AU672715B2 - Process of roasting refractory gold ores - Google Patents
Process of roasting refractory gold ores Download PDFInfo
- Publication number
- AU672715B2 AU672715B2 AU71583/94A AU7158394A AU672715B2 AU 672715 B2 AU672715 B2 AU 672715B2 AU 71583/94 A AU71583/94 A AU 71583/94A AU 7158394 A AU7158394 A AU 7158394A AU 672715 B2 AU672715 B2 AU 672715B2
- Authority
- AU
- Australia
- Prior art keywords
- roasting
- process according
- fluidized
- oed
- sulfur
- 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
- 239000010931 gold Substances 0.000 title claims description 33
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims description 32
- 229910052737 gold Inorganic materials 0.000 title claims description 32
- 238000000034 method Methods 0.000 title claims description 17
- 239000007789 gas Substances 0.000 claims description 42
- 239000000446 fuel Substances 0.000 claims description 31
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 22
- 229910052717 sulfur Inorganic materials 0.000 claims description 22
- 239000011593 sulfur Substances 0.000 claims description 22
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims description 20
- 229910052683 pyrite Inorganic materials 0.000 claims description 20
- 239000011028 pyrite Substances 0.000 claims description 20
- 239000002245 particle Substances 0.000 claims description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 125000004429 atom Chemical group 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 150000001298 alcohols Chemical class 0.000 claims description 3
- 230000001590 oxidative effect Effects 0.000 claims description 3
- 101710178035 Chorismate synthase 2 Proteins 0.000 claims description 2
- 101710152694 Cysteine synthase 2 Proteins 0.000 claims description 2
- 150000002170 ethers Chemical class 0.000 claims description 2
- 125000004430 oxygen atom Chemical group O* 0.000 claims description 2
- 235000009917 Crataegus X brevipes Nutrition 0.000 claims 1
- 235000013204 Crataegus X haemacarpa Nutrition 0.000 claims 1
- 235000009685 Crataegus X maligna Nutrition 0.000 claims 1
- 235000009444 Crataegus X rubrocarnea Nutrition 0.000 claims 1
- 235000009486 Crataegus bullatus Nutrition 0.000 claims 1
- 235000017181 Crataegus chrysocarpa Nutrition 0.000 claims 1
- 235000009682 Crataegus limnophila Nutrition 0.000 claims 1
- 235000004423 Crataegus monogyna Nutrition 0.000 claims 1
- 240000000171 Crataegus monogyna Species 0.000 claims 1
- 235000002313 Crataegus paludosa Nutrition 0.000 claims 1
- 235000009840 Crataegus x incaedua Nutrition 0.000 claims 1
- 210000002837 heart atrium Anatomy 0.000 claims 1
- 229940032330 sulfuric acid Drugs 0.000 claims 1
- 239000000203 mixture Substances 0.000 description 10
- 238000004064 recycling Methods 0.000 description 9
- 239000007787 solid Substances 0.000 description 7
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 235000011464 Pachycereus pringlei Nutrition 0.000 description 1
- 240000006939 Pachycereus weberi Species 0.000 description 1
- 235000011466 Pachycereus weberi Nutrition 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- MNWBNISUBARLIT-UHFFFAOYSA-N sodium cyanide Chemical compound [Na+].N#[C-] MNWBNISUBARLIT-UHFFFAOYSA-N 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- 239000000126 substance Substances 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
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
- C22B1/06—Sulfating roasting
-
- 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
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
- C22B1/10—Roasting processes in fluidised form
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Catalysts (AREA)
Description
i D1 r/UU/I 1 28/5/91 Regulation 3.2(2)
AUSTRALIA
Patents Act 1990
ORIGINAL
COMPLETE SPECIFICATION STANDARD PATENT
I
Do o+
D
r D a r r +r c sro o rrr s
D
rr ou r~~ r*~ *r u Application Number: Lodged: Invention Title: PROCESS OF ROASTING REFRACTORY GOLD ORES The following statement is a full description of this invention, including the best method of performing it known to us -I -i I- A 7667 METALLGESELLSCHAFT AG August 26, 1993 Reuterweg 14 60323 Frankfurt-ou-Main Case No. 95 00 06 Process of Roasting Refractory Gold Ores
DESCRIPTION
This invention relates to a process of i aroasting refractory gold ores in the presence of added fuels ii an oxidizing atmosphere ii a fluidized ued.
