG C of roasting 3h,
Comparative example 1
Using industrial oxidation alumina supporter carry out catalyst preparation, molybdenum nickel ammonia solution prepare using ammonium molybdate, nickel nitrate and ammonium hydroxide into
Row is prepared, and is sprayed according to water absorption rate for 1.0 progress catalyst, catalyst F is made in 470 DEG C of roasting 3h
Comparative example 2
De-oiling is stripped to molybdenum nickel catalyst after the industrial operation of embodiment 1, catalyst G is made in dry, roasting.
The catalyst prepared by embodiment 1 to 5 and comparative example 1,2 is carried out on 200ml fixed bed hydrogenation experimental rigs
Evaluation, reaction pressure are 15.7 MPa, and reaction temperature is 380 DEG C, and hydrogen to oil volume ratio is 800 (v), and raw material oil nature is shown in Table
1,500h result of the test is shown in Table 2.
Table 1
Table 2
| Catalyst | A | B | C | D | E | F | G |
| Demetallization per, % | 61 | 63 | 62 | 67 | 69 | 68 | 40 |
Claims (11)
- A kind of 1. spent catalyst recovery method, it is characterised in that：Including following content：（1）Molybdenum nickel system dead catalyst is stripped, is dried, microwave treatment, crushing；（2）Catalyst after crushing with alkali is mixed, then carries out high-temperature roasting；（3）Calcined catalyst is subjected to Hot water immersion, filtering, meta-aluminate filtrate and nickel oxide solid is made；（4）By step（3）Middle filtrate and aluminium salt acidity solution reaction filter, prepare boehmite, and boehmite is mixed It pinches, be molded, roasting obtained carrier；（5）By step（4）The solution filtered out carries out activated carbon adsorption molybdenum, is desorbed after absorption using ammonium hydroxide, and it is molten that ammonium molybdate is made Liquid；（6）To step（3）Solid adds in acid after middle filter, then removes Fe and Al in solution using alkaline solution adjustment pH value, dense Contraction obtains nickel salt solution；（7）By step（6）In nickel nitrate solution be added to step（5）Solution in, molybdenum nickel ammonia solution is made；（8）Utilize step（4）Middle carrier and step（7）Middle solution is impregnated, dried, roasted, and catalyst is made.
- 2. according to the method described in claim 1, it is characterized in that：Step（1）Described in the molybdenum nickel system hydrogenation catalyst that gives up press Weight content meter contains catalyst solid 70 ~ 90%, petroleum distillate 10 ~ 30%, and the weight of nickel oxide contains in the catalyst after extracting It measures as 3-10%, the weight content of molybdenum oxide is 10-25%.
- 3. according to the method described in claim 1, it is characterized in that：Step（1）Described in extract the organic solvent used as first One or more of benzene, petroleum ether, ethyl alcohol, extraction temperature are 80 ~ 110 DEG C.
- 4. according to the method described in claim 1, it is characterized in that：Step（1）Described in microwave treatment microwave frequency for 915 ~ 2450 MHz, processing time are 3 ~ 8h.
- 5. according to the method described in claim 1, it is characterized in that：Step（1）Described in microwave treatment in gaseous methanol and nitrogen It is carried out under the mixed atmosphere of gas, the volume ratio of gaseous methanol and nitrogen is 1:3-1:5.
- 6. according to the method described in claim 1, it is characterized in that：Step（2）Described in alkali for sodium hydroxide, sodium carbonate, hydrogen One or more of potassium oxide, alkali and contained Al in dead catalyst2O3Molar ratio be 4 ~ 1；The high-temperature roasting temperature is 700 ~ 1000 DEG C, 2 ~ 6h of roasting time.
- 7. according to the method described in claim 1, it is characterized in that：Step（3）Described in hot water temperature be 85 ~ 110 DEG C, liquid Gu volume ratio is 7 ~ 3, dip time is 0.2 ~ 2h.
- 8. according to the method described in claim 1, it is characterized in that：Step（4）Described in acid solution for aluminium chloride, nitric acid Aluminium or aluminum sulfate, the pH of acid solution is 1 ~ 3, step（3）Middle filtrate and acid solution reaction controlling pH value 7 ~ 9, reaction temperature Degree control is 50 ~ 80 DEG C, and the carrier calcination temperature is 500 ~ 1000 DEG C.
