CN1876849A - Ironmaking method - Google Patents
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- CN1876849A CN1876849A CN 200610091218 CN200610091218A CN1876849A CN 1876849 A CN1876849 A CN 1876849A CN 200610091218 CN200610091218 CN 200610091218 CN 200610091218 A CN200610091218 A CN 200610091218A CN 1876849 A CN1876849 A CN 1876849A
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Abstract
The invention discloses a method for iron-smelting which comprises: a direct deoxidizing process which partly deoxidizes material with iron and produces part deoxidized material with iron; a direct smelting process which smelts part deoxidized material with iron and produces smelting raw iron, slag and discharge gas; and a process which collects CO2 from discharge gas without releasing the discharge gas to air.
Description
Technical Field
The invention relates to an iron-making method.
The present invention relates particularly, but not exclusively, to an ironmaking process which employs carbon as a recycled reductant in the process.
Background
Generally speaking, there is provided according to the present invention an ironmaking process for producing iron from an iron-containing feed, the process comprising:
(1) a direct reduction process comprising providing an iron-containing feed (feed material) to a direct reduction vessel, at least partially reducing the feed in the vessel, and producing an at least partially reduced iron-containing feed;
(2) a direct smelting process which comprises supplying solid feed material from the direct reduction process (1) in the form of partially reduced iron-containing feed material to a direct smelting vessel together with (i) solid carbonaceous material and (ii) oxygen-containing gas, smelting the partially reduced iron-containing feed material in the vessel and producing molten pig iron, slag and process off-gas; and
(3) separation and collection of CO from process exhaust gas2And not releasing the exhaust gas to the atmosphere.
The ironmaking process may further comprise sequestration (sequestration) of CO in the off-gas collected in the off-gas collection and separation process (3)2。
Optionally, the ironmaking process may further comprise recovering the collected CO2For example in the form of synthetic coal.
In this alternative, it is preferred that the ironmaking process may further comprise employing intermittent availabilityFrom the collected CO2For example in the form of synthetic coal.
Preferably, the ironmaking process further comprises recycling the recovered solid carbon in the process and employing the carbon as a reducing agent in the process.
Preferably, the ironmaking process includes recycling an amount of recovered solid carbon that is at least 50% of the initial solid reductant used in the direct smelting process (1).
The main motivation for the exhaust gas collection and separation process (3) is toreduce CO2And (5) discharging. In particular, CO with current ironmaking processes2Compared with the emission, the method can greatly reduce the CO in the pig iron production2There is a strong demand for emissions.
In a broad sense, the power generation industry will come to cover CO2Sealing and improving nuclear energy utilization. Large coal power plants with CO in a worldwide region where sequestration is feasible2And (4) sealing and storing to operate cooperatively. However, in the region where sequestration is not feasible, the nuclear energy will more easily become a neutral pillar of a new power generation source. In the latter (i.e., low CO)2Possibility of sealing andand areas of increased nuclear energy utilization), the present invention can play a key role.
Traditionally, nuclear power plants have been installed to provide base load energy. As demand patterns have changed, fossil (natural gas or coal) powered generators have been required to provide additional energy to the grid as necessary. In the future, if CO is reduced2Emissions requirements become more stringent, which makes fossil-powered generators less attractive. Building additional nuclear power capability to provide the peak power required is not currently very attractive because it means that large nuclear power will sit idle for long periods of time. What is lacking at present is an energy storage means that allows these nuclear power plants to operate continuously at full load, thereby eliminating changes on the grid.
Renewable energy (from wind turbines and solar cells) has the problem of limited options for its energy storage. Currently, wind and solar energy are considered problematic because they can only be generated when the climatic conditions are satisfactory. Currently, backup power generation capacity (in the form of fossil powerplants) is required and this limits the amount of renewable energy that can be received on the grid.