Refractory gold ores are ores which cannot directly ue leached with NaCN and which as a goldoearing material contain arsenopyrites or pyrites which cotain more or less organic caruon. They have an extremely low gold content. Before such ores can ue leached with cynides, their sulfur and caroon contents must ue oxidized as completely as possiule. That oxidation is effected uy a roasting with oxygea-coutaining gases. In many refractory gold ores the content of arseuipyrite, pyrite and organic caroon is uot sufficient for the generation of the required reaction heat 1 1 11
-A
-2so that fuel must ue added. Numerous refractory gold ores must be roasted at a relatively low temperature if a high yield of gold is to be achieved in the suosequent leaching.
EP-AO 508 542 teaches to roast gold ores at a temperature from 475 to 6000C and particularly from 500 to 57500. Coal, uutane or propane have oeen mentioned as added fuels. The ignition temperature should be equal to or exceed that of propane. But the proportion of propane and uutane which is comousted to CO2 and H20 is unsatisfactorily low. The combustion results in a production of CO and H2 at consideraole rates. CO and H2 have ignition temperatures from 600 to 65000 and from 560 to 58000C, respectively.
Gold ores can oe roasted only under mild conditions in order to avoid hot spots on the surface of the particle. The yield of gold will highl.y depend, inter alia, on the roasting temperature. The roasting temperature must oe kept uelow the sintering temperature of tne components of the ore which is veing roasted.
Most gold ores contain small amounts of pyrite and/or inorganic caruon. Owing to the dissipation of heat during heating up, from the exhaust gas, during the discharge from the roaster and other operations the heating value of the gold ore is not suffcient for a self-sustaining roasting 2 i even at temperatures of only about 500°C. For this reason a fuel which has low iguition and combustion temperatures must oe added to avoid a decrease of the gold yield.
It is an object of the invention to use a fuel which will reliaoly oe ignited at low temperatures and whicn can ue combusted to produce an exhaust gas which is free of or has only low contents of CO, H 2 and hydrocaruous.
IA the process mentioned first hereinoefore that ooject is accomplished in accordance with the i" invention in that sulfur and/or pyrite is fed as a fuel i to the fluidized bed and roasting is carried out at temperatures from 400 to 650° 0 C ia conjunction with a supply of oxygen-coLItaining gases. The advantage afforded •oy tne process in accordance with the invention resides in that the comoustion of sulfur and/or pyrite does not result iu a production of CO, H 2 and hydrocaroons.
It is surprising tat sulfur and pyrite S can reliably ue ignited at low roasting temperatures.
Sulfur will ourn at temperatures in the range from 200 to 500 °C and pyrite at temperatures in the range from 450 to 600°C. The sulfur and/or pyrite to oe added may oe pre-mixed with the gold ore or may directly oe fed to the fluidized oed.
In accordance with the invention, refractory gold ores are roasted in an orthodox (non- -4circulating) or in a circulating fluidized bed. The oxygen-containing gases are supplied as fluidizing gas to the fluidized bed reactor oelow the nozzle uottom. In accordance with the invention, additional oxygen-containing gases may ue supplied as primary and secondary gases to the fluidized Oed reactor from the sides. The oxygen-containing gases consist of air or of oxygen-enriched air.
A preferred feature resides in that the roasting is carried out at temperatures from 500 to 550 OC. Particularly good gold yields will oe achieved ,at said temperatures.
A preferred feature of the invention resides in that sulfur and/or pyrite and at least one additional fuel selected from hydrocaruons containing 1 to 16 caroon atoms, alcohols containing 1 to 6 caroon 9 atoms and 1 to 2 CH groups, organic ethers containing 2 to 8 caroon atoms and 1 oxygen atom, CS 2 and H 2 S are fed as fuels to the fluidized oed. Because sulfur and/or pyrite are comousted ia conjunction with one or more of said additional fuels, the ignition temperature of said additional fuels will oe decreased if their ignition temperature exceeds the ignition temperature of sulfur or pyrite. As a result, said additional fuels will oe ig- 1nited sooner in such a mixture. If the ignition temperature of one of said additional fuels is below the ignition temperature of sulfur or pyrite, sulfur or pyrite will have a lower ignition temperature in a mixture which contains T 1 1 1 i
A
such an additional fuel.
The concentration of the additional fuels iii a mixture with sulfur and/or pyrite must exceed the ignition limit. The ignition limit of a fuel is the miUimum concentration of a fuel i" a gas mixture in which that fuel can ue ignited. The additional fuels will oe supplied at a concentrationa in excess of their ignition limnit if the heat content in the reactor is not sufficient for a heating to the required roasting temperature. The heat content in the reactor is deterined uy the amounts of carDon and sulfur contained iu the refractory gold ores and oy the rate at which sulfur and/or pyrite is added as a fuel. This means that the roasting temperature can be controlled oy *a control of the rate at which the additional fuels are added. The additional fuels will oe added at such rates that the roasting temperature does not exceed 6500°C 0 f and preferably 550 C and that the exhaust gas from the -at 'fluidized oed has a, H 2 content of <10 vppm, preferaDly <5 vppm, a oii0 content of oy volume, preferaoly C100 vppm and a hydrocaruon content of <100 vppm, -J ~preferauly (150 ppm.
