EP0530893A1 - Procédé pour la fusion de plomb métallique en continu - Google Patents
Procédé pour la fusion de plomb métallique en continu Download PDFInfo
- Publication number
- EP0530893A1 EP0530893A1 EP92202548A EP92202548A EP0530893A1 EP 0530893 A1 EP0530893 A1 EP 0530893A1 EP 92202548 A EP92202548 A EP 92202548A EP 92202548 A EP92202548 A EP 92202548A EP 0530893 A1 EP0530893 A1 EP 0530893A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- lead
- slag
- phase
- primary
- oxygen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
- C22B13/00—Obtaining lead
- C22B13/02—Obtaining lead by dry processes
Definitions
- the invention relates to a process for the continuous melting of metallic lead from precious metal-containing and lead-containing precursors.
- Lead ores practically always contain silver and in many cases gold and platinum. Precious metals can also be contained in lead-containing intermediates or waste. In the pyrometallurgical extraction of lead, the precious metals go into the lead. After refining to remove copper, nickel, cobalt, tin, arsenic and antimony, the removal and extraction of the noble metals from the pre-refined lead lead is generally carried out using the Parkes process. An excess of zinc is introduced into the liquid lead and by cooling silver-zinc-lead mixed crystals are separated out, which are skimmed off as so-called foams or crusts from the lead bath. These foams also contain the other precious metals.
- the excess zinc present in the desilvered lead is removed either by the Harris method by adding NaOH, by the Betterton method by chlorination or by vacuum dezincification.
- the zinc is mechanically adhered to the foams by pressing or segregation and the zinc is removed by distillation and the so-called rich lead is produced, which contains the precious metals in high concentration.
- the rich lead which can contain up to about 50% silver
- the lead is oxidized to PbO in the so-called propellant process by selective oxidation with air and drawn off as a liquid smoothness, leaving behind the silver or Güldisch silver.
- the Güldisch silver is then subjected to refining electrolysis.
- the gold and platinum content in the lead is higher, the gold and platinum content before the actual one can be added by adding small amounts of zinc Desilvering can be enriched in a gold foam that contains little silver. This gold foam is then processed separately to Güldisch silver. In the usual desilvering, the entire lead must be subjected to the process described.
- a method for lead extraction in which a mixture of oxidic and sulfidic lead compounds in a first stage in a moving furnace, e.g. a rotary kiln is melted down, whereby in addition to primary lead, a high-lead-containing slag is formed, which contains the lead partly as oxide and partly as silicate. Lead and slag are withdrawn from the first stage, the slag being extracted in pieces. In a second stage, the slag is melted in a shaft furnace to reduce it, resulting in a low-lead slag and secondary lead. Precious metals in the feed go into the primary lead almost quantitatively.
- Part of the primary lead obtained in the first stage can be oxidized again and form the feed for the first stage as an oxidic component with fresh amounts of sulfidic ore.
- the silver contained in the primary lead is enriched in a small amount of lead so that it can be directly subjected to the driving process.
- This process relates to a batch process in which the slag tapped from the first stage has to be melted down again in the second stage.
- the lead tapped from the first stage must be oxidized to produce a lead worthy of driving.
- a method for processing lead, copper and sulfur containing materials in two separate stages is known, a copper stone phase and a lead containing primary lead phase being formed in the first stage.
- the separated slag phase is reduced in a second stage, with low-lead slag and secondary lead and possibly a cobalt-containing arsenic alloy.
- Both stages can be carried out in shaft furnaces, flame furnaces, short drum furnaces, head-blown rotary converters or bottom-blown tilting converters.
- Arc resistance furnaces are specified as advantageous units.
- Most of the leading silver is accumulated in the first stage in the primary lead and in the copper stone.
- the lead content of the slag in the first stage is set at 20 to 40%.
- the silver content of the lead is largely in the copper stone and the primary lead.
- the silver content of the primary lead is less than 1%, so that the primary lead must be subjected to the usual refining in order to obtain the silver.
- this process is only intended for copper-rich lead materials.
- the precursors can be in any form, for example as oxides, sulfides, sulfates, silicates.
- Metallic precursors such as computer scrap can also be added or used, in which case additives for slag formation may have to be added.
- the precursors do not contain any fuel, for example in sulfidic form, or if their fuel content is insufficient to cover the heat requirement in the oxidation zone, the required fuel is added to the oxidation zone in solid, gaseous or liquid form.
- the fuel can be added by means of nozzles from below or laterally into the melt and / or into the gas space or with the raw material mixture.
- the metal phases in the oxidation zone and the reduction zone are separated from one another by a partition arranged on the bottom of the reactor.
- the slag flows out of the oxidation zone via this partition or through an opening in the partition into the reduction zone.
- the gas spaces of the oxidation and reduction zones can be separated from one another or the gas from the reduction zone flows into the oxidation zone and is used there for after-combustion to cover the heat.
- gases containing oxygen are blown into the lead phase from below or from the side.
- the partial pressure of oxygen in the oxidation zone is set so that only the desired amount of primary lead is obtained from the lead amount and the remaining lead content is driven into the slag as oxide. When starting up, a corresponding rich lead with the desired silver content can be presented, then the oxygen partial pressure required for continuous operation can be set directly.
- an oxygen partial pressure must first be used, in which the lead is enriched with silver to the desired value and little or no primary lead is obtained. To When the desired concentration is reached, the oxygen partial pressure is then set to the value for continuous operation. The oxygen partial pressure is adjusted by regulating the ratio of the amount of oxygen blown in to the amount of the oxidizable constituents contained in the precursors. If fuels are blown into the melt, these must be taken into account. Oxygen, oxygen-enriched air or air can be used as the oxygen-containing gases. By precisely controlling the oxygen partial pressure, the silver content in the primary lead can be increased to such an extent that, for example, Güldischsilver is obtained with a high silver content in the primary materials.
- the secondary lead phase is located under the slag phase in the reduction zone.
- the reducing agent is blown into the lead phase from below or from the side and flows from there into the slag phase and then into the free reactor space.
- Carbon-containing solid, liquid or gaseous materials are used as reducing agents. They are blown in with oxygen-containing gases and at least partially converted to CO and possibly H2 in the lead phase, so that a reducing gas from the lead phase enters the slag phase.
- the combustible components can be post-burned in the escaping gas. If necessary, fuel is burned in the gas space of the reduction zone to cover the heat requirement.
- the advantage of the method of operation according to the invention is that no classical enrichment by adding zinc, Seigers and distillation is required to remove the precious metals from the lead, but the primary lead can be used directly in the driving work. in addition, there is only a very small amount of precious metal in the cycle and / or intermediate products.
- the secondary lead in the reduction zone is largely free of precious metals and does not require desilvering.
- a preferred embodiment consists in that, according to c), the oxygen partial pressure in the oxidation zone is controlled in such a way that the molten primary lead has a silver content of at least 50% and the amount of primary lead is less than 5% of the leading lead content. This makes the extraction of precious metals from the primary lead particularly economical.
- the starting materials used contain sulfidic lead materials.
- Sulfidic lead materials are primarily lead ore concentrates. They are processed according to the QSL procedure, e.g. in U.S. Patent 4,266,971 and U.S. Patent 4,895,595. Other materials containing precious metals can be added to the lead ore.
- the fuel required in the form of sulfide sulfur is already contained in the feedstock in a very uniform distribution, so that very good operating conditions result.
- a preferred embodiment is that in the reduction zone carbon-containing reducing agents and oxygen-containing gases are blown into the secondary lead phase by means of nozzles and a level of the lead phase is set which converts the reducing agent to CO and possibly H2 of at least 50% in the lead phase before Entry into the slag phase causes.
- the amount of oxygen introduced in the oxygen-containing gases is such that the reducing agent in the lead phase is converted to CO and possibly H2 in the desired percentage.
- the education of H2 takes place when using hydrocarbons or through the implementation of volatile constituents contained in the coal.
- the height of the lead phase required for the desired implementation of the reducing agent in the lead phase depends on the type of reducing agent and the oxygen-containing gas, the temperature of the lead phase and the strength and speed of the injection jets.
- the required height can, however, be determined relatively easily empirically for each operating case.
- a protective gas can be blown in as a jacket gas in multi-component nozzles.
- the resulting CO and H2-containing reducing gas is simultaneously heated up in the metal layer and accordingly occurs at high temperature in the slag, creating very good reduction conditions.
- this favors a further conversion to CO and H2 in the slag layer. This ensures that, despite the high lead oxide content of the slag entering the reduction zone, a low-lead slag is generated in the reduction zone.
- the height of the lead phase above floor-blowing nozzles is at least 4 cm and is preferably above 20 cm.
- the QSL reactor has a length of 33 m, an inner diameter of 3 m in the oxidation zone and 2.5 m in the reduction zone.
- a weir is arranged between the oxidation zone and the reduction zone, which mixes the lead phases of the oxidation and reduction zones prevented, but allows the high lead-containing slag to flow out of the oxidation zone into the reduction zone.
- the reactor is equipped with six bottom-blowing nozzles in the oxidation zone and five in the reduction zone.
- Technically pure oxygen is blown into the oxidation zone. Fine-grained coal, technically pure oxygen and nitrogen or natural gas or mixtures as a protective gas for the nozzles are blown into the reduction zone.
- Secondary lead and slag are alternately tapped from the reduction zone, whereby a lead bath of approx. 250 mm is maintained.
- the primary lead or rich lead is continuously withdrawn from the oxidation zone.
- the exhaust gas from the oxidation zone and the reduction zone is drawn off together on the side of the lead of the oxidation zone.
- Approx. 25 t / h of a feed mixture with 10% Ag, 40% Pb and the rest of the slag components are charged onto the slag layer in the oxidation zone.
- the oxygen potential in the oxidation zone is adjusted by adjusting the amount of oxygen blown in so that 10% of the lead lead is obtained as the primary lead and about 99% of the silver lead is collected in this primary lead.
- a rich lead or raw silver with about 70% Ag is generated in the oxidation zone and drawn off from it.
- the low-silver secondary lead with a silver content of approximately 0.01 to 0.02% and the slag are drawn off from the reduction zone.
- the feed mixture corresponds to Example 1.
- the oxygen potential in the oxidation zone is set so that 5% of the lead flow as primary lead accumulate and about 99% of the silver lead is collected in the primary lead. A rich lead or raw silver with about 83% Ag is produced.
- Approx. 25 t / h of a feed mixture with 1% Ag, 40% Pb and the rest of the slag components are fed into the oxidation zone.
- the oxygen potential is adjusted in such a way that about 10% of the lead flow is obtained as primary lead and about 99% of the silver lead is collected in this primary lead.
- a rich lead with about 20% Ag is generated in the oxidation zone and drawn off from it.
- the low-silver secondary lead with a silver content of approximately 0.01% and the slag are drawn off from the reduction zone.
- the feed mixture corresponds to example 3.
- the oxygen potential in the oxidation zone is set so that 5% of the lead lead is obtained as the primary lead and about 99% of the silver lead is collected in the primary lead. A rich lead with about 32% Ag is produced.
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE4129475 | 1991-09-05 | ||
DE4129475A DE4129475A1 (de) | 1991-09-05 | 1991-09-05 | Verfahren zum kontinuierlichen erschmelzen von metallischem blei |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0530893A1 true EP0530893A1 (fr) | 1993-03-10 |
EP0530893B1 EP0530893B1 (fr) | 1995-11-08 |
Family
ID=6439879
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP92202548A Expired - Lifetime EP0530893B1 (fr) | 1991-09-05 | 1992-08-20 | Procédé pour la fusion de plomb métallique en continu |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0530893B1 (fr) |
DE (2) | DE4129475A1 (fr) |
ES (1) | ES2081034T3 (fr) |
GR (1) | GR3018515T3 (fr) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101200777B (zh) * | 2007-09-24 | 2010-06-16 | 云南锡业集团(控股)有限责任公司 | 硫化铅精矿连续冶炼的方法及设备 |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN110804701A (zh) * | 2019-12-06 | 2020-02-18 | 湖北大江环保科技股份有限公司 | 侧吹转炉过饱和富氧熔炼工艺 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2739963A1 (de) * | 1976-09-06 | 1978-03-09 | Metallurgie Hoboken | Verfahren zur behandlung von blei- kupfer-schwefel-beschickungen |
EP0045531A1 (fr) * | 1980-08-06 | 1982-02-10 | Metallgesellschaft Ag | Procédé de fusion directe en continu de plomb métallique à partir de concentrés sulfureux plombifères |
DE3539164C1 (en) * | 1985-11-05 | 1987-04-23 | Kloeckner Humboldt Deutz Ag | Process and smelting furnace for producing non-ferrous metals |
US4741770A (en) * | 1985-04-03 | 1988-05-03 | Cra Services Limited | Zinc smelting process using oxidation zone and reduction zone |
-
1991
- 1991-09-05 DE DE4129475A patent/DE4129475A1/de not_active Withdrawn
-
1992
- 1992-08-20 DE DE59204246T patent/DE59204246D1/de not_active Expired - Fee Related
- 1992-08-20 EP EP92202548A patent/EP0530893B1/fr not_active Expired - Lifetime
- 1992-08-20 ES ES92202548T patent/ES2081034T3/es not_active Expired - Lifetime
-
1995
- 1995-12-21 GR GR950403647T patent/GR3018515T3/el unknown
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2739963A1 (de) * | 1976-09-06 | 1978-03-09 | Metallurgie Hoboken | Verfahren zur behandlung von blei- kupfer-schwefel-beschickungen |
EP0045531A1 (fr) * | 1980-08-06 | 1982-02-10 | Metallgesellschaft Ag | Procédé de fusion directe en continu de plomb métallique à partir de concentrés sulfureux plombifères |
US4741770A (en) * | 1985-04-03 | 1988-05-03 | Cra Services Limited | Zinc smelting process using oxidation zone and reduction zone |
DE3539164C1 (en) * | 1985-11-05 | 1987-04-23 | Kloeckner Humboldt Deutz Ag | Process and smelting furnace for producing non-ferrous metals |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101200777B (zh) * | 2007-09-24 | 2010-06-16 | 云南锡业集团(控股)有限责任公司 | 硫化铅精矿连续冶炼的方法及设备 |
Also Published As
Publication number | Publication date |
---|---|
DE4129475A1 (de) | 1993-03-11 |
ES2081034T3 (es) | 1996-02-16 |
GR3018515T3 (en) | 1996-03-31 |
DE59204246D1 (de) | 1995-12-14 |
EP0530893B1 (fr) | 1995-11-08 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DE3415813C2 (fr) | ||
DE2417978C3 (de) | Verfahren zur kontinuierlichen Gewinnung von Kupfer, Nickel, Kobalt und Blei oder deren Mischunggen aus ihren Sulfidkonzentraten | |
DE3042222C2 (de) | Verfahren zur Reduktion von feinkörnigen, unter anderem Eisenoxide enthaltenden Metalloxiden unter Gewinnung von bei der Temperatur der Eisenschmelze flüchtigen Metallen | |
DE2710970C2 (de) | Verfahren zur Gewinnung von Roh- bzw. Blasenkupfer aus sulfidischem Kupferrohmaterial | |
DE2739963C2 (fr) | ||
DE112007001820B4 (de) | Bleischlackenreduzierung | |
DE2521830A1 (de) | Verfahren und vorrichtung zur thermischen raffination von stark verunreinigtem kupfer in schmelzfluessiger phase | |
DE3611159C2 (fr) | ||
EP0171845B1 (fr) | Procédé et appareillage de traitement pyrométallurgique d'une matte plomb-cuivre en continu | |
EP0530893B1 (fr) | Procédé pour la fusion de plomb métallique en continu | |
EP0045531B1 (fr) | Procédé de fusion directe en continu de plomb métallique à partir de concentrés sulfureux plombifères | |
EP0508501B1 (fr) | Procédé pour la réduction des oxydes de métaux non-ferreux dans des laitiers | |
DE3115502C2 (fr) | ||
DE2645585A1 (de) | Verfahren zur freisetzung von wertmetallinhalten aus schlacken durch aufblasen | |
DE2320548B2 (de) | Verfahren zum Verhütten von Blei | |
DE3920522A1 (de) | Aggregat zur gewinnung von metallischem blei aus sulfidischen bleikonzentraten | |
DE1280479B (de) | Schmelzofen zur kontinuierlichen Herstellung von Spurstein und Verfahren zu seinem Betrieb | |
DE2707578A1 (de) | Verfahren zur gewinnung von rohkupfer aus kupfererzen oder -konzentraten, welche schaedliche oder wirtschaftlich bedeutsame mengen an anderen nichteisenmetallen enthalten | |
DE3304884A1 (de) | Verfahren zur gewinnung von blei aus bleiglanz (bleisulfid) | |
DE589738C (de) | Verfahren zur Gewinnung von Blei, Antimon oder Wismut | |
DE2019019A1 (de) | Verfahren zur Abtrennung und Anreicherung von Zinn aus zinnhaltigen Schlacken, Konzentraten und dgl | |
DE3207026A1 (de) | Verfahren zur konzentrierung oder gewinnung von nichteisenmetallen | |
DE3009934C2 (fr) | ||
DE216653C (fr) | ||
DE590505C (de) | Verfahren zur Gewinnung von Blei, Antimon oder Wismut |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): BE DE ES FR GB GR IT SE |
|
17P | Request for examination filed |
Effective date: 19930513 |
|
17Q | First examination report despatched |
Effective date: 19950327 |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): BE DE ES FR GB GR IT SE |
|
REF | Corresponds to: |
Ref document number: 59204246 Country of ref document: DE Date of ref document: 19951214 |
|
ET | Fr: translation filed | ||
ITF | It: translation for a ep patent filed |
Owner name: STUDIO JAUMANN |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2081034 Country of ref document: ES Kind code of ref document: T3 |
|
REG | Reference to a national code |
Ref country code: GR Ref legal event code: FG4A Free format text: 3018515 |
|
GBT | Gb: translation of ep patent filed (gb section 77(6)(a)/1977) |
Effective date: 19960217 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: BE Payment date: 19960829 Year of fee payment: 5 |
|
PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: FR Payment date: 19960923 Year of fee payment: 5 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GB Payment date: 19960924 Year of fee payment: 5 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: SE Payment date: 19960925 Year of fee payment: 5 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: ES Payment date: 19960930 Year of fee payment: 5 |
|
26N | No opposition filed | ||
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GR Payment date: 19961031 Year of fee payment: 5 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 19970820 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: SE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 19970821 Ref country code: ES Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 19970821 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 19970831 Ref country code: BE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 19970831 |
|
BERE | Be: lapsed |
Owner name: METALLGESELLSCHAFT A.G. Effective date: 19970831 |
|
GBPC | Gb: european patent ceased through non-payment of renewal fee |
Effective date: 19970820 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: FR Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 19980430 |
|
EUG | Se: european patent has lapsed |
Ref document number: 92202548.1 |
|
REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20000121 Year of fee payment: 8 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES Effective date: 20010501 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 19980910 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED. Effective date: 20050820 |