CA1327274C - Method of recovering metals and metal alloys and a plant therefor - Google Patents
Method of recovering metals and metal alloys and a plant thereforInfo
- Publication number
- CA1327274C CA1327274C CA000550403A CA550403A CA1327274C CA 1327274 C CA1327274 C CA 1327274C CA 000550403 A CA000550403 A CA 000550403A CA 550403 A CA550403 A CA 550403A CA 1327274 C CA1327274 C CA 1327274C
- Authority
- CA
- Canada
- Prior art keywords
- coal
- oxygen
- static
- bed layer
- metal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
- C21B13/0013—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state introduction of iron oxide into a bath of molten iron containing a carbon reductant
- C21B13/002—Reduction of iron ores by passing through a heated column of carbon
-
- 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
- C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
Abstract
ABSTRACT OF THE DISCLOSURE:
Disclosed is a method for recovering a metal or metal alloy, in particular a ferro-alloy, by reduction of a metal oxide in a reduction zone formed by a coal bed by passing a reducing gas through the reduction zone. To obtain a metal that has a high affinity of oxygen, lumpy oxidic charging material is guided under the action of gravity through the coal bed consisting of three static bed layers, wherein a bottom layer of degassed coal covering a liquid sump of reduced metal and slag is provided. Furthermore, oxygen or an oxygen-containing gas is fed into a middle layer to form a hot reducing gas consisting essentially of CO, and combustion gases of carbon particles and oxygen or oxygen-containing gas are fed into a top layer.
Disclosed is a method for recovering a metal or metal alloy, in particular a ferro-alloy, by reduction of a metal oxide in a reduction zone formed by a coal bed by passing a reducing gas through the reduction zone. To obtain a metal that has a high affinity of oxygen, lumpy oxidic charging material is guided under the action of gravity through the coal bed consisting of three static bed layers, wherein a bottom layer of degassed coal covering a liquid sump of reduced metal and slag is provided. Furthermore, oxygen or an oxygen-containing gas is fed into a middle layer to form a hot reducing gas consisting essentially of CO, and combustion gases of carbon particles and oxygen or oxygen-containing gas are fed into a top layer.
Description
~32~27~
The invention relates to a method of recovering metals or metal alloys, in particular ferro-alloys, by reducing metal oxides in a reduction zone formed by a coal bed flowed through by a reducing gas, as well as a plant for carrying out the method.
` In EP-A - 0 174 291 a method of melting metals, i.e.
copper, lead, zinc, nickel, cobalt and tin, of oxidic fine-grain non-ferrous metal ores is described, wherein the charging material is charged into a reduction zone formed by a coal fluidized layer in a meltdown gasifier. When passing this reduction zone, the oxidic charging material is reduced to metal, which is collected in the lower part of the meltdown gasifier.
It has shown that the method according to EP-A 0 174 291 may advantageously be used for reducing oxides reacting with elementary carbon at temperatures below 1,000C, yet that problems may occur when recovering metals and metal alloys, in particular ferro-alloys/ such as ferro~manganese, ferro-chromium and ferrosilicon, which are recoverable from their oxides only at temperatures exceeding 1,000C using elementary carbon as the reducing agent, since the period of contact of this oxidic charging materlal which reacts at higher temperatures, with the carbon particles forming the fluidized layer is relatively ; ; short.
The invention aims at avoiding these disadvanta~es and difficulties and has as its object to provide a method and a plant of the initially defined kind which make it possib-le to produce metals and metal alloys, in particular ferro~
alloys, such as ~erro-manganese, ~erro-chromium and ferro-- , . , ~ . : - ~ . , - ~ 32727~
silicon of lumpy oxidic charging material in a meltdown gasifier, wherein the metal has such a high a~finity to oxygen that it reacts with elementary carbon at above 1,000C only.
