CA1093831A - Uranium extraction - Google Patents
Uranium extractionInfo
- Publication number
- CA1093831A CA1093831A CA296,924A CA296924A CA1093831A CA 1093831 A CA1093831 A CA 1093831A CA 296924 A CA296924 A CA 296924A CA 1093831 A CA1093831 A CA 1093831A
- Authority
- CA
- Canada
- Prior art keywords
- uranium
- concentrate
- process according
- pyrite
- range
- 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
- 229910052770 Uranium Inorganic materials 0.000 title claims abstract description 29
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 238000000605 extraction Methods 0.000 title description 10
- 239000012141 concentrate Substances 0.000 claims abstract description 38
- 229910052683 pyrite Inorganic materials 0.000 claims abstract description 20
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000011028 pyrite Substances 0.000 claims abstract description 20
- 238000000034 method Methods 0.000 claims abstract description 17
- NKQAYALHJFYKDG-UHFFFAOYSA-H [U+6].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O Chemical compound [U+6].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O NKQAYALHJFYKDG-UHFFFAOYSA-H 0.000 claims abstract description 11
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000005864 Sulphur Substances 0.000 claims abstract description 9
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000001117 sulphuric acid Substances 0.000 claims abstract description 6
- 235000011149 sulphuric acid Nutrition 0.000 claims abstract description 6
- 235000008504 concentrate Nutrition 0.000 claims description 35
- 239000002253 acid Substances 0.000 claims description 5
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 description 3
- 235000011152 sodium sulphate Nutrition 0.000 description 3
- 229910021653 sulphate ion Inorganic materials 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000005188 flotation Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- -1 alkali metal salt Chemical class 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000010953 base metal Substances 0.000 description 1
- NFMAZVUSKIJEIH-UHFFFAOYSA-N bis(sulfanylidene)iron Chemical compound S=[Fe]=S NFMAZVUSKIJEIH-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 238000009852 extractive metallurgy Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000011819 refractory material Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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
- C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
- C22B60/02—Obtaining thorium, uranium, or other actinides
- C22B60/0204—Obtaining thorium, uranium, or other actinides obtaining uranium
- C22B60/0217—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes
- C22B60/0221—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes by leaching
- C22B60/0226—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes by leaching using acidic solutions or liquors
-
- 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
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Geology (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
ABSTRACT OF DISCLOSURE
A process for extracting uranium values from a pyrite concentrate containing at least 20% by weight sulphur and at least 50 grams per ton of uranium, calculated at U308, including the steps of roasting the concentrate at a temperature in the range 650 to 750°C to convert the uranium to uranium sulphate, and solubilising the uranium sulphate in the roasted concentrate by means of a sulphuric acid leach of pH not exceeding 3.
A process for extracting uranium values from a pyrite concentrate containing at least 20% by weight sulphur and at least 50 grams per ton of uranium, calculated at U308, including the steps of roasting the concentrate at a temperature in the range 650 to 750°C to convert the uranium to uranium sulphate, and solubilising the uranium sulphate in the roasted concentrate by means of a sulphuric acid leach of pH not exceeding 3.
Description
:l~93~3~ ;
T~IIS -invention re'lat'es to the extraction of uraniLIm values from pyrite (FeS2) concentrates.
Pyr-ite concentrates are obtained, for example, by flotation of pyrite ores. Such concentrates con-tain at least 20% by weight sulphur and often gold, uranium and base meta'ls'in addition to iron. Some pyrite concentrates contain . a relat;vely high uranium content, i.e. a uranium content . of at least 50 grams per ton~.calculated as U308. Thls-invention is concerned ~lith the extraction of uranium values from pyrite concentrates which contain at least 50 (Jrams per ton of uran;um~ calculatecl as U308, and more particu'larly with such concentrates which have a uranium content in the rarige 50 grams to 2000 grams per ton, again calculated as U308 .. ::
1~ According to the present invention, a pro'c'ess for extracting uranium values from a pyrite concentrate as deFined a~ove includes the steps of roasting the concentrate to convert the uranium to uranium sulphate, and solubilising uranium sulphate in the roasted concentrate by means of an acid leach oF pH not exceeding 3;
The first step in the process is the roasting of the pyrite concentrate. This roast converts the uranium values in the
T~IIS -invention re'lat'es to the extraction of uraniLIm values from pyrite (FeS2) concentrates.
