CA2318185A1 - Method for producing hot metal - Google Patents
Method for producing hot metal Download PDFInfo
- Publication number
- CA2318185A1 CA2318185A1 CA002318185A CA2318185A CA2318185A1 CA 2318185 A1 CA2318185 A1 CA 2318185A1 CA 002318185 A CA002318185 A CA 002318185A CA 2318185 A CA2318185 A CA 2318185A CA 2318185 A1 CA2318185 A1 CA 2318185A1
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- Canada
- Prior art keywords
- reduction
- fusion
- gas
- gassifier
- zone
- 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.)
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B3/00—General features in the manufacture of pig-iron
- C21B3/02—General features in the manufacture of pig-iron by applying additives, e.g. fluxing agents
-
- 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
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
-
- 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
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Manufacture Of Iron (AREA)
Abstract
According to the inventive method for producing hot metal, feed materials made up of iron ore, preferably in lump and/or pellet form, and optionally, flux materials, preferably lime and/or dolomite are reduced to sponge iron in a reduction area. The resulting sponge iron is then melted down into hot metal in a melt-down gasification area with solid carbon supports and oxygencontaining gases being added and a reduction gas and slag being formed. Said reduction gas is at least partially introduced into the reduction area, reacted there and drawn off as top gas. The invention also relates to an installation for carrying out this method.
Description
Process for producing molten pig iron The invention relates to a process for producing molten pig iron, raw materials formed by iron ore, preferably in the form of pieces and/or pellets, and, if appropriate, additives, preferably limestone and/or dolomite, being reduced to iron sponge in a reduction zone, and the iron sponge being smelted in a fusion/
gassification zone with addition - of solid carbon carriers and oxygen-containing gases to give molten pig iron, and a reduction gas, which is at least partially introduced into the reduction zone, being converted therein and taken off as top gas, and slag being formed. The invention further relates to a plant for carrying out the process.
Such a process is known from DE PS 35 03 493. In this process, a direct reduction shaft furnace is fed, together with iron ore, with a carbon carrier which at least partially reduces again those constituents of the reduction gas which have been oxidized by the reduction of the iron ore. This measure is intended, on the one hand, to prevent the agglomeration of iron ore particles and/or iron sponge particles, but mainly to improve the heat balance of the fusion gassifier, so that its effect on the direct reduction shaft furnace is such that the quantity of gas containing CO and Hz and thus the quantity of reduction gas are diminished.
The diminution of the quantity of reduction gas in a direct reduction shaft furnace is, however, no longer up to date. A substantial part of the economics of a system consisting of fusion gassifier and direct reduction shaft furnace results from the fact that the top gas taken off from the direct reduction shaft furnace can, if appropriate after gas scrubbing, be used again as reduction gas and/or as calorifically utilizable gas. Diminution of the quantity of reduction gas thus also impairs the economics of such a process.
gassification zone with addition - of solid carbon carriers and oxygen-containing gases to give molten pig iron, and a reduction gas, which is at least partially introduced into the reduction zone, being converted therein and taken off as top gas, and slag being formed. The invention further relates to a plant for carrying out the process.
Such a process is known from DE PS 35 03 493. In this process, a direct reduction shaft furnace is fed, together with iron ore, with a carbon carrier which at least partially reduces again those constituents of the reduction gas which have been oxidized by the reduction of the iron ore. This measure is intended, on the one hand, to prevent the agglomeration of iron ore particles and/or iron sponge particles, but mainly to improve the heat balance of the fusion gassifier, so that its effect on the direct reduction shaft furnace is such that the quantity of gas containing CO and Hz and thus the quantity of reduction gas are diminished.
The diminution of the quantity of reduction gas in a direct reduction shaft furnace is, however, no longer up to date. A substantial part of the economics of a system consisting of fusion gassifier and direct reduction shaft furnace results from the fact that the top gas taken off from the direct reduction shaft furnace can, if appropriate after gas scrubbing, be used again as reduction gas and/or as calorifically utilizable gas. Diminution of the quantity of reduction gas thus also impairs the economics of such a process.
