EP3433388A1 - Process and facility for thermal treatment of a sulfur-containing ore - Google Patents
Process and facility for thermal treatment of a sulfur-containing oreInfo
- Publication number
- EP3433388A1 EP3433388A1 EP17715066.1A EP17715066A EP3433388A1 EP 3433388 A1 EP3433388 A1 EP 3433388A1 EP 17715066 A EP17715066 A EP 17715066A EP 3433388 A1 EP3433388 A1 EP 3433388A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- gas
- reactor
- ore
- sulfur
- recycling
- 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
- 238000000034 method Methods 0.000 title claims abstract description 60
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 34
- 239000011593 sulfur Substances 0.000 title claims abstract description 34
- 238000007669 thermal treatment Methods 0.000 title claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 130
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 49
- 238000004064 recycling Methods 0.000 claims abstract description 44
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 37
- 239000001301 oxygen Substances 0.000 claims abstract description 37
- 238000000746 purification Methods 0.000 claims abstract description 25
- 238000001816 cooling Methods 0.000 claims abstract description 21
- 239000012535 impurity Substances 0.000 claims abstract description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 27
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 10
- 238000010521 absorption reaction Methods 0.000 claims description 9
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 claims description 8
- 239000000470 constituent Substances 0.000 claims description 8
- 229910052787 antimony Inorganic materials 0.000 claims description 7
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 claims description 7
- 229910052785 arsenic Inorganic materials 0.000 claims description 7
- 239000000155 melt Substances 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 4
- 238000005243 fluidization Methods 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- 229910017052 cobalt Inorganic materials 0.000 claims description 3
- 239000010941 cobalt Substances 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 230000001276 controlling effect Effects 0.000 claims description 2
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 2
- 229910052737 gold Inorganic materials 0.000 claims description 2
- 239000010931 gold Substances 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 238000002485 combustion reaction Methods 0.000 claims 1
- 239000002826 coolant Substances 0.000 claims 1
- 239000007788 liquid Substances 0.000 claims 1
- 239000006163 transport media Substances 0.000 claims 1
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 26
- 238000001354 calcination Methods 0.000 description 10
- 229940091658 arsenic Drugs 0.000 description 8
- 238000002844 melting Methods 0.000 description 6
- 230000008018 melting Effects 0.000 description 6
- 239000000446 fuel Substances 0.000 description 4
- 230000002349 favourable effect Effects 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 229910000410 antimony oxide Inorganic materials 0.000 description 2
- 229910000413 arsenic oxide Inorganic materials 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000000112 cooling gas Substances 0.000 description 2
- QUQFTIVBFKLPCL-UHFFFAOYSA-L copper;2-amino-3-[(2-amino-2-carboxylatoethyl)disulfanyl]propanoate Chemical compound [Cu+2].[O-]C(=O)C(N)CSSCC(N)C([O-])=O QUQFTIVBFKLPCL-UHFFFAOYSA-L 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- VFNGKCDDZUSWLR-UHFFFAOYSA-N disulfuric acid Chemical compound OS(=O)(=O)OS(O)(=O)=O VFNGKCDDZUSWLR-UHFFFAOYSA-N 0.000 description 2
- 238000011143 downstream manufacturing Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VTRUBDSFZJNXHI-UHFFFAOYSA-N oxoantimony Chemical class [Sb]=O VTRUBDSFZJNXHI-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 229940000425 combination drug Drugs 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- MSNOMDLPLDYDME-UHFFFAOYSA-N gold nickel Chemical compound [Ni].[Au] MSNOMDLPLDYDME-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000007210 heterogeneous catalysis Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 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
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
-
- 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
- C22B15/00—Obtaining copper
- C22B15/0002—Preliminary treatment
- C22B15/001—Preliminary treatment with modification of the copper constituent
- C22B15/0013—Preliminary treatment with modification of the copper constituent by 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/005—Preliminary treatment of ores, e.g. by roasting or by the Krupp-Renn process
Definitions
- the invention relates to a process and a plant for thermal treatment of a sulfur- containing ore in which the ore is calcined at temperatures of between 600 and 1200 °C in the presence of oxygen in a reactor so that between 1 and 90 % by weight of the sulfur contained in the ore is burned to sulfur dioxide and impurities contained are driven off in gaseous form, in which exhaust gas being produced and containing the sulfur dioxide is fed into a gas purification comprising at least one component and/or in which the calcined ore is fed into at least one further process stage.
- the ore is heated at a temperature of between 600 and 1200 °C, preferably 600 to 900 °C.
- This operation is also referred to as calcining.
- sulfur contained in the ore is burned to sulfur dioxide (SO 2 ), by which again heat is produced. Therefore, preferably, this process, after ignition with externally fed fuel, can be conducted in an autothermic manner.
- the energy demand of this process increases with the amounts of impurities in the ore. So the sulfur contained is either no longer capable of allowing an autothermic process control or a very large proportion of the sulfur contained is already consumed during this calcining process, so that into the later melt of the ore more fuel has to be fed from outside.
- a sulfur-containing ore is fed into an autothermal operated reactor and there it is thermally treated at a temperature of between 600 and 1200 °C, pref- erably 600 and 900 °C, particularly preferably 650 and 750 °C in the presence of oxygen.
- So 1 to 90 % by weight, preferably 10 to 60 % by weight of the sulfur contained in the ore is burned to sulfur dioxide and impurities contained are driven off in gaseous form.
- Such a process is referred to as partial calcination.
- a typical ore is characterized by the following composition:
- Table 1 typical composition of ore.
- an exhaust gas from one component of the gas purification and/or an exhaust gas from the further process stage are fed into the reactor as recycling gas.
- a gas used for cooling before, during and/or after the gas purification and/or a gas used for cooling before, during and/or after a process stage is also possible to use a gas used for cooling before, during and/or after the gas purification and/or a gas used for cooling before, during and/or after a process stage as recycling gas or, in an even more preferred embodiment, to use coils in the reactor for a heat transfer medium.
- the recycling gas must have a temperature of higher than 100 °C and thus reduce the energy demand for operating in the given temperature range by feeding it into the reactor.
- the energy demand in the reactor is reduced so that a lower amount of sulfur being contained in the ore has to be burned. So also ores being characterized by lower contents of sulfur can be calcined more easily.
- the procedure according to the present invention is also preferable, because so the calcined ore is characterized by a higher content of sulfur which in turn can act as an internal energy supplier in downstream processing stages.
- the reactor is operated in an autothermic manner, i.e. that during steady operation no fuel has to be fed in or the reactor has to be cooled. This considerably reduces the effort in connection with the required equipment, because in this manner no fuel has to be fed into the reactor.
- the autothermic operation is realized by burning a sufficient amount of sulfur which is also contained in the ore to SO2:
- the temperature in the reactor is controlled by the amount of oxygen which is fed in, because the amount of sulfur which can be burned depends on the oxygen being available.
- the driven off impurities contain arsenic and/or antimony in amounts of between 0.1 and 10 % by weight, preferably 0.5 and 5 % by weight, based on the composition of the ore being fed into the reactor.
- Arsenic and antimony are compounds which in particularly at temperatures of between 650 and 750 °C evaporate and thus can be discharged in gaseous form. At the same time, arse- nic and antimony are highly toxic and thus have to be removed from the ore as early as possible.
- the ore contains in addition at least 20 % by weight of copper, cobalt, gold and/or nickel, whereby the conduction of the process according to the present invention is particularly cost-effective.
- the recycling gas has a temperature of between 200 and 500 °C, particularly preferably between 300 and 450 °C, because in this manner as much as possible heat is introduced into the reactor.
- the temperature of the gas is not so high that the required equipment would be subjected to temperatures which are too high and thus correspondingly would be more cost-intensive to purchase.
- the recycling gas has a proportion of oxygen of between 3 and 20 % by weight. When the reaction procedure is conducted according to the present invention, then such a proportion of oxygen is sufficient for operating the reactor at the required temperatures in an autothermic manner.
- a further advantage of the invention is that due to the fact that now a lower amount of sulfur has to be burned for achieving the required temperatures also the amount of oxygen which has to be provided for the reaction is lower. However, by a decrease of the oxygen content it is possible to reliably avoid the formation of arsenic and/or antimony oxides, which cannot be removed from the ore in gaseous state any longer and thus remain in it and reduce the quality thereof.
- the recycling gas is a mixture of several exhaust gases and/or gases which are used for cooling.
- a mixture in which the oxygen content is adjusted in a targeted man- ner to the desired temperature in the reactor due to the burning of sulfur is a mixture which is of advantage.
- the ore is fed into a process stage being designed as a melt and gases from this melt and/or from a downstream cooling are returned back into the reactor as recycling gas or constituent of the recycling gas.
- the advantage is that the melt is realized at very high temperatures (> 1200 °C) so that also cooling and/or exhaust gases from the melt are characterized by correspondingly high temperatures and a total gas flow which is smaller has to be returned back, since it is already characterized by a very high content of energy.
- a preferable design of the invention is characterized by a gas purification which comprises a process for producing sulfuric acid from sulfur dioxide being contained in the exhaust gas.
- a gas purification which comprises a process for producing sulfuric acid from sulfur dioxide being contained in the exhaust gas.
- Such a process for producing sulfuric acid is, for example, described in DE 10 2005 008109 A1 .
- Such a process releases relatively much energy, so that it is of advantage to reuse this energy for calcination in the form of the recycling gas.
- the source of oxygen is air.
- a gas which is poor in oxygen results, wherein poor in oxygen in the sense of the invention means a proportion of oxygen which is lower than 21 % by volume, preferably lower than 18 % by volume.
- This gas which is poor in oxygen can then be re- turned back into the reactor as recycling gas or as constituent of the recycling gas, so that here the provision of oxygen is minimized and therefore the risk of forming arsenic and/or antimony oxides is considerably reduced.
- the gas purification comprises a process for producing sulfuric acid from SO2
- the SO3 is absorbed with sulfuric acid in at least two stages and that between two adjacent stages the sulfuric acid is guided through a heat exchanger.
- a recovery process is also described in DE 10 2005 008109 A1 .
- the heat exchanger uses air or another gas, preferably with an oxygen content of ⁇ 20 % by volume, so that the cooling gas of the heat exchanger is returned back into the reactor as recycling gas or constituent of the recycling gas.
- the sulfur dioxide is at first reacted to sulfur trioxide and subsequently the sulfur trioxide is absorbed in sulfuric acid.
- the gas which is poor in oxygen from the heterogeneous reaction of SO2 to SO3 and also the heated air from the at least one heat exchanger between both absorbers in the absorption stage are mixed with air so that a specific oxygen content of between 3 and 20 % by weight is adjusted, whereby the temperature in the reactor can be regulated or controlled by regulating or controlling the amount of sulfur to be burned and thus the additional energy amount through the oxygen content.
- the invention also comprises a facility with the features of patent claim 13.
- a plant is designed for conducting a process with the features of patent claims 1 to 12.
- Such a facility for thermal treatment of a sulfur-containing ore comprises an autothermal reactor in which the ore is calcined at temperatures of between 600 and 1200 °C, preferably 600 and 900 °C, particularly preferably 650 to 750 °C in the presence of oxygen. Furthermore, such a facility comprises at least one component of a gas purification and/or a further process stage for treating the ore. Furthermore, according to the present invention, the facility comprises a return line from at least one component of the gas purification and/or the further process stage and/or a return line from a cooling within the gas purification and/or a cooling for the further process stage.
- So heated gas as recycling gas can be returned back into the reactor for calcining, whereby, in addition to the burning of sulfur, the required energy input is reduced.
- the oxygen content in the calcining reactor can be reduced which decreases the risk of forming oxides which can be removed only with high effort, and, on the other hand, so a lower amount of sulfur has to be burned. Therefore, it is possible to process ore with a sulfur content which is not sufficient for achieving the required temperature at all, or the sulfur content of the calcined ore remains higher so that the ore in downstream process stages can be processed better due to the inherent energy content. It is particularly preferable, when the reactor is designed as a fluidized bed reactor, because such a fluidized bed reactor results in very homogenous conditions throughout the whole fluidized bed.
- cooling coils are foreseen. This is particular preferred for a fluidized bed reactor wherein the coils at least partly are immersed into the fluidized bed during operation, but it is not restricted to this reactor type. With these cooling coils, instable process conditions as well as start-up and shut down of the plant can be handled.
- Fig. 1 shows a procedure according to the present invention in a schematic manner.
- Table 2 composition of the introduced ore.
- reactor 1 the ore is thermally treated in a so-called calcining process at temperatures of between 550 and 1000 °C, preferably 680 and 720 °C under auto- thermal conditions.
- sulfur contained in the ore is burned so that SO2 and heat are formed.
- impurities in particularly arsenic and/or antimony, are evaporated which is an energy consuming process.
- Exhaust gases consisting of the introduced air, the produced SO2 and gaseous impurities are subsequently drawn off via line 1 1 and are fed into a cyclone 20.
- the gas purification 22 preferably, comprises a hot filtration and/or a quench, preferably with water, and/or a wet filtration and/or a mercury removal and/or a gas drying, particularly preferably in this arrangement.
- Exhaust gases which are produced so and/or a gas which is used for cooling of one of the mentioned gas components or between the mentioned gas purification components can then be returned back into the reactor 10 via lines 23, 41 and 40 as recycling gas, wherein this recycling gas has a temperature of higher than 100 °C, preferably 300 to 450 °C.
- the gas from the gas purification facility 22 or also directly from line 21 is fed into a sulfur trioxide reactor 30 via line 23 for reacting SO2 to SO3 in a heterogeneously catalyzed reaction.
- the oxygen required for this reaction is introduced via line 31 .
- lines 22 or 23 also an introduction into lines 22 or 23 would be imaginable.
- the exhaust gas which is produced and which is oxygen- depleted, since oxygen from air has been used for the reaction of SO2 to SO3 is fed as recycling gas into reactor 10 via line 42 and line 40.
- the absorption is characterized by a design of at least two stages so that line 35 does not immediately withdraw the end product, but does it fed into a second absorption stage 36 from which then the end product is drawn off via line 37.
- a heat exchanger 39 is located which also uses a gas, preferably air, as a heat carrier medium. So the air fed via line 38 into the heat exchanger 39 can be heated and it can be fed into recycling line 40 via line 44, 43. Similarly, also the use of a process gas which is poor in oxygen instead of air would be imaginable.
- gas which is poor in oxygen thus gas with an oxygen content of between 5 and 20 % by weight, preferably 8 to 14 % by weight is drawn off from the sulfur trioxide reactor 30 via line 42.
- This step of drawing off can also be realized via a chimney (not shown), thus after passing both absorption stages.
- the oxygen content in lines 43, 40 optionally also by further admixing via line 41 , can be controlled or regulated.
- a definition of the oxygen content also results in the stoichiometrically possible conversion of sulfur in reactor 10, whereby in this manner also the amount of heat generated by the burning of sulfur and thus finally the temperature in reactor 10 can be controlled.
- the ore is drawn off from reactor 10 via line 12.
- the particles and fine dusts separated in cyclone 20 are fed by means of line 24.
- the ore can be used elsewhere or it can be directly further processed in a cluster of production plants.
- the ore is fed into a melting furnace 50 via line 51 in which the ore is further purified.
- Exhaust gases which are produced here and originate either directly from the melting furnace 50 or also from a cooling downstream of the melting furnace 50 (not shown) can be fed into reactor 10 via a recycling gas line 60.
- stages for further processing the ore are imaginable from which either directly gas and/or cooling gas used in a corresponding cooling can be used as recycling gas or as constituent of the recycling gas.
- the melting furnace is cooled and via the same recycling gas line in its function as a heat carrier medium also heated gas is returned back into reactor 10.
- it is also imaginable to mix the recycling gas from recycling gas line 60 independently from its origin with the recycling gas from line 40.
- reactor 10 is designed as a fluidized bed reactor so that the recycling gas is used completely or partially as fluidization gas.
- a stationary fluidized bed and also a circulating fluid bed are possible.
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Inorganic Compounds Of Heavy Metals (AREA)
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
RS20201332A RS61023B1 (en) | 2016-03-24 | 2017-03-24 | Process and facility for thermal treatment of a sulfur-containing ore |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102016105574.3A DE102016105574A1 (en) | 2016-03-24 | 2016-03-24 | Method and device for the thermal treatment of a sulphurous ore |
PCT/EP2017/057087 WO2017162857A1 (en) | 2016-03-24 | 2017-03-24 | Process and facility for thermal treatment of a sulfur-containing ore |
Publications (2)
Publication Number | Publication Date |
---|---|
EP3433388A1 true EP3433388A1 (en) | 2019-01-30 |
EP3433388B1 EP3433388B1 (en) | 2020-08-19 |
Family
ID=58464512
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP17715066.1A Active EP3433388B1 (en) | 2016-03-24 | 2017-03-24 | Process and facility for thermal treatment of a sulfur-containing ore |
Country Status (10)
Country | Link |
---|---|
US (1) | US20190017143A1 (en) |
EP (1) | EP3433388B1 (en) |
CN (1) | CN108884514A (en) |
CA (1) | CA3018017C (en) |
CL (1) | CL2018002651A1 (en) |
DE (1) | DE102016105574A1 (en) |
EA (1) | EA201891921A1 (en) |
PL (1) | PL3433388T3 (en) |
RS (1) | RS61023B1 (en) |
WO (1) | WO2017162857A1 (en) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
HRP20230238T1 (en) * | 2020-06-30 | 2023-04-14 | Aura Technologie Gmbh | Method and device for recycling waste containing valuable metals |
Family Cites Families (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1974886A (en) * | 1931-12-15 | 1934-09-25 | Ici Ltd | Roasting of sulphide ores |
US2910348A (en) * | 1952-08-18 | 1959-10-27 | Duisburger Kupferhuette | Working up of sulfide iron ores |
US3351462A (en) * | 1965-01-29 | 1967-11-07 | Anaconda Co | Electric furnace smelting of copper concentrates |
GB1366712A (en) * | 1972-02-03 | 1974-09-11 | Simon Eng Dudley Ltd | Extraction of metals from ores |
DE2515464C2 (en) * | 1975-04-09 | 1977-03-31 | Kloeckner Humboldt Deutz Ag | METHOD AND DEVICE FOR THE PREVENTION OF SULFIDIC COPPER ORE CONCENTRATES |
SE8303184L (en) * | 1983-06-06 | 1984-12-07 | Boliden Ab | PROCEDURE FOR THE PREPARATION OF COPPER MELT MATERIALS AND SIMILAR MATERIALS CONTAINING HIGH CONTAINERS ARSENIK AND / OR ANTIMON |
DE69225993T2 (en) * | 1991-04-12 | 1998-12-10 | Metallgesellschaft Ag | Process for treating ore with recoverable metal materials, including arsenic-containing components |
DE19609284A1 (en) * | 1996-03-09 | 1997-09-11 | Metallgesellschaft Ag | Treating granular sulphidic ores containing gold and/or silver |
US5993514A (en) * | 1997-10-24 | 1999-11-30 | Dynatec Corporation | Process for upgrading copper sulphide residues containing nickel and iron |
DE10260735B4 (en) * | 2002-12-23 | 2005-07-14 | Outokumpu Oyj | Process and plant for heat treatment of sulfide ores |
DE102004009176B4 (en) * | 2004-02-25 | 2006-04-20 | Outokumpu Oyj | Process for the reduction of copper-containing solids in a fluidized bed |
DE102005008109A1 (en) | 2005-02-21 | 2006-08-24 | Outokumpu Technology Oy | Process and plant for the production of sulfuric acid |
DE102008033558A1 (en) * | 2008-07-11 | 2010-01-14 | Outotec Oyj | Process and plant for the production of calcine products |
-
2016
- 2016-03-24 DE DE102016105574.3A patent/DE102016105574A1/en not_active Withdrawn
-
2017
- 2017-03-24 CA CA3018017A patent/CA3018017C/en active Active
- 2017-03-24 EA EA201891921A patent/EA201891921A1/en unknown
- 2017-03-24 WO PCT/EP2017/057087 patent/WO2017162857A1/en active Application Filing
- 2017-03-24 CN CN201780018103.2A patent/CN108884514A/en active Pending
- 2017-03-24 PL PL17715066.1T patent/PL3433388T3/en unknown
- 2017-03-24 RS RS20201332A patent/RS61023B1/en unknown
- 2017-03-24 EP EP17715066.1A patent/EP3433388B1/en active Active
-
2018
- 2018-09-14 CL CL2018002651A patent/CL2018002651A1/en unknown
- 2018-09-17 US US16/133,057 patent/US20190017143A1/en not_active Abandoned
Also Published As
Publication number | Publication date |
---|---|
WO2017162857A1 (en) | 2017-09-28 |
CA3018017A1 (en) | 2017-09-28 |
CN108884514A (en) | 2018-11-23 |
DE102016105574A1 (en) | 2017-09-28 |
RS61023B1 (en) | 2020-12-31 |
EA201891921A1 (en) | 2019-03-29 |
EP3433388B1 (en) | 2020-08-19 |
CL2018002651A1 (en) | 2018-12-14 |
US20190017143A1 (en) | 2019-01-17 |
PL3433388T3 (en) | 2021-02-22 |
CA3018017C (en) | 2024-04-23 |
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