The additional fuels whih may oe employed include mixed hydrocaroons whicha are recovered as fractions oy distillation, such as kerosine, or uecome avail- j able as refinery waste products. In addition to hydro- L caroons, the additional fuels may include mixed alcohols, -1 A 1i -6which become available as waste products in the distillation of ethanol.
A preferred feature of the invention resides in that the particle size of the gold ores is below 1 mm. Good results will oe produced with that particle size.
A preferred feature of the invention resides iLa that 60 to 80 of the gold ore have particle sizes below 75 micrometers. Particularly good results will oe produced with that particle size. The term "particle size" stands for the median particle diameter d 50 A preferred feature of the invention resides in that the 02 content of the gas which is fed to the fluidized oed amounts to 20 to 50 uy volume. The use of oxygen-enriched air will result in an improved ignition of the fuel mixture. The use of oxygen-enriched air is particularly economical.
The use of the additional fuels affords the advantage that they are substantially completely combusted at a low temperature and that the resulting exhaust gas has very low contents of CO, H 2 and hydrocaruous so that said components need not oe removed from the exnaust gas by afterourning In a succeeding production of sulfuric acid it will oe desirable that the contents of CO, H 2 and hydrocarbons
I
-7are very low oecause said substances tend to poison the catalyst used for the oxidation of SO 2 to SO A preferred feature of the invention resides in that a partial stream is branched from the hot exhaust gas which has oeen dedusted and said partial stream of exhaust gas is admixed to the fluidizing gas oefore it is fed to the fluidized bed. The recycling of part of the exhaust gas and the mixing of said part with the fluidiziug gas have the result that the fluidizing gas is heated. The recycling of a part of the exhaust gas will enrich S02 in the exhaust gas.
A preferred feature of the invention resides in that the SO2 gas which has oeen formed oy the roasting of refractory gold ores and is carried away in the exhaust gas is used for a production of sulfuric acid.
The economy of the process in accordance with the invention will oe improved if the SO 2 which has oeen formed oy the roasting and is carried away in the exhaus' gas is used for a production of sulfuric acid without an afterourning. The SO2 gas will be scruobed refore it is fed to the plant for producing sulfuric acid.
A preferred feature of the invention resides in that the roasting is carried out in a circulating fluidized oed.
The circulating fluidized bed system comprises a fluidized bed reactor, a recycling cyclone,
S'I
-8and a recycling line. From the "orthodox" fluidized bed, in which a dense phase is separated by a distinct density step from the overlying gas space, the circulating fluidized oed differs in that it includes states of distribution having no defined ooundary layer. There is io density step oetween the dense phase and the overlying dust space out the solids concentration decreases continuously in the reactor from oottom to top. A gassolids suspension is discharged from the upper part of the reactor. The following ranges will oe obtained if the operating conditions are defined oy the Froude and 1 Archimedes numbers: 0.1 K 3/4 x Fr 2 x k g and 0.01 Ar 100 wherein SAr dk x g and o g x x F2 u g x dk and u the relative gas velocity in m/sec Ar the Archimedes number Fr the Froude number j *1 -r 3 -9the density of the gas in kg/m k the density of the solid particle in kg/m 3 d k the diameter of the spherical particle in m the kinematic viscosity in m /sec g the constant of gravitation in m/sec 2 The suspension discharged from the fluidized oed reactor is fed to the recycling cyclone of the circulating fluidized bed system. Substantially all solids are removed from the suspension in said cyclone and the separated solids are recycled to the i 0 fluidized oed reactor il such a manner that the amount of solids circulated per hour in the circulating fluidized oed system is at least four times the weight of solids contained in the fluidized bed reactor.
The invention will now De explained with reference to the Examples.
EXAMPLE 1 The refractory gold ore which was used contained 8 mg/kg gold, 1.8% by weight sulfur as pyrite and 0.08% by weight caroon. The median particle size do was 30 micrometers, and 100%o of the particles were smaller than 200 micrometers.
The roasting plant was a circulting fluidized Ded system and considdb maihly of a fluidized ued reactor, a recycling cyclone, which was directly I -i -L connected to the gas outlet at the top part of the reactor, and a recycling line. The solids which had !een separated in the cyclone were recycled through the recycling line to the reactor.
