GB1567140A - Process for extracting vanadium from deactivated catalysts - Google Patents
Process for extracting vanadium from deactivated catalysts Download PDFInfo
- Publication number
- GB1567140A GB1567140A GB11405/78A GB1140578A GB1567140A GB 1567140 A GB1567140 A GB 1567140A GB 11405/78 A GB11405/78 A GB 11405/78A GB 1140578 A GB1140578 A GB 1140578A GB 1567140 A GB1567140 A GB 1567140A
- Authority
- GB
- United Kingdom
- Prior art keywords
- catalyst
- vanadium
- steam
- deactivated
- treatment
- 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.)
- Expired
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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
-
- 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/005—Preliminary treatment of ores, e.g. by roasting or by the Krupp-Renn process
-
- 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
- C22B34/00—Obtaining refractory metals
- C22B34/20—Obtaining niobium, tantalum or vanadium
- C22B34/22—Obtaining vanadium
-
- 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
- C22B34/00—Obtaining refractory metals
- C22B34/20—Obtaining niobium, tantalum or vanadium
- C22B34/22—Obtaining vanadium
- C22B34/225—Obtaining vanadium from spent catalysts
-
- 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
Description
(54) IMPROVED PROCESS FOR EXTRACTING
VANADIUM FROM DEACTIVATED CATALYSTS
(71) We, SHELL INTERNATIONALB RE- SEARCH MAATSCHAPPIJ B.V., a company organised under the laws of The Netherlands, of 30 Carel van Bylandtlaan. The Hague,
The Netherlands, do hereby declare the invention, for which we pray that a patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement::- Patent 1,526,927 to which the present application is an addition, relates to a process for extracting vanadium from a catalyst which has been deactivated by use in the treatment of a hydrocarbon oil containing vanadium with hydrogen at elevated temperature and pressure, during which treatment the vanadium content of the catalyst has increased by at least 10 pbw. According to the said patent 1,526,927 the extraction of the vanadium, whereby the vanadium content of the catalyst is decreased by at least 40% of the amount by which it has risen during the deactivation, is carried out by extracting the deactivated catalyst with an aqueous solution of a mineral acid, after which vanadium is separated from the vanadium-containing solution thus obtained.
If the process is applied to a catalyst that has been deactivated in the hydrotreatment of a hydrocarbon oil containing nickel in addition to vanadium, during which treatment the nickel content of the catalyst has increased as well, nickel is also removed from the catalyst in the process. Besides the extraction of vanadium and optionally nickel from deactivated catalysts, the process is also applicable to the regeneration of deactivated catalysts so that they can be used again for catalytic purposes.
According to the said patent 1,526,927 the acid extraction is preferably carried out in the presence of a reducing agent Also, according to the said patent 1,526,927 it is preferred to treat the deactivated catalyst first with steam to remove sulphur and then with an oxygen-containing gas to remove carbon, prior to subjecting it to acid extraction. It should be remarked that, when the aim is not only to extract vanadium and optionally nickel from the catalyst, but also to regenerate the catalyst, the treatment of the deactivated catalyst with an oxygencontaining gas in the way indicated in the examples of the said patent 1,526,927 whereby a small portion of the deactivated catalyst is treated with air for three hours at 550ÇC, is not suitable for larger quantities of deactivated catalyst because of the large amount of heat that would be liberated.
When larger quantities of deactivated catalyst had to be treated with a view to extracting vanadium and optionally nickel from the catalyst as well as regenerating the catalyst, the following three-stage procedure was until recently considered to be the most attractive embodiment of the process according to the said patent 1,526,927.The deactivated catalyst is first treated for 1-5 hours at 250-450"C and atmospheric pressure with a mixture of steam and nitrogen, then for 1-5 days at 350-600 C and atmospheric pressure with a mixture of air and nitrogen and finally it is subjected to acid extraction in the presence of a reducing agent for 0.5-3 hours at 50-150"C. The treatment times required in the various stages are dependent upon, inter alia, the quantities of sulphur, carbon and metals which are present on the deactivated catalyst and the conditions chosen, viz. treatment temperatures, gas flow rates and compositions of treating gases and extraction liquid.Up to now the long treatment time required in the second stage of the three-stage procedure has been considered a serious drawback for using the process according to the said patent 1,526,927 on a commercial scale.