With a method of the initially defined kind this object is achieved according to the invention in that, under the action of gravity, lumpy oxidic charging material is guided through a static coal bed comprised of three layers, wherein - a bottom layer of degassed coal is provided, which covers a liquid sump of reduced metal and slag, - into a middle layer, oxygen or an oxygen-containing gas is introduced so as to form a hot reducing gas consisting essentially of CO, and - into a top layer, combustion gases of carbon par-ticles and oxygen or oxygen-containing gas are in-., troduced.
Advantageously, lumpy oxidic charging material havinga grain size of from 6 to 50 mm, preferably 10 to 30 mm, is used.
For forming the static bed layers, suitably coal having a grain size of ~rom 5 to 100 mm, in particular 5 to 30 mm, is used.
According to a preferred embodiment, the thickness of ; the middle and top static bed layers is maintained between 1 and 4 m.
A further embodiment o~ the method according to the invention in characterised in that dust-like carbon parti-cles are separated from the off-gas passing the static bed layers (reduction zones) and that these carbon particles, _ ~ _ ~327,;~(~
preferably in the hot state, together with oxygen or oxy-gen-containing gas are fed to burners directed into the top static bed layer.
As the coal, preferably coal maintaining its lumpy character after degassing is used, so that with a grain size range of from 5 to 100 mm, preferably 5 to 30 mm, utilized, at least 50 ~ of the degassed coal formed after degassing is present within the original grain size range of from 5 to 100 mm or 5 to 30 mm, respectively, and the remainder is present as undersize grain.
The method according to the invention offers the ad-vantage that all known advantages of the reduction pro-cesses in shaft furnaces heated with fossile energy are maintained, such as counterflow-heat exchange, metallurgi-cal reaction with elementary carbon in the static bed, which is necessary for the xeduction of oxides of non-precious metals, as well as a good separation of metal and slag. Coking or degassing of coal may be carried out with-out the formation of tar and other condensable compounds.
The gas formed during the degassing of the coal acts as additional reducing agent to the reduction gases formed from the gasification of the degassed coal.
A particular advantage of the method consists in that the reduction of oxides of non-precious elements, such as, e.g., silicon, chromium, manganese, can be effected without using electric energy. In the method according to the invention, the energy required for degassing the coal is controlled in a simple manner, because the undersize grain (smaller than 5 mm) is discharged with the hot of~-gases of 0 the meltdown gasifier, separated, returned into the upper .
~327~7~
blowing-in zone of oxygen-containing gases and oxidized by means of the oxygen-containing gases, heat being released.
The grain decomposition behaviour is tested such that a grain fraction of from 16 to 20 mm is subjected to de gassing for one hour in a chamber which has been pre-heated to 1,400C. The volume of the chamber is 12 dm3. After cooling by flushing with cold inert gas, the grain distri-bution is determined.
The invention furthermore comprises a plant for car-rying out the method with a refractorily lined shaEt-shaped meltdown gaslfier, which has, in its upper part, charging openings for introducing coal and lumpy oxidic charging m~t~:~ia~ w~l ~ a ~i~c~ye ~z~c~ ~or o~
wa~ ~ o~ ~he me~t~own yasi~ie~ 5~ein~ penetrate~ ~y s~pp~y : ducts for coal and oxygen or oxygen-containing gas, respec-: tively, and a lower section being provided for collecting : molten metal and liquid slag. This plant is characterised ~ .
-~ in that, under formation of three superposed static bed layers A, B, C
- in the region between the bottom static bed layer A
and t~ mi~lg ~t~ h~ ~ye~ B, ~ ~in~ of bloT~-in pipes for oxygen or oxygen-containing g~s is pro-vided and - at a distance thereabove, in the region between the middle static bed layer B and the top static bed layer C, a ring of burners charged with carbon particles and oxygen or oxygen-containing gas, re-spectively, is provided.
Advantageously, a hot cyclone for separating carbon particles from the off-gas is provided in the discharge ~327~7~
duct for off-gas, and the discharge end of this hot cyclone is in flow connection with the ring of burners.