A mixture containing 48 g pyrite per kg ore was prepared and was charged at a rate of kg/h through a downcomer into the fluidized bed reactor.
Air which coutained 21% by weight oxygen and was at a temperature of 40000 was supplied to the windbox of the fluidized bed reactor at a rate of 22 o sm3/h sadr Ssm /h (sm standard cuuic meter). The carrier gas flowed through the openings of the perforated bottom.
The temperature iLl the reactor was 520 C. The gas from roasting contained 3.3% by volume SO 2 0.2% oy volume C02, 20 vppm CO, and 16.3% oy volume 02. The contents of H 2 and Hydrocarbons were below the detection threshold of 1 vppm. The exhaust gas was scruobed with an alkaline absorbent to remove SO2 and was then discharged through a chimney. The roasted material coitained S* 0.05% uy weight sulfur and (0.01% oy weight carbon.
Its further processing resulted in a gold yield of 94%.
EXAMPLE 2 Example 2 was carried out like Example 1 out with a carrier gas which contained 32% by volume 02 and owing to a recycling of exhaust gas contained 7% by
A
'i el i -ll-~ -11-I volume SO The fluidized bed reactor was supplied 2 with a mixture which contained 50 g sulfur per kg ore. The gas from roasting coutained 12.7% oy volume S0 2 0.1% by volume C02, 5 vppm CO, and 24.2% by volume 02. The contents of H 2 and hydrocaroons were Delow the detection threshold of 1 vppm. The roasted material contained 0.04% 7oy weight sulfur and 0.01% uy weignt caruon. Its further processing resulted in a gold yield of 96%.
The gold ore used in Examples 1 and 2 had the following composition: o o a* 4 8 mg/kg Au e 5.5% uy weight ieS 2 0.07, by weight 2e rIssI The pyrite used in Example 1 had the following composition; 91% oy weight FeS 2% oy weight FeS 79% oy weight SiO, A120u and other components., 2, J ""The sulfur used in Example 2 had the| i following composition: 98% oy weight S 2% oy weignt impurities
Claims (7)
1. A process of roasting refractory gold ores in the presence of added fuels in an oxidizing atmosphere in a fluidized bed, characterized in that sulfur and/or pyrite is fed as a fuel to the fluidized oed and roast- ing is carried out at temperatures from 400 to 650 °C in conjunction with a supply of oxygen-containing gases.
2. A process according to claim 1, characterized ia that the roasting is carried out at temperatures from 500 to 550 C. 5r process according to claim 1 or 2, S characterized in that sulfur and/or pyrite and at least one additional fuel selected from hydrocaroons cotain- ing 1 to 16 caroon atoms, alcohols containing 1 to 6 S caruon atoms and 1 to 2 CH groups, organic ethers con- taining 2 to 8 caroon atoms and 1 oxygen atom, CS 2 and H 2 S are fed as fuels to the fluidized oed.
4. A process according to claims 1 to characterized in that the gold ore has a particle size uelow 1 tum. A process according to claims 1 to 4, characterized in that 60 to 80 of the gold ore have a size oelow 75 micrometers.
6. A process according to claims 1 to characterized in that the 02 content of the gas which is fed to the fluidized bed amounts to 20 to 50 oy volume. T 1 l l I ,,f
7. A process according to claims 1 to 6, characterized iu that a partial stream is branched from the hot exhaust gas which has been dedusted and said partial stream of exhaust gas is admixed to the fluid- izing gas before it is fed to the fluidized oed.
8. A process according to claims 1 to 7, characterized in that the 802 gas which has oeen formed oy the roasting of refractory gold ores and is canied away in the exhaust gas is used for a production of sul- furic acid.