Continued investigation of the process as described in the said patent 1,526,927 has now led to the finding that a comparable result can be obtained as regards vanadium and nickel removal and activity of the regenerated catalyst to that achieved by conducting the process according to the threestage procedure described hereinbefore, but in a much shorter time, if the acid agent tion in the presence of a reducing agent is preceded by treatment of the deactivated catalyst at a temperature above 2500C with a mixture of steam and air of which the steam/air ratio is more than 1.0 at a steam partial pressure above 1 bar.In addition to the fact that with the process now found a much shorter treatment time will suffice for achieving a comparable result as regards vanadium and nickel removal and activity of the regenerated catalyst, this process has two additional advantages over the above-mentioned three-stage procedure in that both the number of treatment stages and the number of gases necessary for treating the deactivated catalyst prior to the acid extraction have decreased by one.
The present patent application therefore relates to an improved process for extracting vanadium from a deactivated catalyst according to the patent 1,526,927 in which process vanadium is extracted from a catalyst which has been deactivated by use in the treatment of a vanadium-containing hydrocarbon oil with hydrogen at elevated temperature and pressure, during which treatment the vanadium content of the catalyst has increased by at least 10 pbw, and in which process the said vanadium extraction, whereby the vanadium content of the catalyst is reduced by at least 40% of the amount by which it has risen during the deactivation (vanadium content of the catalyst expressed in pbw vanadium/100 pbw catalyst carrier), is carried out by extracting the deactivated catalyst with an aqueous solution of a mineral acid (called hereinafter "acid extraction"), after which the vanadium is separated from the vandium-containing solution thus obtained.
The improvement consists in that the acid extraction which is carried out in the presence of a reducing agent, is preceded by a treatment of the deactivated catalyst at a temperature above 250"C with a mixture of steam and air in which the steam/air ratio is more than 1.0 at a steam partial pressure above 1 bar.
In the process according to the present invention the treatment with the mixture of steam and air is conducted at a temperature above 250"C, but preferably below 6000C and in particular at a temperature between 325 and 425"C. In the treatment of the deactivated catalyst with the mixture of steam and air the steam partial pressure is more than 1 bar, but preferably below 5 bar and in particular between 2 and 4 bar. The steam/air ratio of the steam/air mixture used is more than 1.0, but preferably lower than 10 and in particular between 4 and 8.
The acid extraction in the presence of a reducing agent to which the deactivated catalyst should be subjected in the process according to the invention, is preferably carried out at elevated temperature, in particular at a temperature above 50"C. The said extraction is preferably conducted with an aqueous solution of sulphuric acid which has been saturated with sulphur dioxide.
When the process according to the invention is applied to deactivated catalysts which contain nickel in addition to vanadium, it may be advisable to extract the deactivated catalyst with water after the treatment with the steam/air mixture. By this extraction with water, which is preferably carried out at elevated temperature and in particular at a temperature above 50"C, an aqueous nickel-containing solution is obtained from which the nickel can be extracted.
The process according to the present invention is particularly important in those cases in which the aim is not only to extract vanadium and optionally nickel from the deactivated catalyst, but also to regenerate the catalyst (which may, in the fresh condition, contain one or more metals with hydrogenation activity) so that it can be used again for catalytic purposes. The present patent application relates therefore not only to a process for extracting vanadium and optionally nickel from a deactivated catalyst, but also to a process in which this extraction is conducted in such a way that a regenerated catalyst is obtained which can be used again for catalytic purposes, either as such, or after a complementary quantity of metals with hydrogenation activity has been added to it.The process according to the invention is especially important for extracting vanadium and optionally nickel from a catalyst substantially consisting of silica, in combination with regeneration of the catalyst, which catalyst has been used in a process for the hydrodemetallization of a hydrocarbon oil.
Applicants copending application 11404/78 (Serial No. 1 567 139) also relates to an improved process for extracting vanadium from deactivated catalysts.