In the reduction of some iron ores, the problem arises that the interstitial volume per tonne of ore of the charge in the bed of the raw materials does not suffice for passing the quantity of reduction gas required for the ore reduction through the reduction shaft. This can have a number of causes: a high bulk density, or small mean grain size of the ore, a broad grain size distribution or a large proportion of fines, or pronounced grain disintegration of the ore particles or pellets during the reduction, or due to mechanical stress. The interstitial volume is here to be understood as the volume of the voids in a bed. An unduly small interstitial volume results in insufficient and/or fluctuating metallization of the iron sponge since, in addition to the unduly small quantity of reduction gas, the gas distribution within the reduction shaft is also non-uniform. In fact, channels can form within the bed, in which the reduction gas flows preferentially, while other regions obtain a gas flow which is no longer adequate, or none at all.
In addition, the non-uniform gas distribution also leads to a non-uniform temperature distribution in the bed, which adversely affects the calcination of the additives, such as limestone and/or dolomite, contained in the raw materials. Since the metallization and/or calcination, which has not been achieved in the direct reduction shaft furnace, must eventually be completed in the fusion-gassifier, this also leads to a reduction in the smelting performance of the fusion-gassifier and to a plant operation which is altogether unstable.
EP 0,623,684 A has disclosed a process in which waste materials and residues containing coal dust and iron in the metallic form and oxide form are separately collected and agglomerated in three groups in accordance with their composition, the first group mainly containing iron in the oxide form, the second group mainly containing iron in the metallic form and the third group mainly containing carbonaceous substances. These are utilized by feeding the substances of the first group to the reduction zone and those of the second and third groups to the fusion gassification zone.
The use of, in particular, agglomerates containing iron oxide in the reduction zone is, however, not a suitable method for increasing the voidage in the bed, since these agglomerates tend to lead to grain disintegration and have an unduly low mechanical stability.
It is the object of the invention to provide a process, in which a quantity of reduction gas, increased as compared with the state of the art, can be passed through the reduction shaft and a degree of metallization and calcination, which is both increased and made more uniform, of the iron sponge and the additives respectively, is achieved owing to a gas distribution which has been made more uniform.
According to the invention, this object is achieved in such a way that, together with the raw materials, further lumpy additives, which are substantially inert under the reaction conditions of~the reduction zone, are fed to the reduction zone.
In this connection, "inert" is to be understood as an essentially chemical inertness, that is to say the further additives react with the reduction gas and to the raw materials only to a negligible degree or not at all. Moreover, "inert" is also to be understood as being essentially completely resistant to thermal and mechanical stresses. The expulsion of small quantities of gases such as COZ and/or HZO is, however, possible.
The further additives thus do not tend to suffer grain disintegration or increased erosion either due to the shock-like heating occurring on introduction into the reduction zone or owing to the remainder of the bed lying above them in the further course of the reaction.
The further additives migrate essentially unchanged through the reduction zone. The interstitial volume per tonne of ore in the bed is increased by the addition of inert lumpy additives.
According to a preferred embodiment of the process according to the invention, it is possible thereby to pass an increased quantity of reduction gas from the fusion gassification zone through the reduction zone.
The quantity of reduction gas is then about 5 to 50s, preferably 20 to 40~, greater than the quantity required for reducing the iron ore. Owing to the increased interstitial volume, the formation of channels and instances of caking within the bed is also diminished and therefore the gas distribution is also made more uniform, again with the result of an overall enhanced and more uniform metallization and calcination of the raw materials.
Advantageously, the further additives used are coke, which is substantially inert under the reaction conditions, and/or carriers of slag constituents, the main constituents being Ca0 and/or Mg0 and/or SiOZ
and/or A1203.
Whereas it is explicitly demanded in the state of the art described above that the coke charged to the direct reduction shaft furnace reacts at least partially with the reduction gas, this is not desired in this case since the mean grain size of the further additives should not change during the passage through the reduction zone. Such a coke, as used according to the invention, is rendered inert, for example, by a thin layer of ash. In the case of the carriers of slag constituents likewise used according to the invention, the problem of the reaction with the raw materials or the reduction gas does not arise.
According to a preferred embodiment, quartz and/or slag from a steel converter and/or a blast furnace and/or an electric furnace and/or from the fusion gassification zone are used as further additives.