9. A process according to claims 1 to 8, characterized in that the roasting is carried out in a circulating fluidized bed. tic tttt I DATED this 30th day of August 1994. c c METALLGESELLSCHAFI AKTIENGESELLSCHAFT o t t .i WATERMARK PATENT TRADEMARK ATTORNEYS St "THE ATRIUM" 290 BURWOOD ROAD HAWTHORN. VIC. 3122. C ~nI I -14- ABSTRA CT Refractory gold ores are roasted in the presence of added fuels in an oxidizing atmosphere in a fluidized oed at a temperature from 450 to 650 ~C in a fluidized oed, which is supplied with oxygen- containing gases. To achieve a low roasting tempera- ture, sulfur and/or pyrite is used as added as a fuel. C C ILI
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE4329417 | 1993-09-01 | ||
| DE4329417A DE4329417C1 (en) | 1993-09-01 | 1993-09-01 | Process for roasting refractory gold ores |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU7158394A AU7158394A (en) | 1995-03-16 |
| AU672715B2 true AU672715B2 (en) | 1996-10-10 |
Family
ID=6496516
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU71583/94A Expired AU672715B2 (en) | 1993-09-01 | 1994-08-30 | Process of roasting refractory gold ores |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP0641864B1 (en) |
| AU (1) | AU672715B2 (en) |
| DE (2) | DE4329417C1 (en) |
| ES (1) | ES2113050T3 (en) |
| PE (1) | PE11195A1 (en) |
| ZA (1) | ZA946709B (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6482373B1 (en) | 1991-04-12 | 2002-11-19 | Newmont Usa Limited | Process for treating ore having recoverable metal values including arsenic containing components |
| DE4314231A1 (en) * | 1993-04-30 | 1994-11-03 | Metallgesellschaft Ag | Process for roasting refractory gold ores |
| DE19546538A1 (en) * | 1995-12-13 | 1997-06-19 | Metallgesellschaft Ag | Process for the thermal treatment of refractory gold ores |
| US5972302A (en) * | 1996-08-27 | 1999-10-26 | Emr Microwave Technology Corporation | Method for the microwave induced oxidation of pyritic ores without the production of sulphur dioxide |
| CA2263497A1 (en) * | 1996-08-27 | 1998-03-05 | Paul R. Kruesi | Method for microwave induced oxidation of sulphidic ore material in fluidized bed without sulphur dioxide emissions |
| AUPQ078399A0 (en) * | 1999-06-04 | 1999-06-24 | Tox Free Systems Limited | Recovery of gold from gold sulphides |
| BR0212890A (en) * | 2001-09-14 | 2004-10-13 | Alexander Beckmann | Cobalt and nickel extraction process from ore and ore concentrates |
| EP1327693A1 (en) * | 2002-01-12 | 2003-07-16 | Alexander Beckmann | Process for extracting cobalt and nickel from ores and ore concentrates |
| RU2443790C1 (en) * | 2010-07-01 | 2012-02-27 | Открытое акционерное общество "Иркутский научно-исследовательский институт благородных и редких металлов и алмазов" ОАО "Иргиредмет" | Method for determining content of precious metals in ores and their derivatives |
| AP2015008652A0 (en) | 2013-02-20 | 2015-08-31 | Outotec Finland Oy | Process and plant for producing copper and/or cobalt sulfate |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5123956A (en) * | 1991-04-12 | 1992-06-23 | Newmont Mining Corporation | Process for treating ore having recoverable gold values and including arsenic-, carbon- and sulfur-containing components by roasting in an oxygen-enriched gaseous atmosphere |
| AU1076992A (en) * | 1991-02-09 | 1992-08-13 | Outokumpu Oyj | Process for roasting refractory gold ores |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2117028T3 (en) * | 1991-04-12 | 1998-08-01 | Metallgesellschaft Ag | PROCEDURE FOR THE TREATMENT OF MINERAL WITH VALUE OF RECOVERABLE METALS INCLUDING ARSENIC-CONTAINING COMPONENTS. |
-
1993
- 1993-09-01 DE DE4329417A patent/DE4329417C1/en not_active Expired - Lifetime
-
1994
- 1994-08-05 EP EP94202265A patent/EP0641864B1/en not_active Expired - Lifetime
- 1994-08-05 ES ES94202265T patent/ES2113050T3/en not_active Expired - Lifetime
- 1994-08-05 DE DE59405354T patent/DE59405354D1/en not_active Expired - Fee Related
- 1994-08-23 PE PE1994248998A patent/PE11195A1/en not_active IP Right Cessation
- 1994-08-30 AU AU71583/94A patent/AU672715B2/en not_active Expired
- 1994-09-01 ZA ZA946709A patent/ZA946709B/en unknown
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU1076992A (en) * | 1991-02-09 | 1992-08-13 | Outokumpu Oyj | Process for roasting refractory gold ores |
| US5123956A (en) * | 1991-04-12 | 1992-06-23 | Newmont Mining Corporation | Process for treating ore having recoverable gold values and including arsenic-, carbon- and sulfur-containing components by roasting in an oxygen-enriched gaseous atmosphere |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0641864A1 (en) | 1995-03-08 |
| EP0641864B1 (en) | 1998-03-04 |
| AU7158394A (en) | 1995-03-16 |
| ZA946709B (en) | 1995-04-21 |
| DE59405354D1 (en) | 1998-04-09 |
| DE4329417C1 (en) | 1994-08-18 |
| ES2113050T3 (en) | 1998-04-16 |
| PE11195A1 (en) | 1995-05-06 |
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