Disclosure of Invention
The invention makes it easier to use nuclear and renewable energy. Specifically, the ironmaking process of the present invention preferably comprises the steps of:
(a) using coal as a reducing agent in an ironmaking process (as described above);
(b) collecting the resulting CO2Liquefied and stored in suitable storage vessels (in a similar manner as currently employed for LNG (liquefied natural gas) storage) and preferably provides storage capacity sufficient for several days of plant operation; and is
(c) This method is used to derive off-peak (nuclear and/or renewable) energy from CO when it is available2Solid carbon in the form of synthetic coal is recovered and can be safely stored in bulk in stockpiles.
The applicant is not aware of the fact that it is intended to remove CO from2A commercially viable technology for the recovery of solid carbon. However, the basic principle of operation of a possible commercial carbon recovery process can be stated.
For example, recent studies at the university of Arizona (School of Aerospace and mechanical engineering) have shown that solid oxide electrolysis can be used to electrolyze CO2Electrolysis to directly produce solid carbon (synthetic carbon) (Iacomimi, C S and Sridhar, K R, Combined CO)2/H2O Solid Oxide Electrolysis Performance，posterpresented at 204thMeeting of electrolytic Society, Orlando, FL, October 12-162003). While this work is directed to space development and not large tonnage industrial processes, these principles are valuable for large tonnage industrial processes such as the present invention.
One alternative to synthetic coal production is to perfect an established process chemistry, which involves H2Reaction with CO and temperatures of 500 to 700 ℃. Under these conditions, carbon deposition is known to occur by the following reaction:
the process using this scheme can be carried out, for example, from liquid phase CO2Initiation of electrolysis to produce COGas, simultaneously with H2Electrolysis of O to produce H2And O. Then the obtained H2And CO is used to produce synthetic coal.
The present invention is based at least in part on the recognition that this ironmaking process can solve the dual objectives of providing pure raw iron and very low emission of carbon dioxide to the atmosphere under possible future greenhouse constraints, and at the same time it provides a large energy storage system that can more efficiently utilize nuclear and renewable energy sources.
Preferably, the ironmaking process comprises employing recovered solid carbon (e.g. synthetic carbon) in the direct reduction process (1) and/or the direct smelting process (2).
This use of recovered solid carbon means that the carbon is a recycled reactant in the ironmaking process and therefore the amount of solid carbonaceous material required in the process is significantly reduced compared to that used in known processes.
Preferably, the carbon recovery process utilizes electricity, particularly off-peak electricity generated from non-fossil fuels such as nuclear fuel, as an energy source.
Preferably, the off-gas separation nuclear collection process (3) produces no CO2Is used to remove the waste gas rich stream.
Especially when cold oxygen is used as oxygen-containing gas in the direct smelting process (2), the offgas-rich stream may also be free of N2。
Preferably, the ironmaking process includes using an enrichment off-gas in the process. For example, there may be no CO2Is used in the direct reduction process (1) and/or the direct smelting process (2).
Preferably, the off-gas separation and collection process (3) comprises scrubbing the CO from the off-gas2。
Typically, the off-gas separation and collection process (3) comprises scrubbing with a liquid medium such as ammonia scrubbing agentScrubbing CO from exhaust gas2The ammonia detergent is, for example, aMDEA, which is commercially available from BASF Aktiengescellsraft.
The iron-containing feed material may include materials such as iron ore, partially reduced iron ore, and iron-containing waste streams (e.g., iron-containing waste streams from steel mills).
The term "melting" is herein understood to mean hot working in which a chemical reaction is carried out that reduces iron oxide to produce molten iron.
Preferably, the direct smelting process (2) is a molten bath direct smelting process which includes supplying solid feed materials and solid carbonaceous material in the form of at least partially reduced iron-containing feed material from the direct reduction process (1) to a molten bath of molten iron and slag in the direct smelting vessel, supplying an oxygen-containing gas to a space above the molten bath and smelting the partially reduced iron-containing feed material in the molten bath and producing molten iron.
The oxygen-containing gas may be oxygen, air or oxygen-enriched gas.
Preferably, the direct smelting process (2) includes providing the solid feed materials into the molten bath by injecting the solid feed materials and a carrier gas via one or more solids injection lances extending into the vessel.
The carrier gas may be any suitable gas.
Preferably, the carrier gas comprises the enriched gas stream from the off-gas separation and collection step (3).
In the case where the oxygen-containing gas is only oxygen, the enriched gas stream will be free of nitrogen. In this case, one method option is to carry out the direct melting process (2) with a carrier gas as nitrogen-free gas.
The known molten bath direct melting process (2) is generally referred to as the HIsmelt process.
In terms of producing molten iron, in steady state operation, the HIsmelt process comprises the steps of:
(a) injecting (i) an iron-containing feed, typically iron ore in powder form, and (ii) a solid carbonaceous material, typically coal and serving as a reductant and energy source for the iron ore, into a molten bath of molten iron and slag in a direct smelting vessel; and
(b) iron-containing feed material is smelted to iron in the bath.
In steady state operation of the HIsmelt process, solid feed materials in the form of iron-containing feed material and solid carbonaceous feed material, and flux, are injected into the molten bath through a plurality of lances/tuyeres which are inclined to the vertical so as to extend downwardly and inwardly through the side wall of the direct smelting vessel and into the lower region of the vessel so as to deliver at least a portion of the solid feed materials into the metal layer located in the bottom of the vessel. To promote post combustion of the reaction gases in the upper portion of the vessel, an oxygen-containing gas is injected into the upper region of the vessel by downwardly extending lances. Exhaust gas resulting from post-combustion of the reaction gas in the vessel is withdrawn from the upper part of the vessel through an exhaust gas conduit. The vessel includes refractory lined water cooled panels in the side walls and roof of the vessel and through which cooling water is continuously circulated in a continuous loop.
Preferably, the direct reduction process (1) produces a process off-gas and the process comprises separating CO from the process off-gas2And collected.
Preferably, subsequent CO collection from the direct melting process (2)2In the same way, the collected CO separated from the process off-gas from the direct reduction process (1) is subjected to2And (6) processing.
Preferably, the direct reduction process (1) comprises the steps of:
(a) providing an iron-containing feed, a solid carbonaceous material, oxygen and a fluidising gas to a fluidised bed in a direct reduction vessel and maintaining the presence of the fluidised bed in the vessel;
(b) at least partially reducing the iron-containing feed in the vessel; and is
(c) Discharging a product stream comprising the at least partially reduced iron-containing feed from the vessel.
An example of such a direct reduction process is the so-called Circofer process.
The Circofer technique is a direct reduction process that can reduce solid iron ore to 50% or higher metallization.
In reducing the iron-containing feed material to the form of iron ore fines, it is preferred that step (a) includes maintaining the average temperature in the fluidised bed in the range 850 ℃ to 1050 ℃.
Preferably step (a) comprises maintaining the average temperature in the fluidised bed at a temperature of at least 900 c, more preferably at least 950 c.
In addition, where the iron-bearing material is in the form of iron ore powder, it is preferred that the direct reduction process (1) comprises controlling the pressure in the vessel to be in the range of 1 to 10 bar absolute, and preferably in the range of 4 to 8 bar absolute.
Where the iron-containing feed material is in the form of iron ore fines, it is preferred that the fines have a particle size of less than 6 mm.
Preferably, these powders have an average particle size of 0.1 to 0.8 mm.
It is preferable that the first and second liquid crystal layers are formed of,the fluidizing gas comprising a reducing gas such as CO and H2。
Preferably, the direct reduction process (1) comprises withdrawing a product stream comprising the at least partially reduced iron-containing feed from a lower portion of the vessel.
Preferably, the product stream also includes other solids (e.g., char).
Preferably, the direct reduction process (1) comprises separating at least a portion of the other solids from the product stream.
Preferably, the direct reduction process (1) comprises returning solids separated from the product stream to the direct reduction vessel.
Preferably, the direct reduction process (1) comprises removing a waste gas stream containing entrained solids from the upper section of the vessel.
Preferably, the direct reduction process (1) comprises separating solids from the off-gas stream.
Preferably, the direct reduction process (1) comprises maintaining a circulating fluidised bed by separating entrained solids from the off-gas stream and returning solids separated from the off-gas to the vessel.
Preferably, the direct reduction process (1) comprises returning solids separated from off-gases to the lower part of the vessel.
Preferably, the direct reduction process (1) comprises treating the off-gas after the preheating step and returning at least a portion of the treated off-gas to the vessel as fluidizing gas.
Preferably, the off-gas treatment comprises (a) solids removal, (b) cooling, (c) H2O removal, (d) CO removal2One or more of (e) removing, (e) compressing, and (f) reheating.
The above description of the invention includes the separation and collection of CO from process off-gas2And sequester CO2Or from CO2The solid carbon of (2). The description also includes the option of using oxygen as the oxygen-containing gas in the direct melting process (1). The use of oxygen as the oxygen-containing gas has the significant advantage that the ironmaking process does not have to work with N when air or oxygen-enriched gas is used as the oxygen-containing gas2And (6) processing.
In view of the above, in a broad aspect, the present invention also provides an ironmaking process for producing iron using an iron-containing feed, the process comprising:
(1) a direct reduction process comprising providing an iron-containing feed into a direct reduction vessel, at least partially reducing the feed in the vessel, and producing an at least partially reduced iron-containing feed; and
(2) a direct smelting process which comprises supplying solid feed material in the form of partially reduced iron-containing feed material from the direct reduction process (1) together with (i) solid carbonaceous material and (ii) oxygen-containing gas to a direct smelting vessel in which the partially reduced iron-containing feed material is smelted and molten pig iron and slag are produced.
Preferably, the method further comprises the above-described steps for treating the off-gas produced in the direct reduction step (1) and/or the direct melting step (2).
Drawings
The invention will be further described with reference to the following drawings, in which:
fig. 1-4 are flow charts depicting various embodiments of an ironmaking process having a carbon recycling step according to the present invention.
Detailed Description
The ironmaking process shown in fig. 1 produces molten iron using an iron-containing feed material in the form of iron ore powder and includes:
(a) a direct reduction process of partially reducing solid iron ore fines in a direct reduction vessel in the form of a circofer circulating fluidized bed reactor 3; and
(2) a molten bath direct smelting process which comprises supplying (i) solid feed material in the form of partially reduced iron ore powder and solid carbonaceous material in the form of synthetic coal from reactor 3 and (ii) technical grade oxygen to direct smelting vessel 5, smelting and further reducing iron ore which has been partially reduced, and producing molten iron.
More specifically, with reference to the process flow diagram of FIG. 1, (i) a solid feed from reactor 3 inthe form of a partially reduced iron ore powder and (ii) a gas, i.e. by scrubbing CO from the off-gas2The oxygen and rich gas formed are supplied to the Circofer circulating fluidized bed reactor 3 and a fluidized bed is established in the reactor 3.
The above-mentioned supply of solids and gas produces the following reactions in the reactor 3:
the coal volatilizes to char, and the coal volatiles decompose to gaseous products (e.g., H)2And CO), andand at least a portion of the char and/or synthetic coal reacts with oxygen to form CO.
By gaseous products CO and H2The iron ore is directly reduced to at least partially reduced iron ore. These reactions in turn produce CO2And H2O。
Part of CO2With carbon from char and/or synthetic coal to form CO (Boudouard reaction).
Oxidation reactions of solids and gases, e.g. char, synthetic coal and partially reduced iron ore particles, coal volatiles, CO and H2An oxidation reaction with oxygen, which generates heat and promotes the controlled agglomeration of smaller partially reduced iron ore particles with other particles in the fluidized bed.
The above-described direct reduction process also produces an off-gas stream which is discharged from reactor 3 through outlet 27 in the upper portion of reactor 3.
Passing the exhaust stream through CO2Scrubber 29 and divides into two streams, i.e. CO2A stream and a rich gas stream.
As mentioned above, mainly CO and H2Is supplied to the reactor 3 as part of the fluidizing gas for the process.
CO2The stream is supplied to CO2Storing the assembly 31 and compressed to a liquid phase and stored as the liquid phase.
Then, the liquid CO is introduced2Provided to a char recovery plant 33 and processed into synthetic coal.The energy required by the carbon recovery plant is in the form of off-peak electrical energy generated from a non-fossil fuel energy source, such as nuclear fuel.
As described above, synthetic coal is provided and used in a direct reduction process. As described below, synthetic coal is also provided and used in the direct fusion process.
The above-described direct reduction process produces a solid stream comprising at least partially reduced iron ore fines and char, which is discharged from reactor 3 through an outlet 25 in the bottom of reactor 3.
The solid stream produced in the direct reduction process is supplied to the direct smelting vessel 5 and more specifically to the molten bath in the vessel 5. Under static conditions when no smelting process is being carried out on the vessel, the molten bath comprises a layer of molten iron 11 and a layer of slag 13.
In addition, (i) other solid feeds, i.e. synthetic coal and flux, and (ii) gas, i.e. cold oxygen, are supplied to the vessel 5.
The vessel 5 is for example a HIsmelt vessel of the kind described in chinese patent application 01111247.6. The entire contents of which are incorporated herein by reference.
Generally, in the context of the present invention, the HIsmelt vessel 5 is a vertical vessel having: a hearth including a bottom and sides formed of refractory bricks; side walls forming a substantially cylindrical cylinder extending upwardly from a side of the furnace and including an upper cylindrical portion and a lower cylindrical portion; a top portion; an outlet for exhaust gases; an outlet for continuous discharge of molten metal andperiodic discharge of slag. The vessel 5 is equipped with downwardly extending gas injection lances 7 for delivering oxygen into the upper portion of the vessel and a plurality of solids injection lances 9 extending downwardly and inwardly through the side walls of the vessel into the slag layer 13 for injecting partially reduced iron ore fines and coal, synthetic coal and fluxes from the reactor 3 into the molten iron layer 11.
Partially reduced iron ore is smelted in a molten bath.
The direct melting process described above also produces a waste gas stream that is discharged from vessel 5 through outlet 17 in the upper portion of vessel 5.
The exhaust stream is passed through CO2Scrubber 19 and is divided into two gas streams, i.e. CO2A stream and a rich gas stream.
As mentioned above, mainly CO and H2Is supplied to the reactor 3 as part of the fluidizing gas for the direct reduction process.
CO2The stream is supplied to CO2Storing the assembly 31 and compressed to a liquid phase and stored as the liquid phase.
Thereafter, the liquid CO is introduced as described above2Provided to a char recovery plant 33 and processed into synthetic coal.
Thereafter, as described above, the synthetic coal is provided and used in direct melting and direct reduction processes.
The process shown in FIG. 2 is the same as the process of FIG. 1, except that CO from a source is used2The rich gas of the scrubber serves as a carrier gas for supplying the partly reduced iron ore fines and char from the reactor 3 to the vessel 5 through the solids injection lances 9.
Figure 3 is a variation of the above embodiment which involves injecting preheated oxygen-enriched gas into the vessel 5 through the lance 7 instead of cold oxygen. In this case, the exhaust gas from the smelting process is supplied to the exhaust heat recovery system 40. The exhaust gas is used as fuel gas and is combusted with air. The resulting flue gas is then scrubbed in the FGD plant 50 using a lime-containing material as a scrubbing agent to remove SO2. Will result to be essentially free of SO2Is fed to CO2Scrubber 60 for CO2And (6) recovering. For scrubbing CO2An alternative to (a) is to use an ammonia wash process, such as the aMDEA process available from BASF Aktiengescellshaft. The obtained CO is subjected to2Is supplied to the storage unit 31 and is then processed in the char recovery plant 33 as before.