In addition to the outstanding suitability of these materials for the process according to the invention, the use of slag also leads to the utilization of at least a part of slags arising in the iron and steel industry. Hitherto, these stags had either to be dumped or, at best, could be used further in the building materials industry.
Accordingly, the use of slag from a steel converter, in particular a steel converter operated by the LD
process, is particularly preferred. These stags have an especially low phosphorus content and therefore do not cause any additional introduction of phosphorus into the fusion gassification zone which follows the reduction zone.
Advantageously, the mean grain size of the further additives is 6 to 40 mm, preferably 10 to 25 mm. This range of grain sizes essentially corresponds to that of the remaining raw materials and therefore makes it possible to enhance the gas permeability of the bed and makes this more uniform.
According to a further advantageous embodiment of the process according to the invention, the volume of the further additives, relative to the total volume of all the materials fed to the reduction zone, is 5 to 30%, preferably 5 to 20%. In this range, there is an optimum of gas permeability of the bed in the reduction zone, the degree of metallization and/or calcination of the raw materials, of the achievable reduction performance of the reduction zone and also of the smelting performance of the fusion gassification zone.
The invention also relates to a plant for carrying out a process for producing molten pig iron from raw materials formed from iron ore, preferably in the form of pieces and/or pellets and, if appropriate, additives, preferably limestone and/or dolomite, comprising a reduction reactor for iron ore, a fusion-gassifier, a feed line, connecting the fusion gassifier to the reduction reactor, for a reduction gas formed in the fusion gassifier, one or more conveying lines, connecting the reduction reactor to the fusion-gassifier, for the reduction product formed in the reduction reactor, a top gas discharge line starting from the reduction reactor, a feed line, leading into the fusion gassifier, for carbon carriers, and also feed lines, leading into the fusion gassifier, for oxygen-containing gases, and a tapping for pig iron and slag provided on the fusion gassifier.
Such a plant is characterized in that a charging device for the addition of further lumpy additives, which are substantially inert under the reaction conditions prevailing in the reduction reactor, is provided on the reduction reactor.
According to a preferred embodiment, means for controlling the volume flow of top gas taken off from the reduction reactor are provided in the top gas discharge line. These means can be designed as, for example, an adjustable flap. By means of controlling the volume flow of top gas, the volume flow of reduction gas, increased according to the invention, into the reduction reactor is at the same time also adjusted.
Advantageously, a discharge line branches off from the reduction gas feed line which connects the fusion-_ 7 _ gassifier to the reduction reactor and through which that proportion of the reduction gas is withdrawn which is not fed to the reduction reactor. Preferably, a pressure control instrument is provided in this discharge line, which instrument is usually preset to a defined pressure, so that reduction gas is removed from the system when this pressure is exceeded.
Advantageously, the charging device for the further additives includes a weighing device, by means of which the desired quantitative ratio relative to the remaining raw materials is adjusted.
The process according to the invention is explained in more detail below by reference to an illustrative embodiment:
Raw materials in the shaft, without inert material:
150 tonne/hour of ore 15 tonne/hour of limestone 10 tonne/hour of dolomite 157,000 m3/hour of reduction gas Voidage: about 45s Degree of metallization of the Fe sponge: about 800 Degree of calcination of the additives: about 80%
Derived characteristic process data:
Reduction gas/m3 of charge: ~ about 2050 m3 Reduction gas/tonne of ore or pellets: about 1050 m3 Raw materials in the shaft with inert material:
140 tonne/hour of ore 5.5 tonne/hour of dolomite 28.5 tonne/hour of LD slag 166,000 m3/hour of reduction gas Voidage: about 450 Degree of metallization of the Fe sponge: > 900 Degree of calcination of the additives: > 85%
Derived characteristic process data:
Reduction gas/m3 of charge: about 2050 m3 Reduction gas/tonne of ore or pellets: about 1180 m3, that is to say specifically about 12% more gas Gas volumes refer in each case to the standard state, that is to say 273.15 K and 101,325 Pa.
The invention is explained in more detail below by reference to an illustrative embodiment shown in the drawing in Figure 1, the drawing illustrating, in a diagrammatic representation, a preferred embodiment of the plant for carrying out the process according to the invention.