- 9. according to the method described in claim 1, it is characterized in that：Step（5）Middle granularity of activated carbon is 20 ~ 200 mesh；It adsorbed Journey adds in complexing agent.
- 10. according to the method described in claim 1, it is characterized in that：Step（6）Described in acid for sulfuric acid, the alkalescence Solution is sodium hydroxide solution, and sodium hydroxide solution mass concentration is 2 ~ 15%, and adjustment pH value is 5 ~ 6.5.
- 11. according to the method described in claim 1, it is characterized in that：Step（8）Described in drying temperature be 100 ~ 180 DEG C, Drying time is 2 ~ 5h, and calcination temperature is 400 ~ 600 DEG C, and roasting time is 2 ~ 4h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611011393.1A CN108067244B (en) | 2016-11-17 | 2016-11-17 | Method for recycling waste catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611011393.1A CN108067244B (en) | 2016-11-17 | 2016-11-17 | Method for recycling waste catalyst |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108067244A true CN108067244A (en) | 2018-05-25 |
| CN108067244B CN108067244B (en) | 2020-06-09 |
Family
ID=62163218
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611011393.1A Active CN108067244B (en) | 2016-11-17 | 2016-11-17 | Method for recycling waste catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108067244B (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108751241A (en) * | 2018-07-31 | 2018-11-06 | 菏泽华立新材料有限公司 | A kind of alkali treatment method and its processing unit of aluminium isopropoxide dead catalyst |
| CN108893594A (en) * | 2018-06-12 | 2018-11-27 | 昆明冶金高等专科学校 | A kind of method of carbon distribution and sulphur in quick abjection failure platinum-rhenium catalyst |
| CN111821992A (en) * | 2019-04-18 | 2020-10-27 | 中国石油化工股份有限公司 | Preparation method of high-activity hydrodemetallization catalyst |
| CN112619658A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Method for recycling waste hydrogenation catalyst |
| CN112645372A (en) * | 2021-01-19 | 2021-04-13 | 广西化工研究院有限公司 | Method for recycling waste activated alumina regenerant for hydrogen peroxide |
| CN113564386A (en) * | 2021-07-23 | 2021-10-29 | 中国科学院过程工程研究所 | Method for recovering molybdenum from waste nickel-molybdenum catalyst |
| CN113694932A (en) * | 2020-05-22 | 2021-11-26 | 中国石油化工股份有限公司 | Residual oil hydrotreating catalyst and preparation method and recycling thereof |
| CN113789446A (en) * | 2021-08-23 | 2021-12-14 | 常州大学 | Method for recovering molybdenum, vanadium and nickel metals from waste catalyst |
| CN114427029A (en) * | 2020-10-29 | 2022-05-03 | 中国石油化工股份有限公司 | Heavy oil treatment method for realizing metal separation and recovery |
| CN115957770A (en) * | 2021-10-08 | 2023-04-14 | 中国石油化工股份有限公司 | Preparation method of boiling bed residual oil hydrogenation catalyst |
| CN117324046A (en) * | 2023-09-25 | 2024-01-02 | 青岛金牛油脂科技有限公司 | Regeneration method of nickel catalyst for grease hydrogenation |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041388A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Method for recycling metal from waste catalyst containing molybdenum and nickel |
-
2016
- 2016-11-17 CN CN201611011393.1A patent/CN108067244B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102041388A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Method for recycling metal from waste catalyst containing molybdenum and nickel |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108893594A (en) * | 2018-06-12 | 2018-11-27 | 昆明冶金高等专科学校 | A kind of method of carbon distribution and sulphur in quick abjection failure platinum-rhenium catalyst |
| CN108751241A (en) * | 2018-07-31 | 2018-11-06 | 菏泽华立新材料有限公司 | A kind of alkali treatment method and its processing unit of aluminium isopropoxide dead catalyst |
| CN111821992B (en) * | 2019-04-18 | 2022-08-12 | 中国石油化工股份有限公司 | Preparation method of high-activity hydrodemetallization catalyst |