The method and the plant of the invention for carrying out the method are explained in more detail by way of the drawing, which shows a schematic illustration of the melt-down gasifier with additional means connected thereto.
A shaft-like meltdown gasifier denoted by 1 has a refractory lining 2. The bottom region of the meltdown gasifier serves for accommodating molten metal 3 and molten slag 4. A tap opening for metal is denoted by 5, and a tap opening for slag is denoted by 6. In the upper part of the meltdown gasifier, a charging opening 7 for supplying lumpy coal, as well as a charging opening 9 for lumpy oxidic charging material are provided. Above the liquid sump 3, 4, the static coal bed is formed~ i.e. a bottom layer A of degassed coal which is not gas-passed, a middle layer B of degassed coal provided thereabove and passed by gas, and a top layer C of lumpy coal provided thereabove and passed by gas.
The side wall of the meltdown gasifier 1 is penetrated by blow-in pipes, i.e. by a ring of blow-in pipes 8 for oxygen or oxygen-containing gases, respectively. These pipes are arranged in the border region between the non-~ gas-passed static bed layer A and the static bed layer B.
;~ At a distance thereabove, i.e. in the border region between layer B and layer C, a ring of burners 10 pene-trating the side wall of the meltdown gasifier 1 i5 pro-vided, into which a mixture of dust-like carbon particles and oxygen or oxygen-containing gas is introduced. From the upper part of the meltdown gasifier, a discharge duct 11 13~7~
guides the off-gas formed to a hot cyclone 12.
Dust-like carbon particles suspended in the off-gas are separated in the hot cyclone 12 and fed from the dis-charge end of the hot cyclone 12, in which a dosing means 13 is provided, through a duct 14 to the burners 10 arranged in a ring. A duct for oxygen-containing gas leading to the burners 10 is denoted by 15. With the dosing means 13 the filling degree of the hot cyclone 12 can be regulated and the separating effect of the hot cyclone 12 can be influenced. From the upper part of the hot cyclone 12 off-gas is discharged through duct 16.
Advantageously, the method according to the invention is carried out such that coal and lumpy oxidic charging material are commonly introduced through the charging open-ings in the upper part of the meltdown gasifier 1. The coal is degassed in the static bed layer C. The heat required for degassing is provided, on the one hand, by the hot reducing gases rising from the static bed layer B, and, on the other hand, by combustion heat from the carbon partic-20: les burned by means of oxygen-containin~ gases in the : burners 10. The vertical extension of the layer C is selec-ted such that the gas leaving layer C has a minimum tempe-rature of 950C. Thereby it is ensured that tars and other condensable compounds are cracked. Thus an obstruction of the top static bed layer C becomes impossihle. In practice, a layer thickness of from 1 to 4 m has proved to be ad-vantageous for layer C. A vertical extension of from 1 to 4 m also proves to be advantageous for static bed layer B.
Coal degassed ln static bed layer C forms the static bed layer B when it sinks down.
132727~ , The lumpy oxidic charging material is melted in static bed layer B and reduced by the elementary carbon. The heat required for melting and reducing is supplied by gassifying hot degassed coal by means of oxygen-containing gases in~
troduced into the gasifier via the blow-in pipes 8. The molten metal forming in static bed layer B and the molten slag flow down and are collected and tapped below static bed layer A.
The invention relates to a method of recovering metals or metal alloys, in particular ferro-alloys, by reducing metal oxides in a reduction zone formed by a coal bed flowed through by a reducing gas, as well as a plant for carrying out the method.
` In EP-A - 0 174 291 a method of melting metals, i.e.
copper, lead, zinc, nickel, cobalt and tin, of oxidic fine-grain non-ferrous metal ores is described, wherein the charging material is charged into a reduction zone formed by a coal fluidized layer in a meltdown gasifier. When passing this reduction zone, the oxidic charging material is reduced to metal, which is collected in the lower part of the meltdown gasifier.
It has shown that the method according to EP-A 0 174 291 may advantageously be used for reducing oxides reacting with elementary carbon at temperatures below 1,000C, yet that problems may occur when recovering metals and metal alloys, in particular ferro-alloys/ such as ferro~manganese, ferro-chromium and ferrosilicon, which are recoverable from their oxides only at temperatures exceeding 1,000C using elementary carbon as the reducing agent, since the period of contact of this oxidic charging materlal which reacts at higher temperatures, with the carbon particles forming the fluidized layer is relatively ; ; short.
The invention aims at avoiding these disadvanta~es and difficulties and has as its object to provide a method and a plant of the initially defined kind which make it possib-le to produce metals and metal alloys, in particular ferro~
alloys, such as ~erro-manganese, ~erro-chromium and ferro-- , . , ~ . : - ~ . , - ~ 32727~
silicon of lumpy oxidic charging material in a meltdown gasifier, wherein the metal has such a high a~finity to oxygen that it reacts with elementary carbon at above 1,000C only.
With a method of the initially defined kind this object is achieved according to the invention in that, under the action of gravity, lumpy oxidic charging material is guided through a static coal bed comprised of three layers, wherein - a bottom layer of degassed coal is provided, which covers a liquid sump of reduced metal and slag, - into a middle layer, oxygen or an oxygen-containing gas is introduced so as to form a hot reducing gas consisting essentially of CO, and - into a top layer, combustion gases of carbon par-ticles and oxygen or oxygen-containing gas are in-., troduced.
Advantageously, lumpy oxidic charging material havinga grain size of from 6 to 50 mm, preferably 10 to 30 mm, is used.
For forming the static bed layers, suitably coal having a grain size of ~rom 5 to 100 mm, in particular 5 to 30 mm, is used.
According to a preferred embodiment, the thickness of ; the middle and top static bed layers is maintained between 1 and 4 m.
A further embodiment o~ the method according to the invention in characterised in that dust-like carbon parti-cles are separated from the off-gas passing the static bed layers (reduction zones) and that these carbon particles, _ ~ _ ~327,;~(~
preferably in the hot state, together with oxygen or oxy-gen-containing gas are fed to burners directed into the top static bed layer.
As the coal, preferably coal maintaining its lumpy character after degassing is used, so that with a grain size range of from 5 to 100 mm, preferably 5 to 30 mm, utilized, at least 50 ~ of the degassed coal formed after degassing is present within the original grain size range of from 5 to 100 mm or 5 to 30 mm, respectively, and the remainder is present as undersize grain.
The method according to the invention offers the ad-vantage that all known advantages of the reduction pro-cesses in shaft furnaces heated with fossile energy are maintained, such as counterflow-heat exchange, metallurgi-cal reaction with elementary carbon in the static bed, which is necessary for the xeduction of oxides of non-precious metals, as well as a good separation of metal and slag. Coking or degassing of coal may be carried out with-out the formation of tar and other condensable compounds.
The gas formed during the degassing of the coal acts as additional reducing agent to the reduction gases formed from the gasification of the degassed coal.
A particular advantage of the method consists in that the reduction of oxides of non-precious elements, such as, e.g., silicon, chromium, manganese, can be effected without using electric energy. In the method according to the invention, the energy required for degassing the coal is controlled in a simple manner, because the undersize grain (smaller than 5 mm) is discharged with the hot of~-gases of 0 the meltdown gasifier, separated, returned into the upper .
~327~7~
blowing-in zone of oxygen-containing gases and oxidized by means of the oxygen-containing gases, heat being released.
The grain decomposition behaviour is tested such that a grain fraction of from 16 to 20 mm is subjected to de gassing for one hour in a chamber which has been pre-heated to 1,400C. The volume of the chamber is 12 dm3. After cooling by flushing with cold inert gas, the grain distri-bution is determined.
The invention furthermore comprises a plant for car-rying out the method with a refractorily lined shaEt-shaped meltdown gaslfier, which has, in its upper part, charging openings for introducing coal and lumpy oxidic charging m~t~:~ia~ w~l ~ a ~i~c~ye ~z~c~ ~or o~
wa~ ~ o~ ~he me~t~own yasi~ie~ 5~ein~ penetrate~ ~y s~pp~y : ducts for coal and oxygen or oxygen-containing gas, respec-: tively, and a lower section being provided for collecting : molten metal and liquid slag. This plant is characterised ~ .
-~ in that, under formation of three superposed static bed layers A, B, C
- in the region between the bottom static bed layer A
and t~ mi~lg ~t~ h~ ~ye~ B, ~ ~in~ of bloT~-in pipes for oxygen or oxygen-containing g~s is pro-vided and - at a distance thereabove, in the region between the middle static bed layer B and the top static bed layer C, a ring of burners charged with carbon particles and oxygen or oxygen-containing gas, re-spectively, is provided.
Advantageously, a hot cyclone for separating carbon particles from the off-gas is provided in the discharge ~327~7~
duct for off-gas, and the discharge end of this hot cyclone is in flow connection with the ring of burners.
The method and the plant of the invention for carrying out the method are explained in more detail by way of the drawing, which shows a schematic illustration of the melt-down gasifier with additional means connected thereto.
A shaft-like meltdown gasifier denoted by 1 has a refractory lining 2. The bottom region of the meltdown gasifier serves for accommodating molten metal 3 and molten slag 4. A tap opening for metal is denoted by 5, and a tap opening for slag is denoted by 6. In the upper part of the meltdown gasifier, a charging opening 7 for supplying lumpy coal, as well as a charging opening 9 for lumpy oxidic charging material are provided. Above the liquid sump 3, 4, the static coal bed is formed~ i.e. a bottom layer A of degassed coal which is not gas-passed, a middle layer B of degassed coal provided thereabove and passed by gas, and a top layer C of lumpy coal provided thereabove and passed by gas.
The side wall of the meltdown gasifier 1 is penetrated by blow-in pipes, i.e. by a ring of blow-in pipes 8 for oxygen or oxygen-containing gases, respectively. These pipes are arranged in the border region between the non-~ gas-passed static bed layer A and the static bed layer B.
;~ At a distance thereabove, i.e. in the border region between layer B and layer C, a ring of burners 10 pene-trating the side wall of the meltdown gasifier 1 i5 pro-vided, into which a mixture of dust-like carbon particles and oxygen or oxygen-containing gas is introduced. From the upper part of the meltdown gasifier, a discharge duct 11 13~7~
guides the off-gas formed to a hot cyclone 12.
Dust-like carbon particles suspended in the off-gas are separated in the hot cyclone 12 and fed from the dis-charge end of the hot cyclone 12, in which a dosing means 13 is provided, through a duct 14 to the burners 10 arranged in a ring. A duct for oxygen-containing gas leading to the burners 10 is denoted by 15. With the dosing means 13 the filling degree of the hot cyclone 12 can be regulated and the separating effect of the hot cyclone 12 can be influenced. From the upper part of the hot cyclone 12 off-gas is discharged through duct 16.
Advantageously, the method according to the invention is carried out such that coal and lumpy oxidic charging material are commonly introduced through the charging open-ings in the upper part of the meltdown gasifier 1. The coal is degassed in the static bed layer C. The heat required for degassing is provided, on the one hand, by the hot reducing gases rising from the static bed layer B, and, on the other hand, by combustion heat from the carbon partic-20: les burned by means of oxygen-containin~ gases in the : burners 10. The vertical extension of the layer C is selec-ted such that the gas leaving layer C has a minimum tempe-rature of 950C. Thereby it is ensured that tars and other condensable compounds are cracked. Thus an obstruction of the top static bed layer C becomes impossihle. In practice, a layer thickness of from 1 to 4 m has proved to be ad-vantageous for layer C. A vertical extension of from 1 to 4 m also proves to be advantageous for static bed layer B.