Lumpy raw materials containing iron oxide, such as ore 4, if appropriate with uncalcined additives 5, such as limestone and/or dolomite, are charged from above via a feed line 3 to a reduction reactor designed as a shaft furnace 1, that is to say into the reduction zone 2 thereof. The shaft furnace 1 is connected to a fusion-gassifier 6, in which a reduction gas is generated from carbon carriers and oxygen-containing gas, which reduction gas is fed via a feed line 7 to the shaft furnace 1 and flows through the~latter in counter-current to the raw materials 4, 5.
Moreover, further additives 8 are introduced into the reduction reactor 1 by means of a charging device 9.
The charging device is fitted with a weighing device, by means of which the quantitative ratio or the volume ratio of the further additives 8 relative to the raw materials 4, 5 is controlled.
The fusion gassifier 6 has a feed line 10 for solid lumpy carbon carriers 11 and feed lines 12 for oxygen-containing gases. In the fusion gassifier 6, molten pig _ g _ iron 14 and molten slag 15 accumulate below the fusion-gassification zone 13 and are tapped via a tapping 16., The raw materials 4, 5, partially or wholly reduced to iron sponge in the shaft furnace 1 in the reduction zone 2 are fed to the fusion gassifier 6 via one or more conveying lines 17, for example by means of conveyor screws. The upper part of the shaft furnace 1 is adjoined by a discharge line 18 for the top gas formed in the reduction zone 2. The top gas discharge line 18 contains means 19, for example an adjustable flap, for controlling the volume flow of the top gas taken off from the shaft furnace 1. The means 19 provided in the top gas discharge line 18 also control the volume of the reduction gas introduced via the reduction gas feed line 7 into the shaft furnace 1.
From the reduction gas feed line 7, a discharge line 20 branches off, through which reduction gas which is not passed into the reduction reactor 1 is taken off. The discharge line 20 can contain a pressure control instrument 21. The pressure control instrument 21 is usually preset to a defined pressure, so that reduction gas is removed from the system when this pressure is exceeded.
The volume of the reduction gas fed to the shaft furnace 1 is controlled by the interaction of the pressure control instrument 21 and the means 19 for controlling the volume flow.
The invention is not restricted to the illustrative embodiment shown in Figure 1, but also comprises all means known to those skilled in the art, which can be utilized for carrying out the invention.
In addition, the non-uniform gas distribution also leads to a non-uniform temperature distribution in the bed, which adversely affects the calcination of the additives, such as limestone and/or dolomite, contained in the raw materials. Since the metallization and/or calcination, which has not been achieved in the direct reduction shaft furnace, must eventually be completed in the fusion-gassifier, this also leads to a reduction in the smelting performance of the fusion-gassifier and to a plant operation which is altogether unstable.
EP 0,623,684 A has disclosed a process in which waste materials and residues containing coal dust and iron in the metallic form and oxide form are separately collected and agglomerated in three groups in accordance with their composition, the first group mainly containing iron in the oxide form, the second group mainly containing iron in the metallic form and the third group mainly containing carbonaceous substances. These are utilized by feeding the substances of the first group to the reduction zone and those of the second and third groups to the fusion gassification zone.
The use of, in particular, agglomerates containing iron oxide in the reduction zone is, however, not a suitable method for increasing the voidage in the bed, since these agglomerates tend to lead to grain disintegration and have an unduly low mechanical stability.
It is the object of the invention to provide a process, in which a quantity of reduction gas, increased as compared with the state of the art, can be passed through the reduction shaft and a degree of metallization and calcination, which is both increased and made more uniform, of the iron sponge and the additives respectively, is achieved owing to a gas distribution which has been made more uniform.
According to the invention, this object is achieved in such a way that, together with the raw materials, further lumpy additives, which are substantially inert under the reaction conditions of~the reduction zone, are fed to the reduction zone.
In this connection, "inert" is to be understood as an essentially chemical inertness, that is to say the further additives react with the reduction gas and to the raw materials only to a negligible degree or not at all. Moreover, "inert" is also to be understood as being essentially completely resistant to thermal and mechanical stresses. The expulsion of small quantities of gases such as COZ and/or HZO is, however, possible.