| CN111821992A (en) * | 2019-04-18 | 2020-10-27 | 中国石油化工股份有限公司 | Preparation method of high-activity hydrodemetallization catalyst |
| CN112619658A (en) * | 2019-09-24 | 2021-04-09 | 中国石油化工股份有限公司 | Method for recycling waste hydrogenation catalyst |
| CN113694932A (en) * | 2020-05-22 | 2021-11-26 | 中国石油化工股份有限公司 | Residual oil hydrotreating catalyst and preparation method and recycling thereof |
| CN113694932B (en) * | 2020-05-22 | 2024-01-09 | 中国石油化工股份有限公司 | Residual oil hydrotreating catalyst, preparation method and recycling thereof |
| CN114427029A (en) * | 2020-10-29 | 2022-05-03 | 中国石油化工股份有限公司 | Heavy oil treatment method for realizing metal separation and recovery |
| CN112645372A (en) * | 2021-01-19 | 2021-04-13 | 广西化工研究院有限公司 | Method for recycling waste activated alumina regenerant for hydrogen peroxide |
| CN112645372B (en) * | 2021-01-19 | 2023-05-05 | 广西化工研究院有限公司 | Method for recycling waste activated alumina regenerant for hydrogen peroxide |
| CN113564386A (en) * | 2021-07-23 | 2021-10-29 | 中国科学院过程工程研究所 | Method for recovering molybdenum from waste nickel-molybdenum catalyst |
| CN113789446A (en) * | 2021-08-23 | 2021-12-14 | 常州大学 | Method for recovering molybdenum, vanadium and nickel metals from waste catalyst |
| CN115957770A (en) * | 2021-10-08 | 2023-04-14 | 中国石油化工股份有限公司 | Preparation method of boiling bed residual oil hydrogenation catalyst |
| CN117324046A (en) * | 2023-09-25 | 2024-01-02 | 青岛金牛油脂科技有限公司 | Regeneration method of nickel catalyst for grease hydrogenation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108067244B (en) | 2020-06-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108067244A (en) | A kind of spent catalyst recovery method | |
| CN108067245B (en) | Recycling method of hydrotreating catalyst | |
| CN106669847B (en) | A kind of preparation method of alumina support | |
| CN102051483B (en) | Method for reclaiming metals from molybdenum-containing waste catalyst | |
| CN102041388B (en) | Method for recycling metal from waste catalyst containing molybdenum and nickel | |
| TWI465579B (en) | Method for recycling metal in waste catalyst comprised of aluminum | |
| US9926259B1 (en) | Catalyst for fixed bed aniline rectification residue recycling and preparation method | |
| CN111100987B (en) | Recovery method of waste catalyst metal component in tail oil | |
| CN111575478B (en) | Method for separating metal in heavy oil | |
| CN105709853B (en) | A method of recycling the hydrogenation catalyst that gives up | |
| JPS5980737A (en) | Recovery of metals from waste hydrogenation catalyst | |
| CN102050492A (en) | Method for recovering metal from molybdenum-containing spent catalyst | |
| CN112646977A (en) | Method for recovering vanadium, molybdenum, nickel and aluminum from petroleum refining waste catalyst | |
| CN109837393A (en) | A kind of selective recovery is given up the method for valuable metal in hydrogenation catalyst | |
| CN111573733A (en) | Method for recycling waste catalyst | |
| CN108067272A (en) | A kind of hydrogenation catalyst preparation method | |
| CN106669846B (en) | A kind of preparation method of catalyst for demetalation carrier | |
| CN109395770B (en) | Iron-based hydrogenation catalyst and preparation method thereof | |
| CN108067213A (en) | It is a kind of for catalyst of aniline rectification residue recycling and preparation method thereof | |
| CN101435027B (en) | Method for recycling high purity molybdenum from molybdenum-containing spent catalyst | |
| CN101724758A (en) | Method for recycling molybdenum of molybdenum-contained waste catalyst | |
| CN104549491B (en) | Method for recycling completely inactivated hydrocracking catalyst | |
| CN104549492A (en) | Method for totally recycling and reusing waste hydrocracking catalyst | |
| CN102259000A (en) | Recycling method for dead catalyst containing nickel | |
| CN105727979B (en) | A kind of method for preparing catalyst for preparing propene by oxidative dehydrogenation of propane |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |