[go: up one dir, main page]

EP1834000A1 - A method and use of an apparatus for recovery of metals or metal compounds - Google Patents

A method and use of an apparatus for recovery of metals or metal compounds

Info

Publication number
EP1834000A1
EP1834000A1 EP05792438A EP05792438A EP1834000A1 EP 1834000 A1 EP1834000 A1 EP 1834000A1 EP 05792438 A EP05792438 A EP 05792438A EP 05792438 A EP05792438 A EP 05792438A EP 1834000 A1 EP1834000 A1 EP 1834000A1
Authority
EP
European Patent Office
Prior art keywords
solid particles
burner
flame
metal
raw material
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.)
Withdrawn
Application number
EP05792438A
Other languages
German (de)
French (fr)
Inventor
Åke HOLMSTRÖM
Joachim VON SCHÉELE
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.)
Linde GmbH
Original Assignee
Linde GmbH
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 Linde GmbH filed Critical Linde GmbH
Publication of EP1834000A1 publication Critical patent/EP1834000A1/en
Withdrawn legal-status Critical Current

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
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/34—Obtaining zinc oxide
    • 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
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/02—Working-up flue dust
    • 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
    • C22B19/28—Obtaining zinc or zinc oxide from muffle furnace residues
    • 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
    • C22B19/30—Obtaining zinc or zinc oxide from metallic residues or scraps
    • 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
    • C22B5/00—General methods of reducing to metals
    • C22B5/02—Dry methods smelting of sulfides or formation of mattes
    • C22B5/16—Dry methods smelting of sulfides or formation of mattes with volatilisation or condensation of the metal being produced
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates generally to a method for calcining of metal-bearing solid particles or dust.
  • the invention also relates to the use of an apparatus for performing such a method.
  • wastes include but are not limited to electric arc furnace (EAF) steel dusts and foundry wastes as well as zinc-bearing feeds, includ- ing foundry dusts and sludges.
  • EAF electric arc furnace
  • FIG. 1 A prior art plant for metals recycling from steel- making and foundry wastes is described in the article "Metals recycling from steelmaking and foundry wastes by Horsehead resource development” published in 1992 Electric furnace conference proceedings, pages 145- 157.
  • This prior art plant is shown in Fig. 1.
  • the plant disclosed in this article comprises rotary kilns, which are arranged to heat the process mater ⁇ ials and thereby provide a recycling process.
  • This process includes two major steps.
  • the starting material such as a mixture of zinc bearing feed and coal or coke is fed to a first kiln and the starting material is divided into iron-rich material and dust.
  • the dust which is collected in a filter, comprises zinc oxide and other compounds and elements, such as salts, cadmium and lead.
  • calcining is generally meant the conversion of the physical or chemical properties of a substance by the application of heat.
  • An alternative process route to the prior art plant described above consists of liquid slag fuming as the first step and calcining in a rotary kiln as the second step.
  • a major drawback with the described recycling process is the fact that the rotary kilns are large and cumbersome to operate.
  • a rotary kiln described in the above mentioned article could be of a length of up to 100 meters and have a diameter of up to three meters. It is appreciated that a plant including rotary kilns of this kind is expensive to operate.
  • a further drawback is the fact that toxic compounds if present, such as dioxins, are evaporated by the process heat without being broken down. This is due to the limited process temperature of the counter current kiln based calcining process. Vaporized dioxins are then directed to the gas cleaning section of the plant or even the ambient atmosphere, thereby constituting a hazard to the environment.
  • the international publication WO01/86011 Al discloses a method for recovery of metals, wherein metallic fines are supplied to a flame of a burner (20) and the fines are brought to melt and to agglomerate. The agglomerated product is then recovered.
  • An object of the present invention is to provide a method for recovery of metals and metal compounds from metal-bearing solid particles in which the above- mentioned drawbacks with known techniques are avoided or at least mitigated. Another object is to provide a use of an apparatus for recovery of metals and metal compounds from metal-bearing solid particles.
  • the invention is based on the realization that metal- bearing solid particles can be fed directly through the flame of an oxy-fuel burner without melting the metal or metal compound to be recovered, i.e., the original shape and the state of aggregate of the solid particles are maintained.
  • the use of a burner in combination with feeding the solid particles directly into and through the burner flame makes it possible to control the heating process in such a way that the solid particles are left unmelted after having passed the burner flame.
  • the pro ⁇ blems of prior art are overcome or at least mitigated.
  • the heating process can be controlled in a satisfying way, avoid ⁇ ing melting of the metal-bearing solid particles supplied through the burner.
  • control of the process is further enhanced and the volume of the exhaust gas is minimized.
  • Fig. 1 is a schematic diagram of a prior art plant for recovery of metals from metal-bearing dust
  • Fig. 2 is a schematic diagram of an apparatus used with the inventive method
  • Fig. 3 is a sectional view of a burner used with the method according to the invention.
  • Fig. 4 is a cross-sectional view of the burner shown in figure 2;
  • Fig. 5 shows an alternative embodiment of an apparatus used with the inventive method.
  • the starting material such as a mixture of zinc bearing feed and coal or coke is divided into iron-rich material and zinc rich but contaminated dust.
  • the zinc rich dust calcined to a zinc rich product with low contents of impurities In the second kiln is the zinc rich dust calcined to a zinc rich product with low contents of impurities.
  • FIG. 2 an overall diagram of a plant for recovery and upgrading of metals and metal compounds, generally designated 10, is shown.
  • the term recovery is intended to encompass recovery with or without any further treatment of the resulting raw material.
  • the plant 10 is essentially identical to the plant described in the international patent publication WO 01/86011.
  • the plant is built around a burner 20 installed in a sidewall of a fur ⁇ nace 30.
  • the burner is a so-called oxy-fuel burner and is thus supplied with fuel, such as fuel oil, propane, natural gas, or butane through a first feeding line 21 and with oxygen through a second feeding line 22.
  • fuel such as fuel oil, propane, natural gas, or butane
  • oxygen is in this context meant a gas with an O 2 content exceeding 21% and preferably so-called technical oxygen having an O 2 content of 90-99.5%.
  • Metal-bearing dust or solid particles are supplied through a third feeding line 23.
  • EAF electric arc furnace
  • Waelz kiln dusts Waelz kiln dusts
  • slag fuming furnace dusts lead and copper plant dusts and foundry wastes
  • zinc- bearing feeds including foundry dusts.
  • both fines, normally meaning products resulting from crushing and sintering, and dust, normally meaning products collected in filters, are possible raw material for use with the inventive method as well as other equivalent materials, such as powder.
  • the metal-bearing solid particles also contain unwanted compounds, such as cadmium, lead, different salts, sodium chloride, potassium chloride, oxides, fluorides etc. It will be appreciated that the expression compounds are to include elements.
  • the burner 20 will be described in more detail below with reference to Figs. 3 and 4.
  • the third feeding line 23 is also connected to a feeder, generally designated 40.
  • the feeder 40 com ⁇ prises a silo 42, into which solid particles are fed.
  • the solid particles are directed from the silo 42 to a pressure vessel 44, from which they are further directed to the third feeding line 23 connected to the burner 20.
  • a desired supply rate of solid particles to the burner 20 is ensured.
  • the solid particles are intermixed in a fluid acting as bearer, thus creating a slurry that is fed to the burner 20.
  • the burner 20 will now be described in detail with reference to Figs. 3 and 4.
  • the burner 20 comprises a main portion 24, to which the three supply lines 21-23 shown in Fig. 2 are connected.
  • the portion 24 is pro ⁇ vided with an essentially circular cross-section, see Fig. 4, in which the configuration of the supply lines 21-23 appears in more detail.
  • Fuel is supplied through the first supply line 21 in the form of six equi- distant pipes 21a-f placed at a constant distance from the center axis of the main portion 24.
  • Oxygen is supplied through an annular outer portion 22 and thus surrounds the fuel supplied through the pipes 21a-f.
  • solid particles are supplied through the pipe 23, which is co-axially placed in the burner.
  • the burner 20 is mounted in the sidewall of the furnace 30.
  • the burner can be tilted, i.e., can be posi ⁇ tioned in different angles relative to the horizontal and the vertical.
  • the different orientations can be used for obtaining desired characteristics for the calcining process.
  • dust is supplied to the silo 42 of the feeder 40.
  • the dust used in the described process are metal-bearing solid particles.
  • the solid particles making up the dust normally have an overall diameter of less than approximately 5 millimeters, and preferably less than approximately 1 millimeter.
  • the dust fall from the silo and into the pressure ves ⁇ sel 44, wherein the pressure is maintained by means of a gas also functioning as a carrying gas, such as com- pressed air, oxygen, nitrogen or argon.
  • a gas also functioning as a carrying gas such as com- pressed air, oxygen, nitrogen or argon.
  • the dust is then carried to the oxy-fuel burner 20 at a rate, which is determined by the pressure level in the vessel 44, the amount of solid particles in the silo 42 etc.
  • the operation of the oxy-fuel burner 20 is controlled by means of the amount of fuel and oxygen supplied through the first and second supply lines 21 and 22, respectively.
  • the supply lines are connected to sources of fuel and oxygen (not shown), as is con ⁇ ventional.
  • Dust is supplied through the central feeding pipe 23 at a rate that is controlled by the feeder.
  • Fuel is supplied in the six fuel feeding pipes 21a-f, see Fig. 4, while an envelope of oxygen is supplied through the annular feeding area 22.
  • the oxy-fuel mixture results in a flame 25 having properties, such as length, tempera- ture etc., that are controlled by the supply rate of fuel and oxygen.
  • the dust is injected into the central portion of the flame 25.
  • the dust in ⁇ jected into and through the flame 25 is left unmelted by the heat of the flame, i.e., the original shape and state of aggregate of the solid particles are main- tained.
  • the solid particles remain in the flame for a very short time and under strictly controlled conditions.
  • the solid particles can remain in the flame for less than one second and more preferably less than one half second.
  • the heating of particles can be regulated so that — despite the high flame temperature - the particles are not melted but calcining is obtained.
  • the process is controlled by the ratio of solid particles supplied into the flame and the amount of fuel burnt.
  • the heating process is con ⁇ trolled by means of several parameters, of which can be mentioned: temperature and velocity of the flame 25, energy content or density of the injected solid particles, stochiometry, i.e., the ratio oxidizing gas to added fuel, the oxygen content of the oxidizing gas, the supply rate of oxygen and added fuel, the rate of injection of the dust and their character ⁇ istics, the travel time of the solid particles in the flame, and burner characteristics and configuration, such as tilting.
  • the heating of particles can be regulated so that the calcined solid particles, such as zinc oxide particles, fall to the bottom of the furnace 30, wherein they are added to the charge 34.
  • the particles can then be used as raw material for further processing.
  • the zinc oxide can be used as raw material for zinc.
  • the process is run stochiometrically or sub-stochiometrically.
  • the evaporated compounds leave the furnace 30 through one or more exhaust outlets (not shown) and are taken care of in some convenient way. It is believed that the inventive method using relatively high flame temperature breaks down some unwanted toxic compounds, such as dioxin, thereby preventing them from entering the ambient atmosphere.
  • the burner is posi ⁇ tioned in a sidewall of a furnace.
  • other suitable positions are possible, such as in the upper part of the furnace.
  • a con- figuration with more than one burner is also possible.
  • Fig. 5 yet an alternative embodiment is shown, wherein the burner 20 is provided in one end of a rotary kiln 30'.
  • an existing plant can be retrofitted with a burner at the inlet end of the kiln, providing a co-current process instead of the prior art counter-current process.
  • the solid particles are fed to the burner in the same way as in the embodiment described with reference to Fig. 2 but are transported away by the rotation of the kiln 30'.
  • the solid particles are fed to the furnace by means of a feeder.
  • the particles supplied to the furnace could also be free- flowing, carried by means of a feed gear etc.
  • a dry starting material has been shown in the figures.
  • a suitable feeding arrangement comprising a feed screw, for example.
  • the wet part is vaporized by the high temperature of the flame, resulting in exhausts rising through the furnace 30 and subsequently leaving through an exhaust outlet (not shown).

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Metallurgy (AREA)
  • Manufacturing & Machinery (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)

Abstract

A method for recovery of metals or metal compounds from metal-bearing solid particles comprising volatile compounds comprises supplying the solid particles (50) through a flame (25) of a burner (20). The volatile compounds are then evaporated by means of heat from the flame (25) while maintaining the original shape and state of aggregate of the solid particles, thereby providing a raw material product (34). The raw material product (34) is then recovered. By feeding the solid particles directly to the flame, a compact and efficient plant is provided. The melting process can be controlled in a satisfying way, avoiding melting of the metal-bearing solid particles supplied through the burner. The use of a burner is also described.

Description

A METHOD AND USE OF AN APPARATUS FOR RECOVERY OF METALS OR METAL COMPOUNDS
FIELD OF INVENTION The present invention relates generally to a method for calcining of metal-bearing solid particles or dust. The invention also relates to the use of an apparatus for performing such a method.
BACKGROUND Large amounts of environmentally troublesome indust¬ rial wastes are generated in different processes in metallurgic industry. Such wastes include but are not limited to electric arc furnace (EAF) steel dusts and foundry wastes as well as zinc-bearing feeds, includ- ing foundry dusts and sludges.
A prior art plant for metals recycling from steel- making and foundry wastes is described in the article "Metals recycling from steelmaking and foundry wastes by Horsehead resource development" published in 1992 Electric furnace conference proceedings, pages 145- 157. This prior art plant is shown in Fig. 1. The plant disclosed in this article comprises rotary kilns, which are arranged to heat the process mater¬ ials and thereby provide a recycling process. This process includes two major steps. In a first step the starting material, such as a mixture of zinc bearing feed and coal or coke is fed to a first kiln and the starting material is divided into iron-rich material and dust. The dust, which is collected in a filter, comprises zinc oxide and other compounds and elements, such as salts, cadmium and lead. These other compounds and elements are unwanted and the dust is fed in a second step to a second kiln and is there divided into zinc oxide and dust comprising the other compounds and elements, for example salts, cadmium and lead. This second step is referred to as the calcining step. By calcining is generally meant the conversion of the physical or chemical properties of a substance by the application of heat.
An alternative process route to the prior art plant described above consists of liquid slag fuming as the first step and calcining in a rotary kiln as the second step.
In both the first and the second step of the first described process route and the in the second step of the alternative process route, hot air and possibly oxygen is added to the processes. Also, in a rotary kiln a large part of the heating energy is transferred to the material from the lining of the rotary kiln, i.e., as indirect heating.
A major drawback with the described recycling process is the fact that the rotary kilns are large and cumbersome to operate. For example, a rotary kiln described in the above mentioned article could be of a length of up to 100 meters and have a diameter of up to three meters. It is appreciated that a plant including rotary kilns of this kind is expensive to operate.
Another drawback is the fact that the process time is rather long; the processed material is transported by means of gravity as the kiln rotates. This relatively long process creates a bottleneck in the total recovery process.
A further drawback is the fact that toxic compounds if present, such as dioxins, are evaporated by the process heat without being broken down. This is due to the limited process temperature of the counter current kiln based calcining process. Vaporized dioxins are then directed to the gas cleaning section of the plant or even the ambient atmosphere, thereby constituting a hazard to the environment.
It is thus appreciated that the handling and recovery of metal-bearing dusts and solid particles from such processes are often difficult and costly problems. The pressure from both public authorities and customers to find new solutions is constantly increasing.
Up to now no feasible alternative to the use of rotary kilns has been found for the process of calcining metal-bearing dusts wherein the recovered metal is obtained in solid form, i.e., wherein the recovered metal is not melted. It is however very difficult to combine an acceptable metallurgical result with an energy efficient and environmentally safe kiln process. Furthermore, due to the inherent low weight dust is easily carried away by the gas to be mixed with the exhaust from the furnace, thus lowering the yield and constituting an environmental hazard.
The international publication WO01/86011 Al discloses a method for recovery of metals, wherein metallic fines are supplied to a flame of a burner (20) and the fines are brought to melt and to agglomerate. The agglomerated product is then recovered.
SUMMARY OF THE INVENTION
An object of the present invention is to provide a method for recovery of metals and metal compounds from metal-bearing solid particles in which the above- mentioned drawbacks with known techniques are avoided or at least mitigated. Another object is to provide a use of an apparatus for recovery of metals and metal compounds from metal-bearing solid particles.
The invention is based on the realization that metal- bearing solid particles can be fed directly through the flame of an oxy-fuel burner without melting the metal or metal compound to be recovered, i.e., the original shape and the state of aggregate of the solid particles are maintained. The use of a burner in combination with feeding the solid particles directly into and through the burner flame makes it possible to control the heating process in such a way that the solid particles are left unmelted after having passed the burner flame.
According to a first aspect of the present invention there is provided a method for recovering of metals and metal compounds as defined in claim 1.
According to a second aspect of the present invention there is provided a use of an apparatus for recovering of metals and metal compounds as defined in claim 11.
With the method according to the invention, the pro¬ blems of prior art are overcome or at least mitigated. By feeding the solid particles directly to the flame, a compact and efficient plant is provided. The heating process can be controlled in a satisfying way, avoid¬ ing melting of the metal-bearing solid particles supplied through the burner.
In a preferred embodiment, by using an oxygen-enriched gas with a burner, the control of the process is further enhanced and the volume of the exhaust gas is minimized.
BRIEF DESCRIPTION OF DRAWINGS
The invention is now described, by way of example, with reference to the accompanying drawings, in which:
Fig. 1 is a schematic diagram of a prior art plant for recovery of metals from metal-bearing dust;
Fig. 2 is a schematic diagram of an apparatus used with the inventive method;
Fig. 3 is a sectional view of a burner used with the method according to the invention;
Fig. 4 is a cross-sectional view of the burner shown in figure 2; and
Fig. 5 shows an alternative embodiment of an apparatus used with the inventive method.
DETAILED DESCRIPTION OF THE INVENTION
In the following, a detailed description of the method and the apparatus according to the invention will be given. The expressions dust and solid particles will be used alternately in this description. By these expressions are to be understood particles in the solid state and having an overall diameter of approxi¬ mately 5 millimeters or below. Agglomerated products, i.e., sintered or compacted aggregates of fines, are here not included.
A prior art plant and a method of operating it have already been described with reference to Fig. 1. In the first kiln, the starting material, such as a mixture of zinc bearing feed and coal or coke is divided into iron-rich material and zinc rich but contaminated dust.
In the second kiln is the zinc rich dust calcined to a zinc rich product with low contents of impurities.
Starting with Fig. 2, an overall diagram of a plant for recovery and upgrading of metals and metal compounds, generally designated 10, is shown. In this context, the term recovery is intended to encompass recovery with or without any further treatment of the resulting raw material. The plant 10 is essentially identical to the plant described in the international patent publication WO 01/86011. The plant is built around a burner 20 installed in a sidewall of a fur¬ nace 30. The burner is a so-called oxy-fuel burner and is thus supplied with fuel, such as fuel oil, propane, natural gas, or butane through a first feeding line 21 and with oxygen through a second feeding line 22. By oxygen is in this context meant a gas with an O2 content exceeding 21% and preferably so-called technical oxygen having an O2 content of 90-99.5%. Metal-bearing dust or solid particles are supplied through a third feeding line 23. From the following description, it is clear that the inventive method is applicable to electric arc furnace (EAF) steel dusts, Waelz kiln dusts, slag fuming furnace dusts, lead and copper plant dusts and foundry wastes as well as zinc- bearing feeds, including foundry dusts. Thus, both fines, normally meaning products resulting from crushing and sintering, and dust, normally meaning products collected in filters, are possible raw material for use with the inventive method as well as other equivalent materials, such as powder.
The metal-bearing solid particles also contain unwanted compounds, such as cadmium, lead, different salts, sodium chloride, potassium chloride, oxides, fluorides etc. It will be appreciated that the expression compounds are to include elements.
The burner 20 will be described in more detail below with reference to Figs. 3 and 4.
The third feeding line 23 is also connected to a feeder, generally designated 40. The feeder 40 com¬ prises a silo 42, into which solid particles are fed. The solid particles are directed from the silo 42 to a pressure vessel 44, from which they are further directed to the third feeding line 23 connected to the burner 20. By means of this arrangement, a desired supply rate of solid particles to the burner 20 is ensured. In an alternative embodiment, the solid particles are intermixed in a fluid acting as bearer, thus creating a slurry that is fed to the burner 20.
In the bottom of the furnace there is gathered a charge 34 resulting from the material supplied to the furnace 30.
The burner 20 will now be described in detail with reference to Figs. 3 and 4. The burner 20 comprises a main portion 24, to which the three supply lines 21-23 shown in Fig. 2 are connected. The portion 24 is pro¬ vided with an essentially circular cross-section, see Fig. 4, in which the configuration of the supply lines 21-23 appears in more detail. Fuel is supplied through the first supply line 21 in the form of six equi- distant pipes 21a-f placed at a constant distance from the center axis of the main portion 24. Oxygen is supplied through an annular outer portion 22 and thus surrounds the fuel supplied through the pipes 21a-f. Finally, solid particles are supplied through the pipe 23, which is co-axially placed in the burner.
As already mentioned, the burner 20 is mounted in the sidewall of the furnace 30. In the preferred embodi¬ ment, the burner can be tilted, i.e., can be posi¬ tioned in different angles relative to the horizontal and the vertical. The different orientations can be used for obtaining desired characteristics for the calcining process.
In the following, the method for recovering metals and metal compounds will be described in detail. Initially, dust is supplied to the silo 42 of the feeder 40. The dust used in the described process are metal-bearing solid particles. The solid particles making up the dust normally have an overall diameter of less than approximately 5 millimeters, and preferably less than approximately 1 millimeter.
The dust fall from the silo and into the pressure ves¬ sel 44, wherein the pressure is maintained by means of a gas also functioning as a carrying gas, such as com- pressed air, oxygen, nitrogen or argon. By means of the pressure in the pressure vessel 44, the dust is then carried to the oxy-fuel burner 20 at a rate, which is determined by the pressure level in the vessel 44, the amount of solid particles in the silo 42 etc.
The operation of the oxy-fuel burner 20 is controlled by means of the amount of fuel and oxygen supplied through the first and second supply lines 21 and 22, respectively. The supply lines are connected to sources of fuel and oxygen (not shown), as is con¬ ventional.
The operation of the burner 20 will now be described in detail with reference to Figs. 3 and 4. Dust is supplied through the central feeding pipe 23 at a rate that is controlled by the feeder. Fuel is supplied in the six fuel feeding pipes 21a-f, see Fig. 4, while an envelope of oxygen is supplied through the annular feeding area 22. The oxy-fuel mixture results in a flame 25 having properties, such as length, tempera- ture etc., that are controlled by the supply rate of fuel and oxygen. The higher oxygen content, the higher temperature, resulting in a theoretical flame tempera¬ ture as high as 1900-2500°C and a flame velocity of 100 meters per second.
Thus, the dust is injected into the central portion of the flame 25. As is seen from Fig. 3, the dust in¬ jected into and through the flame 25 is left unmelted by the heat of the flame, i.e., the original shape and state of aggregate of the solid particles are main- tained. This is made possible by the fact that the solid particles remain in the flame for a very short time and under strictly controlled conditions. For example, the solid particles can remain in the flame for less than one second and more preferably less than one half second. Thus, the heating of particles can be regulated so that — despite the high flame temperature - the particles are not melted but calcining is obtained.
Basically, the process is controlled by the ratio of solid particles supplied into the flame and the amount of fuel burnt. However, the heating process is con¬ trolled by means of several parameters, of which can be mentioned: temperature and velocity of the flame 25, energy content or density of the injected solid particles, stochiometry, i.e., the ratio oxidizing gas to added fuel, the oxygen content of the oxidizing gas, the supply rate of oxygen and added fuel, the rate of injection of the dust and their character¬ istics, the travel time of the solid particles in the flame, and burner characteristics and configuration, such as tilting. Thus the heating of particles can be regulated so that the calcined solid particles, such as zinc oxide particles, fall to the bottom of the furnace 30, wherein they are added to the charge 34. The particles can then be used as raw material for further processing. For example, the zinc oxide can be used as raw material for zinc.
In the preferred embodiment, the process is run stochiometrically or sub-stochiometrically.
The evaporated compounds leave the furnace 30 through one or more exhaust outlets (not shown) and are taken care of in some convenient way. It is believed that the inventive method using relatively high flame temperature breaks down some unwanted toxic compounds, such as dioxin, thereby preventing them from entering the ambient atmosphere.
Preferred embodiments of the method and the use of an apparatus according to the invention have been de¬ scribed. The person skilled in the art realizes that these can be varied within the scope of the appended claims. Thus, although an oxy-fuel burner 20 has been shown, other equivalent burners, such as plasma burn¬ ers, can be used as long as desired oxygen levels exceeding 21% are obtained. Also oxy-fuel burners of other configurations than the disclosed one can be used, such as a burner with a different number of fuel pipes than six.
In the embodiment shown in Fig. 2, the burner is posi¬ tioned in a sidewall of a furnace. However, it is realized that other suitable positions are possible, such as in the upper part of the furnace. Also, a con- figuration with more than one burner is also possible. In Fig. 5, yet an alternative embodiment is shown, wherein the burner 20 is provided in one end of a rotary kiln 30'. In this way, an existing plant can be retrofitted with a burner at the inlet end of the kiln, providing a co-current process instead of the prior art counter-current process. The solid particles are fed to the burner in the same way as in the embodiment described with reference to Fig. 2 but are transported away by the rotation of the kiln 30'.
In the described embodiments, the solid particles are fed to the furnace by means of a feeder. However, the particles supplied to the furnace could also be free- flowing, carried by means of a feed gear etc.
A dry starting material has been shown in the figures. In the case the dust particles are intermixed in a liquid, such as water or sludge, a suitable feeding arrangement must be provided, comprising a feed screw, for example. Also, when arriving to the furnace, the wet part is vaporized by the high temperature of the flame, resulting in exhausts rising through the furnace 30 and subsequently leaving through an exhaust outlet (not shown).

Claims

1. A method for recovery of metals or metal compounds from metal-bearing solid particles comprising volatile compounds, the method comprising the following steps:
a) supplying the solid particles (50) through a flame (25) of a burner (20) ,
b) bringing the volatile compounds to evaporate by means of heat from the flame (25) while maintaining the original shape and state of aggregate of the solid particles, thereby providing a raw material product (34), and
c) recovering the raw material product (34).
2. The method according to claim 1, wherein the burner (20) is an oxy-fuel burner.
3. The method according to claim 1 or 2, wherein the burner is supplied with an oxidizing gas having an O2 content of at least 21% O2.
4. The method according to claim 3, wherein the burner is supplied with an oxidizing gas having an O2 content of at least 90% O2.
5. The method according to any of claims 1-4, wherein the solid particles (50) comprise zinc oxide.
6. The method according to any of claims 1-5, wherein the volatile elements are elements from the group comprising cadmium, lead, different salts, sodium chloride, potassium chloride, oxides, and fluorides.
7. The method according to any of claims 1-6, wherein the solid particles (50) have a diameter of less than approximately 5 millimeters, and more preferably a diameter of less than approximately 1 millimeter.
8. The method according to any of claims 1-7, wherein the calcining process of step b) is controlled by means of at least some of the following parameters: temperature and velocity of the flame (25), energy content or density of the solid particles, the ratio oxidizing gas to added fuel of the burner (20), the oxygen content of the oxidizing gas, the supply rate of oxygen and added fuel, the oxygen content in exhaust gas, the supply rate of the solid particles and their characteristics, the travel time of the solid particles in the flame, and burner characteristics and configuration, such as tilting.
9. The method according to any of claims 1-8, wherein step a) comprises supplying the solid particles (50) essentially to the central portion of the flame (25) .
10. The method according to any of claims 1-9, wherein the solid particles remain in the flame (25) for less than one second, and more preferably for less than one half second.
11. Use of an apparatus for recovery of metals and metal compounds from metal-bearing solid particles comprising volatile compounds, the apparatus comprising:
- a burner (20) having a flame (25) during operation thereof,
- a feeder (40) connected to the burner for supplying metal-bearing solid particles comprising volatile compounds through the flame (25) of the burner (20),
- a device (21,22) for controlling the flame (25) of the burner (20) so as to evaporate the volatile compounds by means of heat from the flame while maintaining the original shape and state of aggregate of the solid particles, thereby providing raw material product (34), and
- a device (30) for recovering the raw material product (34).
EP05792438A 2004-10-12 2005-10-11 A method and use of an apparatus for recovery of metals or metal compounds Withdrawn EP1834000A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE0402467A SE0402467D0 (en) 2004-10-12 2004-10-12 A method and use of an apparatus for calcining
PCT/SE2005/001506 WO2006041394A1 (en) 2004-10-12 2005-10-11 A method and use of an apparatus for recovery of metals or metal compounds

Publications (1)

Publication Number Publication Date
EP1834000A1 true EP1834000A1 (en) 2007-09-19

Family

ID=33434238

Family Applications (1)

Application Number Title Priority Date Filing Date
EP05792438A Withdrawn EP1834000A1 (en) 2004-10-12 2005-10-11 A method and use of an apparatus for recovery of metals or metal compounds

Country Status (9)

Country Link
US (1) US20070215019A1 (en)
EP (1) EP1834000A1 (en)
KR (1) KR20070060127A (en)
BR (1) BRPI0515963A (en)
CA (1) CA2580648A1 (en)
NO (1) NO20072458L (en)
SE (1) SE0402467D0 (en)
WO (1) WO2006041394A1 (en)
ZA (1) ZA200702043B (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2010114611A (en) 2007-09-14 2011-10-20 Баррик Гольд Корпорейшн (CA) METHOD OF RESTORING PLATINUM METALS USING REDUCERS
BR112015007715A2 (en) * 2012-10-08 2017-07-04 Air Liquide process and apparatus for improving the combustion of a secondary fuel in a rotary kiln

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB265558A (en) * 1926-02-04 1927-06-09 Krupp Fried Grusonwerk Ag Improvements in or relating to processes for the treatment of zinciferous flue dust
DE551366C (en) * 1930-11-26 1932-05-30 Fried Krupp Grusonwerk Akt Ges Process for the afterburning of exhaust gases from metallurgical processes
US3979205A (en) * 1971-04-07 1976-09-07 Wanzenberg Fritz Walter Metal recovery method
US4551313A (en) * 1984-02-27 1985-11-05 Amax Inc. Flash sublimation and purification of molybdenum oxide
US4643110A (en) * 1986-07-07 1987-02-17 Enron, Inc. Direct fuel-fired furnace arrangement for the recovery of gallium and germanium from coal fly ash
DE4009671A1 (en) * 1990-03-26 1991-10-02 Dinda Kickdown Gmbh Disposing of waste contg. heavy metals, esp. sewage sludge etc. - by high temp. combustion in admixture with quinoline giving prod. used as substitute for heavy metal ore
GB9316437D0 (en) * 1993-08-06 1993-09-22 Harcros Chemicals Uk Limited Zinc oxide and a process for making it
DE69520259T2 (en) * 1994-12-08 2001-08-09 Daido Tokushuko K.K., Nagoya Process and furnace for the disposal of steel mill waste and operating methods for this furnace
JPH09310126A (en) * 1996-05-16 1997-12-02 Daido Steel Co Ltd Method for producing metal from metal oxide
SE518531C2 (en) * 2000-05-05 2002-10-22 Aga Ab Methods for recycling metals
SE522953C2 (en) * 2001-02-22 2004-03-16 Aga Ab Method and apparatus for treating sludge by means of a burner
DE10212680A1 (en) * 2002-03-22 2003-10-09 Degussa Nanoscale zinc oxide, process for its production and use
US20040050207A1 (en) * 2002-07-17 2004-03-18 Wooldridge Margaret S. Gas phase synthesis of nanoparticles in a multi-element diffusion flame burner

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2006041394A1 *

Also Published As

Publication number Publication date
NO20072458L (en) 2007-05-14
WO2006041394A1 (en) 2006-04-20
SE0402467D0 (en) 2004-10-12
US20070215019A1 (en) 2007-09-20
KR20070060127A (en) 2007-06-12
BRPI0515963A (en) 2008-08-12
ZA200702043B (en) 2008-09-25
CA2580648A1 (en) 2006-04-20

Similar Documents

Publication Publication Date Title
CN104105802B (en) base metal recycling
WO1999016913A1 (en) Rotary hearth furnace for reducing oxides, and method of operating the furnace
JP2010111941A (en) Method for producing ferrovanadium
CN109652653A (en) A kind of inorganic dangerous waste system process
CZ301924B6 (en) Refining technology of and a device for treating metalline zinc-containing waste in revolving furnace
CN109306407A (en) A kind of device and method that metallurgy dedusting ash containing zinc is administered and utilized
WO2009114155A2 (en) Feed material compostion and handling in a channel induction furnace
KR19990008192A (en) Method for recovering metal from iron oxide containing mass
US6989043B2 (en) Method and an apparatus for recovery of metals
WO2009114157A2 (en) Feed material compostion and handling in a channel induction furnace
EP4062117B1 (en) Improved plasma induced fuming furnace
AU2001260856A1 (en) A method and an apparatus for recovery of metals
WO2009114156A2 (en) Feed material compostion and handling in a channel induction furnace
WO2009114159A2 (en) Feed material compostion and handling in a channel induction furnace
EP1834000A1 (en) A method and use of an apparatus for recovery of metals or metal compounds
CN209292440U (en) A kind of device that metallurgy dedusting ash containing zinc is administered and utilized
JP3508072B2 (en) Method and apparatus for producing massive artificial aggregate for concrete
JP3451901B2 (en) Operating method of mobile hearth furnace
WO2013156832A1 (en) Pyrometallurgical treatment of slags
JP2004090004A (en) Industrial waste treatment plant
WO2009114160A2 (en) Feed material compostion and handling in a channel induction furnace
WO2011002467A1 (en) Slag control in a channel induction furnace

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

17P Request for examination filed

Effective date: 20070315

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR

RIN1 Information on inventor provided before grant (corrected)

Inventor name: HOLMSTROEM, AKE

Inventor name: VON SCHEELE, JOACHIM

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: LINDE AKTIENGESELLSCHAFT

DAX Request for extension of the european patent (deleted)
RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: LINDE AG

17Q First examination report despatched

Effective date: 20091109

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20110621