Figure 4 is another variation which involves the use of an iron ore preheater 70. This differs from the fluidized bed in fig. 1-3 in that it does not have any carbon supply and only performs a moderate pre-reduction (typically 10% oxygen scavenging from the ore). Thus, significantly more reduction work is performed in the smelting vessel 5 and the metal output (for example for a given furnace size) reflects this.
As in each of the previous embodiments, through a waste heat recoverer 40, an FGD plant 50 and CO2The scrubber 60 treats the exhaust gas from the furnace. The obtained CO is subjected to2Supplied to the storage unit 31 and processed in the carbon recovery plant 33 as before.
Various modifications may be made to the embodiments of the invention shown in fig. 1 to 4 without departing from the spirit and scope of the invention.
Claims (28)
1. An ironmaking process for producing iron from an iron-containing feed, the process comprising:
(1) a direct reduction process comprising providing an iron-containing feed to a direct reduction vessel, at least partially reducing a feedstock in the vessel, and producing an at least partially reduced iron-containing feed;
(2) a direct smelting process that includes supplying solid feed material in the form of partially reduced iron-containing feed material from the direct reduction process (1) to a direct smelting vessel together with (i) solid carbonaceous material and (ii) oxygen-containing gas, smelting the partially reduced iron-containing feed material in the vessel, and producing molten pig iron, slag and process off-gas; and
(3) separation and collection of CO from process off-gas2And not released to the atmosphere.
2. The method of claim 1, wherein the off-gas collection and separation process (3) comprises sequestration of CO obtained from the off-gas2。
3. The method of claim 1, wherein the off-gas collection and separation process (3) comprises collecting CO from the collected CO2For example to synthesisSolid carbon in the form of coal.
4. The method of claim 3, further comprising using intermittently available non-fossil energy sources to remove CO from the collected CO2For example in the form of synthetic coal.
5. The method of claim 3 or 4, further comprising reusing in the method solid carbon recovered in the off-gas collection and separation process (3) and using the carbon as a reductant in the method.
6. The method defined in claim 5 includes recycling the recovered solid carbon in an amount that is at least 50% of the initial solid reductant used in the direct smelting process (1).
7. The method of any one of claims 3 to 6, comprising using the recovered solid carbon, for example in the form of synthetic coal, in the direct reduction process (1) and/or the direct smelting process (2).
8. The method of any one of claims 4 to 7, wherein the carbon recovery process employs electrical energy, in particular off-peak electrical energy generated from non-fossil fuels, such as nuclear fuels, as an energy source.
9. The method according to any one of the preceding claims, wherein the off-gas separation and collection process (3) produces an off-gas rich stream, in which CO is present2Is removed.
10. The method of claim 9, comprising using off-gas rich gas in the direct reduction process (1) and/or the direct smelting process (2).
11. The method defined in any one of the preceding claims wherein the off-gas separation and collection process (3) includes scrubbing CO from the off-gas2。
12. The method of claim 11, wherein the off-gas separation and collection process comprises using a liquid medium, such as ammonia scrubber, to remove CO from the off-gas2And washing off.
13. The method defined in any one of the preceding claims wherein the direct smelting process (2) is a molten bath direct smelting process which includes supplying solid feed materials and solid carbonaceous material in the form of at least partially reduced iron-containing feed material from the direct reduction process (1) to a molten bath of molten iron and slag in the direct smelting vessel, supplying oxygen-containing gas to a space above the molten bath and smelting the partially reduced iron-containing feed material in the molten bath and producing molten iron.
14. The process of claim 13 wherein the oxygen-containing gas is oxygen, air or oxygen-enriched air.
15. The method defined in claim 13 or claim 14 wherein the direct smelting process (2) includes injecting the solid feed materials and the carrier gas through one or more solids injection lances that extend into the vessel to provide the solid feed materials to the molten bath.