The invention will now be explained with reference to the following examples.
EXAMPLE I
A catalyst comprising 0.5 pbw nickel and 2.0 pbw vanadium per 100 pbw silica carrier was prepared by impregnating a silica carrier with an aqueous solution of nickel nitrate and vanadium oxalate, after which the composition was dried and calcined. (catalyst A) was used in the sulphidic form for the hydrodemetallization of a hydrocarbon oil (oil A) with a total vanadium and nickel content of 62 ppmw, a
Cs-asphaltenes content of 6.4 %w and a sulphur content of 3.9 %w, which oil had been obtained as the residue in the atmospheric distillation of a crude oil from the
Middle East.The hydrodemetallization was carried out by passing the oil together with hydrogen in a downward direction through a cylindrical, vertically disposed fixed catalyst bed at a temperature of 420"C, a total pressure of 150 bar, a space velocity of 5 kg.l-'.h-' and a gas flow rate (measured at the reactor outlet) of 250 N1 H2.kg1. The activity of the catalyst, expressed as "% vanadium removed" (= average vanadium removal over the period of catalyst age from 1 tonne oil/kg catalyst to 4 tonnes oil/kg catalyst), was 51. After the catalyst had been deactivated in this process, It was extracted with toluene to remove remnants of residual. oil and after evaporation of the toluene from the catalyst the latter was analysed.The deactivated catalyst (catalyst B) contained 9.7 pbw carbon, 20.6 pbw sulphur, 4.1 pbw nickel and 24.3 pbw vanadium per 100 pbw silica.
EXAMPLE II
5 kg of Catalyst B was treated with a 4:1 steam/nitrogen mixture for three hours at 350"C, atmospheric pressure and a gas flow rate of 2 N1 gas mixture. (g catalyst)-1.h--1.
The catalyst was then treated with a 1:9 air/ nitrogen mixture for 50 hours at 400 C, atmospheric pressure and a gas flow rate of
I N1 gas mixture (g catalyst)-l.h-l. Finally, the catalyst was extracted for two hours at 90"C with stirring with 40 1 2 N sulphuric acid which had been saturated with sulphur dioxide. After the extracted catalyst had been washed with water, it was dried at 120"C and calcined for three hours at 550"C.
On analysis of the catalyst thus obtained (catalyst C), 96% of the vanadium and 95% of the nickel were found to have been removed from the catalyst by this treatment.
EXAMPLE 111
5 kg of Catalyst B was treated with a 7:1 steam/air mixture for 25 hours at 400"C, a steam partial pressure of 3.5 bar and a gas rate of 0.6 N1 gas mixture. (g catalyst)-1.h-1. The catalyst was then extracted for two hours at 90"C with stirring with 40 1 2 N sulphuric acid which had been saturated with sulphur dioxide. After the extracted catalyst had been washed with water, it was dried at 120"C and calcined for three hours at 5500 C. On analysis of the catalyst thus obtained (catalyst D), 96% of the vanadium and 95% of the nickel were found to have been removed from the catalyst by this treatment.
EXAMPLE IV
5 kg of Catalyst B was treated with a 5:1
steam/air mixture for 20 hours at 3500 C, a steam partial pressure of 3.0 bar and a gas flow rate of 0.6 N1 gas mixture. (g catalyst)-l.h--l. The catalyst was then subjected to acid extraction in the same way as described in Example III. On analysis of the catalyst thus obtained (catalyst E), 94% of the vanadium and 92% of the nickel were found to have been removed from the catalyst by this treatment.
EXAMPLE V
5 kg of Catalyst B was treated with a 1:2 steam/air mixture for 20 hours at 4000 C, a steam partial pressure of 0.6 bar and a gas flow rate of 0.4 N1 gas mixture. ig catalyst)-l.h-l, The catalyst was then subjected to acid extraction in the same way as described in Example III. On analysis of the catalyst thus obtained (catalyst F), 95% of the vanadium and 95% of the nickel were found to have been removed from the catalyst by this treatment.