The further additives thus do not tend to suffer grain disintegration or increased erosion either due to the shock-like heating occurring on introduction into the reduction zone or owing to the remainder of the bed lying above them in the further course of the reaction.
The further additives migrate essentially unchanged through the reduction zone. The interstitial volume per tonne of ore in the bed is increased by the addition of inert lumpy additives.
According to a preferred embodiment of the process according to the invention, it is possible thereby to pass an increased quantity of reduction gas from the fusion gassification zone through the reduction zone.
The quantity of reduction gas is then about 5 to 50s, preferably 20 to 40~, greater than the quantity required for reducing the iron ore. Owing to the increased interstitial volume, the formation of channels and instances of caking within the bed is also diminished and therefore the gas distribution is also made more uniform, again with the result of an overall enhanced and more uniform metallization and calcination of the raw materials.
Advantageously, the further additives used are coke, which is substantially inert under the reaction conditions, and/or carriers of slag constituents, the main constituents being Ca0 and/or Mg0 and/or SiOZ
and/or A1203.
Whereas it is explicitly demanded in the state of the art described above that the coke charged to the direct reduction shaft furnace reacts at least partially with the reduction gas, this is not desired in this case since the mean grain size of the further additives should not change during the passage through the reduction zone. Such a coke, as used according to the invention, is rendered inert, for example, by a thin layer of ash. In the case of the carriers of slag constituents likewise used according to the invention, the problem of the reaction with the raw materials or the reduction gas does not arise.
According to a preferred embodiment, quartz and/or slag from a steel converter and/or a blast furnace and/or an electric furnace and/or from the fusion gassification zone are used as further additives.
In addition to the outstanding suitability of these materials for the process according to the invention, the use of slag also leads to the utilization of at least a part of slags arising in the iron and steel industry. Hitherto, these stags had either to be dumped or, at best, could be used further in the building materials industry.
Accordingly, the use of slag from a steel converter, in particular a steel converter operated by the LD
process, is particularly preferred. These stags have an especially low phosphorus content and therefore do not cause any additional introduction of phosphorus into the fusion gassification zone which follows the reduction zone.
Advantageously, the mean grain size of the further additives is 6 to 40 mm, preferably 10 to 25 mm. This range of grain sizes essentially corresponds to that of the remaining raw materials and therefore makes it possible to enhance the gas permeability of the bed and makes this more uniform.
According to a further advantageous embodiment of the process according to the invention, the volume of the further additives, relative to the total volume of all the materials fed to the reduction zone, is 5 to 30%, preferably 5 to 20%. In this range, there is an optimum of gas permeability of the bed in the reduction zone, the degree of metallization and/or calcination of the raw materials, of the achievable reduction performance of the reduction zone and also of the smelting performance of the fusion gassification zone.
The invention also relates to a plant for carrying out a process for producing molten pig iron from raw materials formed from iron ore, preferably in the form of pieces and/or pellets and, if appropriate, additives, preferably limestone and/or dolomite, comprising a reduction reactor for iron ore, a fusion-gassifier, a feed line, connecting the fusion gassifier to the reduction reactor, for a reduction gas formed in the fusion gassifier, one or more conveying lines, connecting the reduction reactor to the fusion-gassifier, for the reduction product formed in the reduction reactor, a top gas discharge line starting from the reduction reactor, a feed line, leading into the fusion gassifier, for carbon carriers, and also feed lines, leading into the fusion gassifier, for oxygen-containing gases, and a tapping for pig iron and slag provided on the fusion gassifier.
Such a plant is characterized in that a charging device for the addition of further lumpy additives, which are substantially inert under the reaction conditions prevailing in the reduction reactor, is provided on the reduction reactor.
According to a preferred embodiment, means for controlling the volume flow of top gas taken off from the reduction reactor are provided in the top gas discharge line. These means can be designed as, for example, an adjustable flap. By means of controlling the volume flow of top gas, the volume flow of reduction gas, increased according to the invention, into the reduction reactor is at the same time also adjusted.
Advantageously, a discharge line branches off from the reduction gas feed line which connects the fusion-_ 7 _ gassifier to the reduction reactor and through which that proportion of the reduction gas is withdrawn which is not fed to the reduction reactor. Preferably, a pressure control instrument is provided in this discharge line, which instrument is usually preset to a defined pressure, so that reduction gas is removed from the system when this pressure is exceeded.
Advantageously, the charging device for the further additives includes a weighing device, by means of which the desired quantitative ratio relative to the remaining raw materials is adjusted.
The process according to the invention is explained in more detail below by reference to an illustrative embodiment:
Raw materials in the shaft, without inert material:
150 tonne/hour of ore 15 tonne/hour of limestone 10 tonne/hour of dolomite 157,000 m3/hour of reduction gas Voidage: about 45s Degree of metallization of the Fe sponge: about 800 Degree of calcination of the additives: about 80%
Derived characteristic process data:
Reduction gas/m3 of charge: ~ about 2050 m3 Reduction gas/tonne of ore or pellets: about 1050 m3 Raw materials in the shaft with inert material:
140 tonne/hour of ore 5.5 tonne/hour of dolomite 28.5 tonne/hour of LD slag 166,000 m3/hour of reduction gas Voidage: about 450 Degree of metallization of the Fe sponge: > 900 Degree of calcination of the additives: > 85%
Derived characteristic process data:
Reduction gas/m3 of charge: about 2050 m3 Reduction gas/tonne of ore or pellets: about 1180 m3, that is to say specifically about 12% more gas Gas volumes refer in each case to the standard state, that is to say 273.15 K and 101,325 Pa.
The invention is explained in more detail below by reference to an illustrative embodiment shown in the drawing in Figure 1, the drawing illustrating, in a diagrammatic representation, a preferred embodiment of the plant for carrying out the process according to the invention.
Lumpy raw materials containing iron oxide, such as ore 4, if appropriate with uncalcined additives 5, such as limestone and/or dolomite, are charged from above via a feed line 3 to a reduction reactor designed as a shaft furnace 1, that is to say into the reduction zone 2 thereof. The shaft furnace 1 is connected to a fusion-gassifier 6, in which a reduction gas is generated from carbon carriers and oxygen-containing gas, which reduction gas is fed via a feed line 7 to the shaft furnace 1 and flows through the~latter in counter-current to the raw materials 4, 5.
Moreover, further additives 8 are introduced into the reduction reactor 1 by means of a charging device 9.
The charging device is fitted with a weighing device, by means of which the quantitative ratio or the volume ratio of the further additives 8 relative to the raw materials 4, 5 is controlled.
The fusion gassifier 6 has a feed line 10 for solid lumpy carbon carriers 11 and feed lines 12 for oxygen-containing gases. In the fusion gassifier 6, molten pig _ g _ iron 14 and molten slag 15 accumulate below the fusion-gassification zone 13 and are tapped via a tapping 16., The raw materials 4, 5, partially or wholly reduced to iron sponge in the shaft furnace 1 in the reduction zone 2 are fed to the fusion gassifier 6 via one or more conveying lines 17, for example by means of conveyor screws. The upper part of the shaft furnace 1 is adjoined by a discharge line 18 for the top gas formed in the reduction zone 2. The top gas discharge line 18 contains means 19, for example an adjustable flap, for controlling the volume flow of the top gas taken off from the shaft furnace 1. The means 19 provided in the top gas discharge line 18 also control the volume of the reduction gas introduced via the reduction gas feed line 7 into the shaft furnace 1.
From the reduction gas feed line 7, a discharge line 20 branches off, through which reduction gas which is not passed into the reduction reactor 1 is taken off. The discharge line 20 can contain a pressure control instrument 21. The pressure control instrument 21 is usually preset to a defined pressure, so that reduction gas is removed from the system when this pressure is exceeded.
The volume of the reduction gas fed to the shaft furnace 1 is controlled by the interaction of the pressure control instrument 21 and the means 19 for controlling the volume flow.
The invention is not restricted to the illustrative embodiment shown in Figure 1, but also comprises all means known to those skilled in the art, which can be utilized for carrying out the invention.