16. The method of claim 15, wherein the carrier gas comprises the rich gas stream from the off-gas separation and collection step (3).
17. The method of any one of the preceding claims, wherein the direct reduction process (1) produces a process off-gas and the direct reduction process comprises passing the collected CO2Separated from the process off-gas.
18. The method of claim 17, wherein the CO subsequently collected from the direct smelting process (2) is subsequently condensed2In the same way, the collected CO separated from the process off-gas from the direct reduction process (1) is subjected to2And (6) processing.
19. The method of any one of the preceding claims, wherein the direct reduction process (1) comprises the steps of:
(a) providing an iron-containing feed, a solid carbonaceous material, oxygen, and a fluidizing gas to a fluidized bed in a direct reduction vessel and maintaining the fluidized bed in the vessel;
(b) at least partially reducing the iron-containing feed in the vessel; and is
(c) A product stream comprising the at least partially reduced iron-containing feed is withdrawn from the vessel.
20. The process defined in claim 19 wherein step (a) includes maintaining the average temperature in the fluidised bed in the range of 850 ℃ to 1050 ℃ when the iron-containing feed material is in the form of iron ore powder.
21. The method defined in claim 19 or claim 20 wherein, when the iron-bearing material is in the form of iron ore powder, the direct reduction process (1) includes controlling the pressure in the vessel to be in the range of 1-10 bar absolute, and preferably in the range of 4-8 bar absolute.
22. A process according to any one of claims 19 to 21 wherein when the iron-bearing feed material is in the form of iron ore powder, the particle size of the powder is less than 6 mm.
23. The method defined in any one of claims 19 to 22 wherein the fluidising gas includes a reducing gas, such as CO and H2。
24. The method defined in any one of claims 19 to 23 wherein the direct reduction process (1) includes withdrawing a product stream that includes the at least partially reduced iron-containing feed material from a lower part of the vessel.
25. The process defined in claim 24 wherein direct reduction process (1) includes separating at least a portion of the other solids from the product stream.
26. The process defined in claim 25 wherein the direct reduction process (1) includes returning solids separated from the product stream to the direct reduction vessel.
27. A method of making iron from an iron-bearing feed material, the method comprising:
(1) a direct reduction process comprising providing an iron-containing feed to a direct reduction vessel, at least partially reducing a feedstock in the vessel, and producing an at least partially reduced iron-containing feed; and
(2) a direct smelting process which comprises supplying a solid feed material in the form of a partially reduced iron-containing feed material from the direct reduction process (1) together with (i) solid carbonaceous material and (ii) oxygen-containing gas to a direct smelting vessel where the partially reduced iron-containing feed material is smelted and molten pig iron and slag are produced.
28. The method of claim 27, further comprising the step of treating the off-gas produced in the direct reduction step (1) and/or the direct smelting step (2).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2005902958 | 2005-06-07 | ||
| AU2005902958A AU2005902958A0 (en) | 2005-06-07 | An ironmaking process |
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|---|---|
| CN1876849A true CN1876849A (en) | 2006-12-13 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011017995A1 (en) * | 2009-08-14 | 2011-02-17 | 中冶赛迪工程技术股份有限公司 | Method for reusing outlet coal gas as reducing gas in direct reduction process |
| CN104017923A (en) * | 2014-06-18 | 2014-09-03 | 汪春雷 | Ironmaking method and ironmaking furnace system |
-
2006
- 2006-06-07 CN CN 200610091218 patent/CN1876849A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011017995A1 (en) * | 2009-08-14 | 2011-02-17 | 中冶赛迪工程技术股份有限公司 | Method for reusing outlet coal gas as reducing gas in direct reduction process |
| CN104017923A (en) * | 2014-06-18 | 2014-09-03 | 汪春雷 | Ironmaking method and ironmaking furnace system |
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Application publication date: 20061213 |