EXAMPLE Vl 5 kg of Catalyst B was treated with a 2:1 steam/air mixture for 25 hours at 1500C, a steam partial pressure of 1.5 bar and a gas flow rate of 2 N1 gas mixture. (g catalyst)-l.h-'. The catalyst was then subjected to acid extraction in the same way as described in Example III. On analysis of the catalyst thus obtained (catalyst G), 40 Ó of the vanadium and 45% of the nickel were found to have been removed from the catalyst by this treatment.
EXAMPLE VH Catalysts containing 0.5 pbw nickel and 2.0 pbw vanadium per 100 pbw silica carrier were prepared by impregnating catalysts C and F with an aqueous solution of nickel nitrate and vanadyl oxalate, after which the compositions were dried and calcined. Cata
lysts C' and F' thus obtained were used
in the sulphidic form for the hydrodemetal
lization of oil A under the same conditions
as the hydrodemetallization of this oil by
catalyst A described in Example I. The acti
vities of catalysts C and F', expressed as
"percentage vanadium removed", were 48
and 10, respectively.
EXAMPLE VIII In the same way as described in Example
VII, catalysts D' and E' were prepared from
catalysts D and E and usec for the hydrode
metallization of oil A. The activities of
catalysts D and El, expressed as "percentage
vanadium removed", were 50 and 49, res
pectively.
Of the examples I-VIII, Nos. III, IV and
VIII are examples according to the present invention. The other examples have been included for comparison.
Example I relates to a hydrodemetallization in which a fresh catalyst A deactivates to the deactivated catalyst B.
Example II relates to the three-stage procedure described hereinbefore in which a regenerated catalyst C is prepared from the deactivated catalyst B and in which it takes 53 hours in all to carry out the first two stages.
Examples III and IV relate to the improved process according to the invention in which regenerated catalysts D and E are prepared from the deactivated catalyst B.
Comparison of examples II, III and IV shows that the process according to the invention leads to the same excellent metal removal as the three-stage procedure. However, the treatment with the steam/air mixture, which has replaced the first and the second stage of the three-stage procedure, takes only 20-25 hours.
Examples V and VI relate to the treatment of the deactivated catalyst with a mixture of steam and air followed by acid extraction, in which "regenerated" catalysts F and G are prepared from deactivated catalyst B.
During the treatment with the steam/air mixture, the steam partial pressure and the steam/air ratio employed were too low in
Example V and the temperature was too low in Example VI. This resulted in an insufficient metal removal for catalyst G (and consequently in a low activity!) and, as is seen from Example VII, in a low activity for catalyst F.
From Examples VII and VIII it is seen that catalysts which have been regenerated according to the present invention (catalysts
D' and E') show the same high activity as a catalyst which has been regenerated according to the three-stage procedure (catalyst Cry).
WHAT WE CLAIM IS:
1. An improved process for extracting vanadium from a deactivating catalyst according to patent 1,526,927 in which process vanadium is extracted from a catalyst which has been deactivated by use in the treatment of a vanadium-containing hydrocarbon oil with hydrogen at elevated temperature and pressure, during which treatment the vanadium content of the catalyst has increased by at least 10 pbw, and in which process the said vanadium extraction, whereby the vanadium content of the catalyst is reduced by at least 40% of the amount by which it has risen during the deactivation (vanadium content of the catalyst expressed in pbw vanadium/100 pbw catalyst), is carried out by extracting the deactivated catalyst with an aqueous solution of a mineral acid (called hereinafter "acid extraction"), after which the vanadium is separated from the vanadium-containing solution thus obtained wherein the improvement consists in that the acid extraction which is carried out in the presence of a reducing agent, is preceded by a treatment of the deactivated catalyst at a temperature above 250"C with a mixture of steam and air in which the steam/air ratio is more than 1.0 at a steam partial pressure above 1 bar.
2. A process according to claim 1, characterized in that the treatment of the deactivated catalyst with a mixture of steam and air is conducted at a temperature below 600 C.
3. A process according to claim 2, characterized in that the said temperature is between 325 and 425"C.
4. A process according to any one of claims 1-3, characterized in that the treatment of the deactivated catalyst with a mixture of steam and air is conducted at a steam partial pressure below 5 bar.