Claims (12)
1. Process for producing molten pig iron, raw materials formed by iron ore, preferably in the form of pieces and/or pellets and, if appropriate, additives, preferably limestone and/or dolomite, being reduced to iron sponge in a reduction zone, and the iron sponge being smelted in a fusion-gassification zone with addition of solid carbon carriers and oxygen-containing gases to give molten pig iron, and a reduction gas, which is at least partially introduced into the reduction zone, being converted therein and taken off as top gas, and slag being formed, characterized in that, together with the raw materials, further lumpy additives, which are substantially inert under the reaction conditions of the reduction zone are fed to the reduction zone.
2. Process according to Claim 1, characterized in that the quantity of the reduction gas introduced into the reduction zone is 5 to 50%, preferably 20 to 40%, greater than the quantity required for reducing the iron ore.
3. Process according to one of Claims 1 or 2, characterized in that the further additives used are coke, which is substantially inert under the reaction conditions, and/or carriers of slag constituents, the main components being CaO and/or MgO and/or SiO2 and/or Al2O3.
4. Process according to one of Claims 1 to 3, characterized in that the further additives used are quartz and/or slag from a steel converter and/or a blast furnace and/or an electric furnace and/or from the fusion gassification zone.
5. Process according to Claim 4, characterized in that the further additive used is slag from a steel converter, in particular a steel converter operated by the LD process.
6. Process according to Claims 1 to 5, characterized in that the mean grain size of the further additives is 6 to 40 mm, preferably 10 to 25 mm.
7. Process according to one of Claims 1 to 6, characterized in that the volume of the further additives, relative to the total volume of all the materials fed to the reduction zone, is 5 to 30%, preferably 5 to 20%.
8. Plant for producing molten pig iron from raw materials (4, 5) formed from iron ore (4), preferably in the form of pieces and/or pellets, and, if appropriate, additives (5), preferably limestone and/or dolomite, comprising a reduction reactor (1) for iron ore, a fusion gassifier (6), a feed line (7), connecting the fusion gassifier (6) to the reduction reactor (1), for a reduction gas formed in the fusion gassifier (6), one or more conveying lines (17), connecting the reduction reactor (1) to the fusion gassifier (6), for the reduction product formed in the reduction reactor (1), a top gas discharge line (18) starting from the reduction reactor (1), a feed line (10), leading into the fusion gassifier (6), for carbon carriers (11), and also feed lines (12), leading into the fusion gassifier (6), for oxygen-containing gases, and a tapping (16) for pig iron (14) and slag (15) provided on the fusion gassifier, characterized in that a charging device (9) for the addition of further lumpy additives (8), which are substantially inert under the reaction conditions prevailing in the reduction reactor (1), is provided on the reduction reactor (1).
9. Plant according to Claim 8, characterized in that means (19) for controlling the volume flow of top gas taken off from the reduction reactor (1) are provided in the top gas discharge line.
10. Plant according to one of Claims 8 or 9, characterized in that a discharge line (20) branches off from the reduction gas feed line (7).
11. Plant according to one of Claims 8 to 10, characterized in that a pressure control instrument (21) is provided in the discharge line (20).
12. Plant according to one of Claims 8 to 11, characterized in that the charging device (9) for the further additives (8) includes a weighing device.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ATA49/98 | 1998-01-15 | ||
| AT0004998A AT407054B (en) | 1998-01-15 | 1998-01-15 | METHOD FOR PRODUCING LIQUID PIG IRON |
| PCT/EP1998/008453 WO1999036579A1 (en) | 1998-01-15 | 1998-12-22 | Method for producing hot metal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2318185A1 true CA2318185A1 (en) | 1999-07-22 |
Family
ID=3480178
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002318185A Abandoned CA2318185A1 (en) | 1998-01-15 | 1998-12-22 | Method for producing hot metal |
Country Status (12)
| Country | Link |
|---|---|
| EP (1) | EP1047795A1 (en) |
| JP (1) | JP2002509192A (en) |
| KR (1) | KR20010034175A (en) |
| CN (1) | CN1285880A (en) |
| AT (1) | AT407054B (en) |
| AU (1) | AU2417099A (en) |
| BR (1) | BR9814005A (en) |
| CA (1) | CA2318185A1 (en) |
| PL (1) | PL341942A1 (en) |
| TW (1) | TW479073B (en) |
| WO (1) | WO1999036579A1 (en) |
| ZA (1) | ZA99166B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110512043A (en) * | 2019-09-11 | 2019-11-29 | 中南大学 | A kind of method of gas-based shaft kiln calcined limestone coproduction iron ore prereduction product |
| CN111218535A (en) * | 2020-03-15 | 2020-06-02 | 苏亚杰 | Method for producing direct reduced iron by heating circulating reducing gas in gas production of molten iron bath coal |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB706318A (en) * | 1950-01-30 | 1954-03-31 | Somogyi Francis Paul | A method for the heat-treatment of materials in vertical shaft furnaces |
| DE1026080B (en) * | 1952-06-03 | 1958-03-13 | Rheinische Kalksteinwerke | Method for achieving coke savings in the shaft furnace |
| US3214263A (en) * | 1961-09-05 | 1965-10-26 | Indian Iron & Steel Company Lt | Treatment of haematite iron ore for use in the production of iron |
| US3635456A (en) * | 1970-04-29 | 1972-01-18 | Dravo Corp | Apparatus for direct reduction of iron oxide compacts |
| DE2813977A1 (en) * | 1977-07-13 | 1979-01-25 | John Edward Rehder | Smelting metal oxide compacts in shaft furnace - using non-coking carbonaceous reductant and controlled combustion conditions |
| DE2921786A1 (en) * | 1979-05-29 | 1980-12-11 | Veszpremi Vegyipari Egyetem | Iron powder made by redn. of iron oxide - which contains additives preventing reduced particles from baking together, and where additives form oxide(s) which may remain in prod. |
| DE3421878A1 (en) * | 1984-06-13 | 1985-12-19 | Klöckner-Humboldt-Deutz AG, 5000 Köln | Process and plant for the continuous production of pig iron |
| DE3503493A1 (en) * | 1985-01-31 | 1986-08-14 | Korf Engineering GmbH, 4000 Düsseldorf | METHOD FOR THE PRODUCTION OF RAW IRON |
| SE9003494L (en) * | 1990-11-01 | 1992-05-02 | Ssab Tunnplaat Ab | TAKE CARE OF FINE CORN REMEDY PRODUCTS |
| AT403055B (en) * | 1993-05-07 | 1997-11-25 | Voest Alpine Ind Anlagen | METHOD FOR RECYCLING IRONIC WASTE OR RESIDUES |
-
1998
- 1998-01-15 AT AT0004998A patent/AT407054B/en not_active IP Right Cessation
- 1998-12-21 TW TW087121293A patent/TW479073B/en active
- 1998-12-22 JP JP2000540280A patent/JP2002509192A/en not_active Withdrawn
- 1998-12-22 CN CN98813116A patent/CN1285880A/en active Pending
- 1998-12-22 WO PCT/EP1998/008453 patent/WO1999036579A1/en not_active Application Discontinuation
- 1998-12-22 BR BR9814005-1A patent/BR9814005A/en active Search and Examination
- 1998-12-22 EP EP98966675A patent/EP1047795A1/en not_active Withdrawn
- 1998-12-22 KR KR1020007007802A patent/KR20010034175A/en not_active Application Discontinuation
- 1998-12-22 AU AU24170/99A patent/AU2417099A/en not_active Abandoned
- 1998-12-22 CA CA002318185A patent/CA2318185A1/en not_active Abandoned
- 1998-12-22 PL PL98341942A patent/PL341942A1/en unknown
-
1999
- 1999-01-11 ZA ZA9900166A patent/ZA99166B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| ZA99166B (en) | 1999-07-12 |
| TW479073B (en) | 2002-03-11 |
| AT407054B (en) | 2000-12-27 |
| WO1999036579A1 (en) | 1999-07-22 |
| PL341942A1 (en) | 2001-05-07 |
| EP1047795A1 (en) | 2000-11-02 |
| BR9814005A (en) | 2000-10-10 |
| ATA4998A (en) | 2000-04-15 |
| CN1285880A (en) | 2001-02-28 |
| AU2417099A (en) | 1999-08-02 |
| KR20010034175A (en) | 2001-04-25 |
| JP2002509192A (en) | 2002-03-26 |
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