Coal degassed ln static bed layer C forms the static bed layer B when it sinks down.
132727~ , The lumpy oxidic charging material is melted in static bed layer B and reduced by the elementary carbon. The heat required for melting and reducing is supplied by gassifying hot degassed coal by means of oxygen-containing gases in~
troduced into the gasifier via the blow-in pipes 8. The molten metal forming in static bed layer B and the molten slag flow down and are collected and tapped below static bed layer A.
Claims (13)
1. A method of recovering a metal or a metal alloy which comprises reducing a metal oxide in a reduction zone formed by a coal bed with a reducing gas passing through the reduction zone, wherein:
the coal bed is a three-layer static coal bed having i) a bottom static bed layer of degassed coal covering a liquid sump of reduced metal or metal alloy and slag, ii) a middle static bed layer, and (iii) a top static bed layer, the metal oxide is in a lump form and is guided under gravity action through the three-layer static coal bed, one of oxygen and an oxygen-containing gas is introduced into the middle static bed layer so as to form a hot reducing gas consisting essentially of CO, and combustion gases of carbon particles and one of oxygen and oxygen-containing gas are fed into the top static bed layer.
the coal bed is a three-layer static coal bed having i) a bottom static bed layer of degassed coal covering a liquid sump of reduced metal or metal alloy and slag, ii) a middle static bed layer, and (iii) a top static bed layer, the metal oxide is in a lump form and is guided under gravity action through the three-layer static coal bed, one of oxygen and an oxygen-containing gas is introduced into the middle static bed layer so as to form a hot reducing gas consisting essentially of CO, and combustion gases of carbon particles and one of oxygen and oxygen-containing gas are fed into the top static bed layer.
2. A method as set forth in claim 1, wherein the metal oxide in a lump form, has a grain size of from 6 to 50 mm.
3. A method as set forth in claim 2, wherein the metal oxide in a lump form has a grain size of from 10 to 30 mm.
4. A method as set forth in claim 1, wherein the static coal bed layers are formed by coal having a grain size of from
5 to 100 mm.
5. A method as set forth in claim 4, wherein the coal has a grain size of from 5 to 30 mm.
5. A method as set forth in claim 4, wherein the coal has a grain size of from 5 to 30 mm.
6. A method as set forth in claim 1, wherein the thickness of the middle static bed layer and the top static bed layer is maintained between 1 and 4 m.
7. A method as set forth in claim 1, which further comprises:
separating dust-like carbon particles from an off-gas that passed through the static bed layers, and feeding the dust-like carbon particles together with one of oxygen and oxygen-containing gas to burners directed into the top static bed layer.
separating dust-like carbon particles from an off-gas that passed through the static bed layers, and feeding the dust-like carbon particles together with one of oxygen and oxygen-containing gas to burners directed into the top static bed layer.
8. A method as set forth in claim 7, wherein the separated carbon particles are fed in a hot state to the burners.
9. A method as set forth in any one of claims 1 to 8, wherein ferro-alloy is recovered.
10. A method as set forth in claim 9, wherein the ferro-alloy is ferro-manganese, ferro-chromium or ferro-silicon.
11. A method as set forth in claim 9, wherein the reduction is carried out such that an off-gas leaving the top bed layer is maintained at a temperature of at least 950°C.