5. A process according to claim 4, characterized in that the said pressure is between 2 and 4 bar.
6. A process according to any one of claims 1-5, characterized in that the treatment of the deactivated catalyst with a mixture of steam and air is conducted with a gas mixture in which the steam/air ratio is lower than 10.
7. A process according to claim 6, characterized in that the said ratio is between 4 and 8.
8. A process according to any one of claims 1-7, characterized in that the acid extraction in the presence of a reducing agent is carried out at a temperature above 500 C, 9. A process according to any one of claims 1-8, characterized in that the acid extraction in the presence of a reducing agent is carried out with an aqueous solution of sulphuric acid which has been saturated with sulphur dioxide.
10. A process according to any one of claims 1-9, characterized in that nickel is removed from the deactivated catalyst by extraction with water at a temperature above 50"C, after the deactivated catalyst has been treated with the steam/air mixture.
11. A process according to any one of claims 1-10, characterized in that it is applied to a catalyst substantially consisting of silica, which catalyst has been used in a process for the hydrodemetallization of a hydrocarbon oil.
12. A process for extracting vanadium and optionally nickel from a deactivated catalyst, whether or not with regeneration of the catalyst, substantially as described hereinbefore and in particular with reference to
Examples III, IV and VIII.
**WARNING** end of DESC field may overlap start of CLMS **.
Claims (15)
1. An improved process for extracting vanadium from a deactivating catalyst according to patent 1,526,927 in which process vanadium is extracted from a catalyst which has been deactivated by use in the treatment of a vanadium-containing hydrocarbon oil with hydrogen at elevated temperature and pressure, during which treatment the vanadium content of the catalyst has increased by at least 10 pbw, and in which process the said vanadium extraction, whereby the vanadium content of the catalyst is reduced by at least 40% of the amount by which it has risen during the deactivation (vanadium content of the catalyst expressed in pbw vanadium/100 pbw catalyst), is carried out by extracting the deactivated catalyst with an aqueous solution of a mineral acid (called hereinafter "acid extraction"), after which the vanadium is separated from the vanadium-containing solution thus obtained wherein the improvement consists in that the acid extraction which is carried out in the presence of a reducing agent, is preceded by a treatment of the deactivated catalyst at a temperature above 250"C with a mixture of steam and air in which the steam/air ratio is more than 1.0 at a steam partial pressure above 1 bar.
2. A process according to claim 1, characterized in that the treatment of the deactivated catalyst with a mixture of steam and air is conducted at a temperature below 600 C.
3. A process according to claim 2, characterized in that the said temperature is between 325 and 425"C.
4. A process according to any one of claims 1-3, characterized in that the treatment of the deactivated catalyst with a mixture of steam and air is conducted at a steam partial pressure below 5 bar.
5. A process according to claim 4, characterized in that the said pressure is between 2 and 4 bar.
6. A process according to any one of claims 1-5, characterized in that the treatment of the deactivated catalyst with a mixture of steam and air is conducted with a gas mixture in which the steam/air ratio is lower than 10.
7. A process according to claim 6, characterized in that the said ratio is between 4 and 8.
8. A process according to any one of claims 1-7, characterized in that the acid extraction in the presence of a reducing agent is carried out at a temperature above 500 C,
9. A process according to any one of claims 1-8, characterized in that the acid extraction in the presence of a reducing agent is carried out with an aqueous solution of sulphuric acid which has been saturated with sulphur dioxide.
10. A process according to any one of claims 1-9, characterized in that nickel is removed from the deactivated catalyst by extraction with water at a temperature above 50"C, after the deactivated catalyst has been treated with the steam/air mixture.
11. A process according to any one of claims 1-10, characterized in that it is applied to a catalyst substantially consisting of silica, which catalyst has been used in a process for the hydrodemetallization of a hydrocarbon oil.
12. A process for extracting vanadium and optionally nickel from a deactivated catalyst, whether or not with regeneration of the catalyst, substantially as described hereinbefore and in particular with reference to
Examples III, IV and VIII.
13. Vanadium and optionally nickel ex
tracted from a deactivated catalyst according to a process as described in claim 12.