Pyr-ite concentrates are obtained, for example, by flotation of pyrite ores. Such concentrates con-tain at least 20% by weight sulphur and often gold, uranium and base meta'ls'in addition to iron. Some pyrite concentrates contain . a relat;vely high uranium content, i.e. a uranium content . of at least 50 grams per ton~.calculated as U308. Thls-invention is concerned ~lith the extraction of uranium values from pyrite concentrates which contain at least 50 (Jrams per ton of uran;um~ calculatecl as U308, and more particu'larly with such concentrates which have a uranium content in the rarige 50 grams to 2000 grams per ton, again calculated as U308 .. ::
1~ According to the present invention, a pro'c'ess for extracting uranium values from a pyrite concentrate as deFined a~ove includes the steps of roasting the concentrate to convert the uranium to uranium sulphate, and solubilising uranium sulphate in the roasted concentrate by means of an acid leach oF pH not exceeding 3;
The first step in the process is the roasting of the pyrite concentrate. This roast converts the uranium values in the
2 - ~
... . .
..
~ V~3~33~
concentrate to uranium sulphate. The roast is preferably carried out at a temperature in the range of 650 to 750C
and more preferably in the range 650 to 700C. Roasting temperatures in excess of 750C are undesirable because refractories tend to forlll at these temperatures and this is disadvantageous.
The roast is preferably carried out in a standard fluidised bed roaster such as those illustrated in the article oF
R.B. Thompson and R. Roesner ''Fluid ~ed Roasting - Principles and Practice" in "Extractive Metallurgy of Copper, Nickel and Cobalt" by Paul Queneau, Interscience 1961.
The extraction of uranium values from the pyrite concentrate is improved by carrying out the roast in the presence of a suitable alkali metal salt such as sulphate or carbonate or alkali metal hydroxide. The preferred alkali metal is sodium and the preferred salt is the sulphate. Only small quantities of the salt or hydroxide are required to improve the extraction. The salt or hydroxide is typically used in an amol1nt of 1 to 10%, preferably 1 to 5%, by weight of the concentrate.
The residence time in the roaster ~ill Yary according to the nature of the concentrate and the degree of conversion of uranium to uranium sulphate required. In general, the longer the residence time~ ~he better the final extraction.
.. , . ;
~ 3~3 The uranium sulphate is ex-tracted frolll the roas~ed con~
centrate by means of an acid leach of pH no~ exceecling
... . .
..
~ V~3~33~
concentrate to uranium sulphate. The roast is preferably carried out at a temperature in the range of 650 to 750C
and more preferably in the range 650 to 700C. Roasting temperatures in excess of 750C are undesirable because refractories tend to forlll at these temperatures and this is disadvantageous.
The roast is preferably carried out in a standard fluidised bed roaster such as those illustrated in the article oF
R.B. Thompson and R. Roesner ''Fluid ~ed Roasting - Principles and Practice" in "Extractive Metallurgy of Copper, Nickel and Cobalt" by Paul Queneau, Interscience 1961.
The extraction of uranium values from the pyrite concentrate is improved by carrying out the roast in the presence of a suitable alkali metal salt such as sulphate or carbonate or alkali metal hydroxide. The preferred alkali metal is sodium and the preferred salt is the sulphate. Only small quantities of the salt or hydroxide are required to improve the extraction. The salt or hydroxide is typically used in an amol1nt of 1 to 10%, preferably 1 to 5%, by weight of the concentrate.
The residence time in the roaster ~ill Yary according to the nature of the concentrate and the degree of conversion of uranium to uranium sulphate required. In general, the longer the residence time~ ~he better the final extraction.
.. , . ;
~ 3~3 The uranium sulphate is ex-tracted frolll the roas~ed con~
centrate by means of an acid leach of pH no~ exceecling
3. The p~l oF the acid leach i5 typically in the range 1 to 3. The preferred acid leach is sulphuric acid. The leach time can vary~ but is typically 20 - 120 minutes.
The pyrite concentrate is generally fed to the roasting step either as a dry mass or as a slurry. When the con centrate is in the fornl of a slurry, the water content will generally be less than 50% by weight of the slurry.
10 - The pyrite concentrate will typically have a sulphur content of 20 to 50%5 generally 30 to ~0%, by weight.
Any base metals such as copper, cobolt and nickel present in the pyrite concen~rate are simultaneously extracted with the uraniunl values. The uraniuln values from the uranium rich leach solution may be recovered by methods known in the art such as solvent extraction or iron ex-change .
The process of the invention provides a very efFective , . - .: :
. . - . i -: .
, . , ..... ,~ . . ~, ~3~3~3~33~L
extrac~ion of uran-ium values from pyrite concentrates and a far better extract-ion than has been achieved in the past using a stron~ acidic''leach on its own.
