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WO1987003010A1 - Reacteur a lances dont la partie superieure est submergee et fonte directe de materiaux a base de sulfures de zinc a l'interieur dudit reacteur - Google Patents

Reacteur a lances dont la partie superieure est submergee et fonte directe de materiaux a base de sulfures de zinc a l'interieur dudit reacteur Download PDF

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Publication number
WO1987003010A1
WO1987003010A1 PCT/AU1986/000350 AU8600350W WO8703010A1 WO 1987003010 A1 WO1987003010 A1 WO 1987003010A1 AU 8600350 W AU8600350 W AU 8600350W WO 8703010 A1 WO8703010 A1 WO 8703010A1
Authority
WO
WIPO (PCT)
Prior art keywords
zone
zinc
slag
furnace
process according
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.)
Ceased
Application number
PCT/AU1986/000350
Other languages
English (en)
Inventor
John Millice Floyd
Brian William Lightfoot
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Outotec Ausmelt Pty Ltd
Original Assignee
Ausmelt Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Ausmelt Ltd filed Critical Ausmelt Ltd
Publication of WO1987003010A1 publication Critical patent/WO1987003010A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/04—Obtaining zinc by distilling
    • C22B19/16—Distilling vessels
    • 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
    • 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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/04—Obtaining zinc by distilling

Definitions

  • This invention relates to a furnace for smelting sulphide materials, and to a smelting process carried out therein.
  • the smelting of zinc concentrates has traditionally been carried out in a roast-reduction two stage process in which a roasting stage produces a solid calcine or sinter which is then fed to a reduction stage in which zinc is produced as a vapour and collected in a condenser.
  • the Imperial Smelting Process uses a blast furnace to smelt zinc sinter. Coke is used as both fuel and reductant in this process, and the gases pass into a lead splash condenser where zinc is collected at a low concentration in a stream of lead recirculating through a cooler where a zinc rich phase is • collected. This process suffers from the need to use expensive coke as both fuel and reductant and the feed materials and air must be preheated to high temperatures in order to ensure that reaction gases remain at high temperatures to avoid back oxidation of Zn to ZnO before reaching the condenser.
  • the present invention provides a novel apparatus comprising a furnace for smelting zinc sulphide material having a liquid slag layer and a gas space, and including an upwardly extending, preferably substantially vertical, fluid-cooled wall which extends into the slag layer and divides the gas space into a first and a second zone; each zone- having at least one top submerged lance extending downwardly, preferably substantially vertically, through the gas space, into the slag layer therein; and at least one flue gas offtake from each zone; the furnace being adapted to enable circulation and mixing of the slag between the two zones.
  • the oxidizing gas injected into the slag in the 20 first zone through, at least one top submerged lance may be air, air enriched with oxygen, or oxygen.
  • Fuel for example coal or natural gas may be injected together with the oxidizing gas.
  • Reductant for example coal or natural gas
  • a carrier gas is preferably an oxidizing gas which may be for example air, air enriched with oxygen or oxygen.
  • Zinc metal vapour removed from the second zone may 30 be recovered in a splash condenser.
  • lead fume produced in the first zone is separated from the flue gases and recycled to the slag in the first zone, thereby producing a lead bullion which is tapped from the furnace.
  • Fig. 1 is a diagrammatic representation of a cross-section of a furnace according to the invention
  • Fig. 2 is a sectional view on line II-II of Figure 1
  • Fig. 3 is a flow-sheet representing continuous sulphide smelting of low-lead zinc sulphide concentrate according to the invention.
  • Fig. 4 is a flow-sheet illustrating continuous sulphide smelting of high-lead zinc sulphide concentrate according to the invention.
  • FIGs 1 and 2 illustrate the relatively simple direct smelting system which we have devised for zinc sulphide containing feed material which overcomes the main problems of the ISP and retort processes.
  • the process uses a new system for a reactor 10, having a peripheral wall 12 which, in horizontal section as in Figure 2, is formed of two inter-connected penannular portions 13,14. Across the junction of portions 13,14 the interior of reactor 10 is divided by a liquid-cooled/ preferably water-cooled, wall 16 which separates two gas streams of two zones 17,18 of reactor 10 as shown in Figure 1. Coolant for wall 16 is supplied by a inlet pipe (not shown) and leaves via an outlet pipe (not shown).
  • oxidation zone 17 of the reactor 10 zinc concentrate feed is fed continuously into the reactor in dry powdered form, via at least one lance 20.
  • the feed may be wet, as with filter cake, and fed directly through the roof of the furnace by suitable means.
  • Air, or an oxygen-air mixture is blown into liquid slag bath 22 of oxidation zone 17, via such lance 20, at a suitable rate to oxidise all of the sulphides in the feed to oxides.
  • Any fuel requirements are supplied by coal injected into the bath with the air.
  • the air and oxygen and coal are injected through top submerged lances 20 so as to avoid the impingement of the reacting gases on a refractory lining of wall 12 or of hearth 24 of the furnace, and thus to limit the refractory erosion.
  • Smelting reactions in oxidation zone 17 produce a slag, of composition determined by the feed and flux material fed to the furnace and by the quantity of slag recirculating between oxidation zone 17 and the second, reduction zone 18.
  • Some volatile constituents of the feed such as lead, cadmium, arsenic and antimony can be volatilised in the smelting conditions in zone 17 to produce a fume, removed via offtake 26, which may contain most of these volatile materials; almost all of the zinc remaining in the slag.
  • This fume is collected in a baghouse or electrostatic precipitator before the gases, containing sulphur dioxide, are passed to a suitable conventional system for disposal or dispersal and thereby enable production of less impure, or substantially pure, zinc by reduction of the slag, depending on feed composition.
  • zone 18 at least one top submerged lance 30 is used to inject coal, with air or oxygen, to product strongly reducing conditions. These conditions result in reduction of ZnO dissolved in the slag to Zn vapour, which is condensed from flue gases removed via offtake 32. The flue gases then pass through conventional dust separation systems and are burnt to remove their CO and Km content before dispersal. This combustion can be usefully used to produce steam or generate electricity.
  • Slag is able to be tapped off from the reactor at intervals, through a tapping system 34.
  • Bullion or speiss which can also be produced, are able to be tapped at intervals through a tapping system 36.
  • the composition of the slag is controlled to produce a suitable viscosity at the operating temperature for any feed composition by the flux additions and the tapping frequency.
  • reactor 10 of Figure 1 is operated with a low- lead zinc sulphide feed from source 40 to produce all of the lead and other volatile constituents as fume, which is passed from oxidation zone 17 to dust collector 42 and treated separately for recovery of values.
  • the reduction zone 18 is operated under conditions of excess coal feeding as lump material fed to the slag surface, or as fine material injected down the lance, to generate a gas very rich in CO and H_ and containing low levels of CO- and H-O.
  • the zinc vapour in this gas is collected in a zinc condenser 44 to produce zinc for market. Gases from condenser 44 pass to dust collector 46, with solids from the latter being recycled to the line from source 40.
  • the reactor 10 of Figure 1 is operated with a high lead zinc sulphide feed from source 50.
  • the fume solids from collector 52 are recycled to oxidation zone 17 to force all the lead to report to the slag.
  • the lead in the slag is reduced to metal in the reducion zone 18 and is tapped off for refining.
  • the conditions in zone 18 are maintained just sufficiently reducing with injected coal to produce zinc as vapour which is collected in a lead splash condenser 54.
  • the lead may be maintained at about 525°C in the condenser 54 where its solubility for zinc is about 2.5%. It then recirculates to a cooling system 56 where liquid zinc with about 1.2% lead separates at about 425°C.
  • This example illustrates the operation of the process to produce high-grade zinc using the flow sheet as illustrated in Figure - 3.
  • Thirty-two tons per hour of zinc concentrate containing 63.0% zinc, 0.30% lead, 0.12% cadmium, 1.8% iron 0.40% Si0 2 , 0.90% CaO and 30.80% sulphur was injected together with 0.5 tph of silica flux, 2 tph fume, 3
  • Two lances 30 were used to inject 10 tph of fine coal and 48,000 Nm 3/h of air into the bath at zone 18.
  • This produced gas containing 20 tph zinc metal which passed to a lead splash condenser in which zinc and lead were dissolved in a spray of lead-zinc alloy.
  • the alloy produced flowed to a cooling and separating section where zinc with about 1.2% lead was collected.
  • the lead-zinc alloy was then recirculated to the splash condenser to take up more zinc.
  • the gases from the splash condenser passed through an electrostatic precipitator, a combustion chamber, and boiler and then were able to be dispersed as clean gas to the atmosphere through a stack.
  • Slag was tapped from system 34 at 4-hourly intervals from the reduction zone 18 of the furnace in batches of 6.4 tons of slag containing 2.8% zinc, 33.9% iron, 35.3% Si0 2 and 17.54% CaO.
  • the plant is small for its production rate because of the intense nature of smelting and reduction operations. This results in low fuel requirements because of the small heat losses. It also gives a reduction in capital costs and more easy control of emission.
  • Feed preparation for the processes is minimal so that the capital cost of the plant is low, operations are simple and there are savings in labour and maintenance costs and most ancillary feed materials can be fed to the reactor in an untreated form.
  • the process is flexible in that it can be used to treat a wide variety of feed-types without modification
  • the reactor is described as being formed of two sections of penannular form, between which a fluid cooled wall extends.
  • This arrangement in which the reactor has a horizontal section approximating a figure eight form, is highly useful as it facilitates the circulation of slag within, and between the oxidation and reduction zones under the action of solid and gaseous feed to each zone.
  • the reactor can be of other forms.
  • the reactor can be circular or elliptical in overall form, with similar benefit.
  • the reactor can be of square or rectangular section in overall form, although such forms provide less than optimum slag circulation.

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)

Abstract

Four (10) et procédé destinés à recueillir du zinc à partir de matériaux sulfurés. Le matériau à base de sulfure de zinc est, en même temps qu'un gaz oxydant, introduit par une lance (20) dans la première zone (17) des deux zones latéralement adjacentes (17, 18) formées par un espace de gaz à l'intérieur du four, ledit espace étant divisé par une paroi (16) refroidie par fluide s'étendant vers le haut dans une couche de laitier, ce qui produit de l'oxyde de zinc dissout dans le laitier et des oxydes de soufre évacués avec les gaz de fumée via la branche d'évacuation (26) des gaz de fumée. Les conditions permettant la circulation et le mélange du laitier entre les deux zones sont maintenues. Un agent de réduction est introduit dans la seconde zone (18) via une lance (30), afin de réduire l'oxyde de zinc en métal de zinc, lequel est vaporisé et évacué avec les gaz de fumée via la branche d'évacuation (32) des gaz de fumée.
PCT/AU1986/000350 1985-11-19 1986-11-19 Reacteur a lances dont la partie superieure est submergee et fonte directe de materiaux a base de sulfures de zinc a l'interieur dudit reacteur Ceased WO1987003010A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AUPH347385 1985-11-19
AUPH3473 1985-11-19

Publications (1)

Publication Number Publication Date
WO1987003010A1 true WO1987003010A1 (fr) 1987-05-21

Family

ID=3771377

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU1986/000350 Ceased WO1987003010A1 (fr) 1985-11-19 1986-11-19 Reacteur a lances dont la partie superieure est submergee et fonte directe de materiaux a base de sulfures de zinc a l'interieur dudit reacteur

Country Status (3)

Country Link
AU (1) AU592398B2 (fr)
CA (1) CA1308918C (fr)
WO (1) WO1987003010A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2234528A (en) * 1989-07-13 1991-02-06 Tolltreck International Limite Zinc recovery process
EP0427699A1 (fr) * 1989-11-10 1991-05-15 A. Ahlstrom Corporation Procédé et appareil pour le traitement de concentrés de zinc
FR2666592A1 (fr) * 1990-09-12 1992-03-13 Siderurgie Fse Inst Rech Dispositif d'extraction de metaux volatils, tels que le zinc et le plomb, sous forme d'oxydes a partir de dechets oxydes contenant du fer, et procede utilisant ce dispositif.
GB2251252A (en) * 1990-10-09 1992-07-01 Sumitomo Metal Mining Co Pyrometallurgical process for refining zinc sulfide concentrates
EP0489083A4 (fr) * 1989-08-24 1994-01-19 Ausmelt Pty. Ltd.
WO2020149777A1 (fr) * 2019-01-14 2020-07-23 Val'eas Recycling Solutions Ab Traitement d'un matériau à base de fer ferrique comprenant du zinc et du soufre

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IE904367A1 (en) * 1989-12-05 1991-06-05 Mount Isa Mines Zinc smelting

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB792846A (en) * 1954-07-26 1958-04-02 Eugene Warland Continuous method for reducing oxidic zinc ores indirectly by means of carbon and apparatus for carrying out the method
AU5605873A (en) * 1972-06-26 1974-11-28 Borax Consolidated Limited Improvements in or relating to zinc and lead smelting
US4141721A (en) * 1976-12-16 1979-02-27 Frolov Jury F Method and apparatus for complex continuous processing of polymetallic raw materials
AU5551386A (en) * 1985-04-03 1986-10-09 Cra Services Limited Smelting process

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB792846A (en) * 1954-07-26 1958-04-02 Eugene Warland Continuous method for reducing oxidic zinc ores indirectly by means of carbon and apparatus for carrying out the method
AU5605873A (en) * 1972-06-26 1974-11-28 Borax Consolidated Limited Improvements in or relating to zinc and lead smelting
US4141721A (en) * 1976-12-16 1979-02-27 Frolov Jury F Method and apparatus for complex continuous processing of polymetallic raw materials
AU5551386A (en) * 1985-04-03 1986-10-09 Cra Services Limited Smelting process

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2234528A (en) * 1989-07-13 1991-02-06 Tolltreck International Limite Zinc recovery process
EP0489083A4 (fr) * 1989-08-24 1994-01-19 Ausmelt Pty. Ltd.
EP0427699A1 (fr) * 1989-11-10 1991-05-15 A. Ahlstrom Corporation Procédé et appareil pour le traitement de concentrés de zinc
FR2666592A1 (fr) * 1990-09-12 1992-03-13 Siderurgie Fse Inst Rech Dispositif d'extraction de metaux volatils, tels que le zinc et le plomb, sous forme d'oxydes a partir de dechets oxydes contenant du fer, et procede utilisant ce dispositif.
GB2251252A (en) * 1990-10-09 1992-07-01 Sumitomo Metal Mining Co Pyrometallurgical process for refining zinc sulfide concentrates
US5178667A (en) * 1990-10-09 1993-01-12 Sumitomo Metal Mining Company Limited Dry process for refining zinc sulfide concentrates
GB2251252B (en) * 1990-10-09 1995-01-25 Sumitomo Metal Mining Co Pyrometallurgical process for refining mixtures of zinc sulfide and lead sulfide concentrates
WO2020149777A1 (fr) * 2019-01-14 2020-07-23 Val'eas Recycling Solutions Ab Traitement d'un matériau à base de fer ferrique comprenant du zinc et du soufre

Also Published As

Publication number Publication date
CA1308918C (fr) 1992-10-20
AU6731187A (en) 1987-06-02
AU592398B2 (en) 1990-01-11

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