14. Catalysts that have been regenerated according to a process as described in claim
12.
15. Catalc processes in which a catalyst
according to claim 14 is used.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL7703181A NL7703181A (en) | 1977-03-24 | 1977-03-24 | IMPROVED METHOD FOR RECOVERING VANADIUM FROM DEACTIVATED CATALYSTS. |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| GB1567140A true GB1567140A (en) | 1980-05-14 |
Family
ID=19828224
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB11405/78A Expired GB1567140A (en) | 1977-03-24 | 1978-03-22 | Process for extracting vanadium from deactivated catalysts |
Country Status (14)
| Country | Link |
|---|---|
| JP (1) | JPS53119209A (en) |
| AU (1) | AU516502B2 (en) |
| BE (1) | BE864852R (en) |
| CA (1) | CA1116582A (en) |
| DE (1) | DE2812597A1 (en) |
| FR (1) | FR2384854A2 (en) |
| GB (1) | GB1567140A (en) |
| IT (1) | IT1093669B (en) |
| MX (1) | MX147986A (en) |
| NL (1) | NL7703181A (en) |
| NO (1) | NO152939C (en) |
| SE (1) | SE444581B (en) |
| SU (1) | SU688108A3 (en) |
| ZA (1) | ZA781661B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0034853A1 (en) * | 1980-02-20 | 1981-09-02 | Shell Internationale Researchmaatschappij B.V. | Process for the removal of vanadium-containing acid from an acid-extracted deactivated demetallization catalyst |
| US5437849A (en) * | 1992-05-21 | 1995-08-01 | Metallgesellschaft Aktiengesellschaft | Method of processing vanadium-containing residues |
| WO1997023289A1 (en) * | 1995-12-22 | 1997-07-03 | Commonwealth Scientific And Industrial Research Organisation | Oxidation catalyst system |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2985647B2 (en) * | 1993-02-26 | 1999-12-06 | 住友金属鉱山株式会社 | Dissolution method of spent catalyst |
| JP2751093B2 (en) * | 1994-03-11 | 1998-05-18 | 住友金属鉱山株式会社 | Method for recovering valuable metals from spent catalyst |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1272899B (en) * | 1964-05-22 | 1968-07-18 | Inst Njeftjechimitscheskogo Si | Process for the regeneration of coked oxidic hydrogenation catalysts |
| FR1602405A (en) * | 1968-06-11 | 1970-11-23 | ||
| FR1603515A (en) * | 1968-11-05 | 1971-05-03 | Regeneration of catalysts used in the hydro-treatment - of sulphurous hydrocarbon charges containing metallic | |
| JPS5144114A (en) * | 1974-06-01 | 1976-04-15 | Kawasaki Heavy Ind Ltd | TAISUISEISETSUKOBUROTSUKU MATAHA PANERUNOSEIZOHOHO |
| JPS51121A (en) * | 1974-06-20 | 1976-01-05 | Fujimori Sangyo | CHUKUSURA BUKOZOTAI |
| GB1526927A (en) * | 1974-10-15 | 1978-10-04 | Shell Int Research | Process for recovering vanadium from deactivated catalyst |
-
1977
- 1977-03-24 NL NL7703181A patent/NL7703181A/en not_active Application Discontinuation
-
1978
- 1978-02-09 CA CA000296567A patent/CA1116582A/en not_active Expired
- 1978-03-14 BE BE1008766A patent/BE864852R/en not_active IP Right Cessation
- 1978-03-17 MX MX17281478A patent/MX147986A/en unknown
- 1978-03-22 FR FR7808313A patent/FR2384854A2/en active Granted
- 1978-03-22 IT IT2145378A patent/IT1093669B/en active
- 1978-03-22 ZA ZA00781661A patent/ZA781661B/en unknown
- 1978-03-22 AU AU34435/78A patent/AU516502B2/en not_active Expired
- 1978-03-22 GB GB11405/78A patent/GB1567140A/en not_active Expired
- 1978-03-22 DE DE19782812597 patent/DE2812597A1/en not_active Withdrawn
- 1978-03-22 JP JP3179278A patent/JPS53119209A/en active Granted
- 1978-03-22 SU SU782591397A patent/SU688108A3/en active
- 1978-03-22 SE SE7803322A patent/SE444581B/en not_active IP Right Cessation
- 1978-03-22 NO NO781027A patent/NO152939C/en unknown
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0034853A1 (en) * | 1980-02-20 | 1981-09-02 | Shell Internationale Researchmaatschappij B.V. | Process for the removal of vanadium-containing acid from an acid-extracted deactivated demetallization catalyst |
| US5437849A (en) * | 1992-05-21 | 1995-08-01 | Metallgesellschaft Aktiengesellschaft | Method of processing vanadium-containing residues |
| WO1997023289A1 (en) * | 1995-12-22 | 1997-07-03 | Commonwealth Scientific And Industrial Research Organisation | Oxidation catalyst system |
Also Published As
| Publication number | Publication date |
|---|---|
| NO781027L (en) | 1978-09-26 |
| SE444581B (en) | 1986-04-21 |
| DE2812597A1 (en) | 1978-09-28 |
| ZA781661B (en) | 1979-03-28 |
| BE864852R (en) | 1978-09-14 |
| FR2384854B2 (en) | 1980-10-24 |
| FR2384854A2 (en) | 1978-10-20 |
| NO152939C (en) | 1985-12-18 |
| SU688108A3 (en) | 1979-09-25 |
| NO152939B (en) | 1985-09-09 |
| IT1093669B (en) | 1985-07-26 |
| JPS53119209A (en) | 1978-10-18 |
| MX147986A (en) | 1983-02-22 |
| AU3443578A (en) | 1979-09-27 |
| NL7703181A (en) | 1978-09-26 |
| CA1116582A (en) | 1982-01-19 |
| IT7821453A0 (en) | 1978-03-22 |
| JPS637819B2 (en) | 1988-02-18 |
| SE7803322L (en) | 1978-09-25 |
| AU516502B2 (en) | 1981-06-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0437608B1 (en) | Process for decomposing ammonia | |
| US5728918A (en) | Catalyst treatment | |
| US4359379A (en) | Process for fluid catalytic cracking of distillation residual oils | |
| US4795726A (en) | Method for the regeneration of spent alumina-based catalysts | |
| US3114701A (en) | Catalytic hydrodenitrification process | |
| US2627527A (en) | Oxidation of olefins to alkenals | |
| JPS6012908B2 (en) | How to regenerate a deactivated catalyst | |
| US2573726A (en) | Catalytic desulphurisation of naphthas | |
| US2687381A (en) | Method of preparing a cobalt, molybdenum impregnated catalyst composite | |
| GB1567140A (en) | Process for extracting vanadium from deactivated catalysts | |
| US3456029A (en) | Process for the purification of lower olefin gases | |
| US2728710A (en) | Process for hydrodesulfurizing hydrocarbons | |
| CA1048952A (en) | Desulphurisation catalysts and their use | |
| US1904218A (en) | Process for restoring the activity of hydrogenation catalysts | |
| US1819055A (en) | Desulphurization of gases and vapors | |
| US2939883A (en) | Dehydrogenation of alcohols to | |
| US3460913A (en) | Regeneration of sulfur contaminated catalysts | |
| DE1901171B2 (en) | METHOD OF REMOVING SULFUR DIOXIDE FROM EXHAUST GASES, IN PARTICULAR SMOKE GASES | |
| CA1313651C (en) | Regeneration of an iron based natural catalyst used in the hydroconversion of heavy crudes and residues | |
| GB1567139A (en) | Process for extracting vanadium from deactivated catalysts | |
| EP0034853B1 (en) | Process for the removal of vanadium-containing acid from an acid-extracted deactivated demetallization catalyst | |
| US4435522A (en) | Method of producing a catalyst for liquefaction of coal | |
| EP0236306A1 (en) | Removal of inorganic contaminants from catalysts | |
| US2970957A (en) | Removal of vanadium and/or sodium from petroleum hydrocarbons | |
| US3105812A (en) | Process of removing nitrogen compounds by oxidation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PS | Patent sealed [section 19, patents act 1949] |