The invention is illustrated by means of the fo'llowing examples.
'EXAMPLE i A pyrite concentrate, obta;ned from -the flotation of a ~,' pryite ore was found on analysis to contain 600 grams per ton of uranium, calculated as U308, and a sulphur content of 35% by weight.
The pyrlte concentrate was roasted -in a standarcl f1uidisecl bed roaster at 6~0C for an average period of 3 hours in the presence of sodium sulphate. The sodium su'lphate was present in an amount of 2% by weight of the concentrate. The roasted ~-~
concentrate was then subiected to a sulphuric acid leach of pH3 ~ ' for 60 minutes.
( ,i Analysis of the 'leach solution showed a uranium extraction in excess o-F 90%.
''E MPLE 2 A pyrite concentrate was found on analysis to contain 4'l%
by ~eight su'lphur and 600 grams per ton of uranium~ calculated as U308 . .... . .,, , ~
,. , ., . , . ~. , ~, . .. . . .
, ~ .
3~3~33'~
This concentrate was subjected to the same procedure as Example 19 save ~hat in a first experiment a roast temperature of 680C ;n the absence of sodium sulphate was used and in a secolld experiment a ~emperature of 690C in the presence of
The pyrite concentrate is generally fed to the roasting step either as a dry mass or as a slurry. When the con centrate is in the fornl of a slurry, the water content will generally be less than 50% by weight of the slurry.
10 - The pyrite concentrate will typically have a sulphur content of 20 to 50%5 generally 30 to ~0%, by weight.
Any base metals such as copper, cobolt and nickel present in the pyrite concen~rate are simultaneously extracted with the uraniunl values. The uraniuln values from the uranium rich leach solution may be recovered by methods known in the art such as solvent extraction or iron ex-change .
The process of the invention provides a very efFective , . - .: :
. . - . i -: .
, . , ..... ,~ . . ~, ~3~3~3~33~L
extrac~ion of uran-ium values from pyrite concentrates and a far better extract-ion than has been achieved in the past using a stron~ acidic''leach on its own.
The invention is illustrated by means of the fo'llowing examples.
'EXAMPLE i A pyrite concentrate, obta;ned from -the flotation of a ~,' pryite ore was found on analysis to contain 600 grams per ton of uranium, calculated as U308, and a sulphur content of 35% by weight.
The pyrlte concentrate was roasted -in a standarcl f1uidisecl bed roaster at 6~0C for an average period of 3 hours in the presence of sodium sulphate. The sodium su'lphate was present in an amount of 2% by weight of the concentrate. The roasted ~-~
concentrate was then subiected to a sulphuric acid leach of pH3 ~ ' for 60 minutes.
( ,i Analysis of the 'leach solution showed a uranium extraction in excess o-F 90%.
''E MPLE 2 A pyrite concentrate was found on analysis to contain 4'l%
by ~eight su'lphur and 600 grams per ton of uranium~ calculated as U308 . .... . .,, , ~
,. , ., . , . ~. , ~, . .. . . .
, ~ .
3~3~33'~
This concentrate was subjected to the same procedure as Example 19 save ~hat in a first experiment a roast temperature of 680C ;n the absence of sodium sulphate was used and in a secolld experiment a ~emperature of 690C in the presence of
4% by weight sodiunl sulphate was used. The leach tilne in each case was 20 minutes. The results obtained were as follows:
.
' Roast Temperature Na2$04 .~ % U Extraction 680 o 25 : :
__ __ ' EXAMPLE 3 _ . :
A pyrite concentrate was found on analysis to contain 24%
by weigh~ sulphur and 300 grarns per ton of uranium, calculated as U88 ~:.. ~) `' .
This concentrate was subjected to the same procedure as in Example 1~ save that the t~mperatures and sodium sulphate contents as set out below and a sulphuric acid leach solution of pH 1,1 were used:
Roast Temperature . Na2S04 % .. % U Extraction '. ~0 680 2 48 660 6 8~
.
' Roast Temperature Na2$04 .~ % U Extraction 680 o 25 : :
__ __ ' EXAMPLE 3 _ . :
A pyrite concentrate was found on analysis to contain 24%
by weigh~ sulphur and 300 grarns per ton of uranium, calculated as U88 ~:.. ~) `' .
This concentrate was subjected to the same procedure as in Example 1~ save that the t~mperatures and sodium sulphate contents as set out below and a sulphuric acid leach solution of pH 1,1 were used:
Roast Temperature . Na2S04 % .. % U Extraction '. ~0 680 2 48 660 6 8~
Claims
THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS
1.