12. An apparatus for recovering a metal or a metal alloy by reducing a metal oxide in a reduction zone formed by a coal bed with a reducing gas passing through the coal bad, which comprises:
a refractorily lined shaft-like meltdown gasifier having an upper part, a side wall and a lower part, the upper part including openings for receiving coal and the oxide in a lump form as well as a discharge duct for an off-gas, the side wall having supply ducts for coal and one of oxygen and an oxygen-containing gas penetrating the said side wall, and the lower part being provided with outlets for collecting the metal or metal alloy in a molten state and molten slag, wherein:
(a) the gasifier is adapted such that a bottom static coal-bed layer covering a liquid sump of reduced metal and slag, a middle static coal-bed layer and a top static coal-bed layer are superposed within the gasifier when the apparatus is in use;
(b) the side wall is provided with a ring of blow-in pipes for one of oxygen and oxygen-containing gas in a region between the bottom static coal-bed layer and the middle static coal-bed layer; and (c) the side wall is provided with a ring of burners for burning carbon particles with one of oxygen or oxygen-containing gas between the middle static coal-bed layer and the top static coal-bed layer.
a refractorily lined shaft-like meltdown gasifier having an upper part, a side wall and a lower part, the upper part including openings for receiving coal and the oxide in a lump form as well as a discharge duct for an off-gas, the side wall having supply ducts for coal and one of oxygen and an oxygen-containing gas penetrating the said side wall, and the lower part being provided with outlets for collecting the metal or metal alloy in a molten state and molten slag, wherein:
(a) the gasifier is adapted such that a bottom static coal-bed layer covering a liquid sump of reduced metal and slag, a middle static coal-bed layer and a top static coal-bed layer are superposed within the gasifier when the apparatus is in use;
(b) the side wall is provided with a ring of blow-in pipes for one of oxygen and oxygen-containing gas in a region between the bottom static coal-bed layer and the middle static coal-bed layer; and (c) the side wall is provided with a ring of burners for burning carbon particles with one of oxygen or oxygen-containing gas between the middle static coal-bed layer and the top static coal-bed layer.
13. An apparatus as set forth in claim 12, further comprising a hot cyclone for separating carbon particles from the off-gas and provided in the discharge duct for the off-gas, the said hot cyclone having a discharge end, and means flow-connecting the discharge end of the hot cyclone with the said ring of burners.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT0288786A AT386007B (en) | 1986-10-30 | 1986-10-30 | METHOD AND SYSTEM FOR THE EXTRACTION OF METALS OR. METAL ALLOYS |
| ATA2887/86 | 1986-10-30 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1327274C true CA1327274C (en) | 1994-03-01 |
Family
ID=3541877
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000550403A Expired - Fee Related CA1327274C (en) | 1986-10-30 | 1987-10-28 | Method of recovering metals and metal alloys and a plant therefor |
Country Status (16)
| Country | Link |
|---|---|
| JP (1) | JP2572085B2 (en) |
| KR (1) | KR950001910B1 (en) |
| CN (1) | CN1011894B (en) |
| AT (1) | AT386007B (en) |
| AU (1) | AU597119B2 (en) |
| BR (1) | BR8705782A (en) |
| CA (1) | CA1327274C (en) |
| CZ (1) | CZ279400B6 (en) |
| DD (1) | DD262677A5 (en) |
| DE (1) | DE3735965A1 (en) |
| IN (1) | IN171251B (en) |
| PH (1) | PH26200A (en) |
| SK (1) | SK278936B6 (en) |
| SU (1) | SU1547713A3 (en) |
| UA (1) | UA2124A1 (en) |
| ZA (1) | ZA878021B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3543634A1 (en) * | 2018-03-23 | 2019-09-25 | Air Products and Chemicals, Inc. | Oxy-fuel combustion system and method for melting a pelleted charge material |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT386006B (en) * | 1986-10-30 | 1988-06-27 | Voest Alpine Ag | METHOD AND SYSTEM FOR THE EXTRACTION OF METALS OR. METAL ALLOYS |
| CN102974669B (en) * | 2012-11-30 | 2014-12-24 | 宁波思明汽车科技有限公司 | Fusible alloy recycling method for pipe forming |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IN164687B (en) * | 1984-08-16 | 1989-05-13 | Voest Alpine Ag | |
| SE453304B (en) * | 1984-10-19 | 1988-01-25 | Skf Steel Eng Ab | KIT FOR MANUFACTURE OF METALS AND / OR GENERATION OF BATTLE FROM OXIDE ORE |
| AT382390B (en) * | 1985-03-21 | 1987-02-25 | Voest Alpine Ind Anlagen | METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR STEEL PRE-PRODUCTS |
| AT386006B (en) * | 1986-10-30 | 1988-06-27 | Voest Alpine Ag | METHOD AND SYSTEM FOR THE EXTRACTION OF METALS OR. METAL ALLOYS |
-
1986
- 1986-10-30 AT AT0288786A patent/AT386007B/en not_active IP Right Cessation
-
1987
- 1987-10-19 IN IN911/DEL/87A patent/IN171251B/en unknown
- 1987-10-21 AU AU80004/87A patent/AU597119B2/en not_active Ceased
- 1987-10-23 DE DE19873735965 patent/DE3735965A1/en active Granted
- 1987-10-26 ZA ZA878021A patent/ZA878021B/en unknown
- 1987-10-27 CZ CS877689A patent/CZ279400B6/en not_active IP Right Cessation
- 1987-10-27 SK SK7689-87A patent/SK278936B6/en unknown
- 1987-10-28 CA CA000550403A patent/CA1327274C/en not_active Expired - Fee Related
- 1987-10-28 DD DD87308360A patent/DD262677A5/en unknown
- 1987-10-29 SU SU874203623A patent/SU1547713A3/en active
- 1987-10-29 UA UA4203623A patent/UA2124A1/en unknown
- 1987-10-29 BR BR8705782A patent/BR8705782A/en not_active IP Right Cessation
- 1987-10-29 JP JP62274591A patent/JP2572085B2/en not_active Expired - Lifetime
- 1987-10-30 CN CN87107202A patent/CN1011894B/en not_active Expired
- 1987-10-30 PH PH36004A patent/PH26200A/en unknown
- 1987-10-30 KR KR1019870012076A patent/KR950001910B1/en not_active IP Right Cessation
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3543634A1 (en) * | 2018-03-23 | 2019-09-25 | Air Products and Chemicals, Inc. | Oxy-fuel combustion system and method for melting a pelleted charge material |
| US11060792B2 (en) | 2018-03-23 | 2021-07-13 | Air Products And Chemicals, Inc. | Oxy-fuel combustion system and method for melting a pelleted charge material |
Also Published As
| Publication number | Publication date |
|---|---|
| KR880005276A (en) | 1988-06-28 |
| ZA878021B (en) | 1988-04-29 |
| DD262677A5 (en) | 1988-12-07 |
| KR950001910B1 (en) | 1995-03-06 |
| PH26200A (en) | 1992-03-18 |
| ATA288786A (en) | 1987-11-15 |
| AU597119B2 (en) | 1990-05-24 |
| CN1011894B (en) | 1991-03-06 |
| SK768987A3 (en) | 1998-04-08 |
| DE3735965A1 (en) | 1988-05-05 |
| AT386007B (en) | 1988-06-27 |
| BR8705782A (en) | 1988-05-31 |
| DE3735965C2 (en) | 1991-01-10 |
| CN87107202A (en) | 1988-05-18 |
| CZ279400B6 (en) | 1995-04-12 |
| SU1547713A3 (en) | 1990-02-28 |
| JPS63128132A (en) | 1988-05-31 |
| SK278936B6 (en) | 1998-04-08 |
| CZ768987A3 (en) | 1994-11-16 |
| IN171251B (en) | 1992-08-22 |
| UA2124A1 (en) | 1994-12-26 |
| AU8000487A (en) | 1988-05-05 |
| JP2572085B2 (en) | 1997-01-16 |
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| Date | Code | Title | Description |
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| MKLA | Lapsed |