A process for extracting uranium values from a pyrite con-centrate containing at least 20% by weight sulphur and at least 50 grams per ton of uranium, calculated as U3O8, including the steps of roasting the concentrate to convert the uranium to uranium sulphate, and solubilising the uranium sulphate in the roasted concentrate by means of an acid leach solution of pH not exceeding 3.
2.
A process according to claim 1 wherein the roast is carried out at a temperature in the range 650 to 750°C.
3.
A process according to claim 1 wherein the roast is carried out at a temperature in the range 650 to 700°C.
4.
A process according to claim 1 wherein the pyrite concentrate contains 20 to 50% by weight sulphur.
5.
A process according to claim 1 wherein the pyrite con-centrate contains 30 to 40% by weight sulphur.
6.
A process according to claim 1 wherein the pyrite con-centrate contains uranium calculated at U3O8, in the range of 50 grams to 2000 grams per ton.
7.
A process according to claim 1 wherein the pH of the leach solution is in the range 1 to 3.
8.
A process according to claim 7 wherein the leach solution is a sulphuric acid leach.
9.
A process for extracting uranium values from a pyrite con-centrate containing at least 20% by weight sulphur and at least 50 grams per ton of uranium, calculated at U308, in-cluding the steps of roasting the concentrate at a temperature in the range 650 to 750°C to convert the uranium to uranium sulphate, and solubilising the uranium sulphate in the roasted concentrate by means of a sulphuric acid leach of pH not exceeding 3.
10.
A process according to claim 9 wherein the pH of the leach solution is in the range 1 to 3.
A process according to claim 9 wherein the roast is carried out at a temperature in the range 650°C to 700°C.
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS
1.
A process for extracting uranium values from a pyrite con-centrate containing at least 20% by weight sulphur and at least 50 grams per ton of uranium, calculated as U3O8, including the steps of roasting the concentrate to convert the uranium to uranium sulphate, and solubilising the uranium sulphate in the roasted concentrate by means of an acid leach solution of pH not exceeding 3.
2.
A process according to claim 1 wherein the roast is carried out at a temperature in the range 650 to 750°C.
3.
A process according to claim 1 wherein the roast is carried out at a temperature in the range 650 to 700°C.
4.
A process according to claim 1 wherein the pyrite concentrate contains 20 to 50% by weight sulphur.
5.
A process according to claim 1 wherein the pyrite con-centrate contains 30 to 40% by weight sulphur.
6.
A process according to claim 1 wherein the pyrite con-centrate contains uranium calculated at U3O8, in the range of 50 grams to 2000 grams per ton.
7.
A process according to claim 1 wherein the pH of the leach solution is in the range 1 to 3.
8.
A process according to claim 7 wherein the leach solution is a sulphuric acid leach.
9.
A process for extracting uranium values from a pyrite con-centrate containing at least 20% by weight sulphur and at least 50 grams per ton of uranium, calculated at U308, in-cluding the steps of roasting the concentrate at a temperature in the range 650 to 750°C to convert the uranium to uranium sulphate, and solubilising the uranium sulphate in the roasted concentrate by means of a sulphuric acid leach of pH not exceeding 3.
10.
A process according to claim 9 wherein the pH of the leach solution is in the range 1 to 3.
A process according to claim 9 wherein the roast is carried out at a temperature in the range 650°C to 700°C.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA77/0995 | 1977-02-18 | ||
| ZA00770995A ZA77995B (en) | 1977-02-18 | 1977-02-18 | Uranium extraction |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1093831A true CA1093831A (en) | 1981-01-20 |
Family
ID=25571259
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA296,924A Expired CA1093831A (en) | 1977-02-18 | 1978-02-14 | Uranium extraction |
Country Status (4)
| Country | Link |
|---|---|
| AU (1) | AU513412B2 (en) |
| CA (1) | CA1093831A (en) |
| SE (1) | SE7801854L (en) |
| ZA (1) | ZA77995B (en) |
-
1977
- 1977-02-18 ZA ZA00770995A patent/ZA77995B/en unknown
-
1978
- 1978-02-14 CA CA296,924A patent/CA1093831A/en not_active Expired
- 1978-02-16 AU AU33353/78A patent/AU513412B2/en not_active Expired
- 1978-02-17 SE SE7801854A patent/SE7801854L/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| ZA77995B (en) | 1978-08-30 |
| SE7801854L (en) | 1978-08-19 |
| AU3335378A (en) | 1979-08-23 |
| AU513412B2 (en) | 1980-11-27 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |