CN104053791B - The synthetic gas with high carbon monoxide content is used to produce the method and system of direct-reduced iron - Google Patents
The synthetic gas with high carbon monoxide content is used to produce the method and system of direct-reduced iron Download PDFInfo
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- CN104053791B CN104053791B CN201280066978.7A CN201280066978A CN104053791B CN 104053791 B CN104053791 B CN 104053791B CN 201280066978 A CN201280066978 A CN 201280066978A CN 104053791 B CN104053791 B CN 104053791B
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- Prior art keywords
- gas
- carbon monoxide
- carbonic acid
- monoxide conversion
- top gas
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B5/00—Making pig-iron in the blast furnace
- C21B5/06—Making pig-iron in the blast furnace using top gas in the blast furnace process
-
- 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
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/24—Increasing the gas reduction potential of recycled exhaust gases by shift reactions
-
- 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
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/26—Increasing the gas reduction potential of recycled exhaust gases by adding additional fuel in recirculation pipes
-
- 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
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
- C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
-
- 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
- Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
-
- 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
- Y02P10/25—Process efficiency
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
- Manufacture Of Iron (AREA)
Abstract
The invention provides the method and system for the production of direct-reduced iron, it comprises: from direct-reduction stove, remove top gas; Carbon monoxide conversion reactor is used to carry out carbon monoxide conversion to described top gas, to form the top gas through carbon monoxide conversion of the carbon monoxide content with reduction; By coal gas, synthetic gas with to export in gas a kind of joins at least partially in the top gas of carbon monoxide conversion, to form composition gas; Use carbonic acid gas to remove unit and from described composition gas, remove carbonic acid gas, to form poor carbonic acid gas composition gas; And after being heated to reduction temperature, provide described poor carbonic acid gas composition gas, as the reducing gas for the preparation of direct-reduced iron to described direct-reduction stove.
Description
Invention field
Present invention relates in general to the method and system for the production of direct-reduced iron (DRI).More specifically, the present invention relates to the method and system for using synthesis (syn) gas with high carbon monoxide (CO) content to produce DRI.
Background of invention
The synthetic gas generated by coal gasifying process etc. contains a large amount of CO, appropriate hydrogen (H
2) and oxygenant, as water vapour (H
2and carbonic acid gas (CO O)
2).Oxidant level can change according to generating the synthetic gas technique that use.Such as, if use smelting furnace-gasifier to generate synthetic gas, thus produce molten pig as product or by product, then use the intermediate product of smelting furnace gas generation pre-reduced iron and supplied melt back furnace, and the waste gas exported from pre-reduction unit is used for other purposes, CO
2content can very high (> 25%).This synthetic gas can have the CO content of > 40% and the H of about 15%
2content.In order to use this synthetic gas for direct-reduction (DR), H
2/ CO ratio should close to 1.0 and CO
2be less than about 5%.
Use and there is about 54%CO, 30%H
2, and 11%CO
2coal gas or synthetic gas.This synthetic gas is added to the recirculation top gas from DR stove, carries out CO afterwards
2remove, moistening, be heated to close to reduction temperature and in the reactor of the direct upstream of DR stove reaction or conversion (CO+H
2o<=>CO
2+ H
2).Obtain having about 43%H
2with 41%CO, H
2/ CO is than the reducing gas being 1.05, and it is applicable to the DR of iron.Adversely, Restore All gas needs to flow through conversion reactor, and this needs relatively large conversion reactor.Required high conversion reaction actuator temperature (about 800 degrees Celsius) also significantly increases equipment cost.
Additive method and system conversion directly export gas from the high CO content of smelting furnace-gasifier, use gas afterwards in DR equipment loop (DR plant circuit).By CO
2before removing, in one or two reactor, conversion exports gas.At CO
2before removing, the recirculation top gas of white DR stove is added to the output gas of conversion in the future, or can by it at CO
2add after removing.About these method and systems, desirably at CO
2the H had between about 2/1 to 20/1 is obtained after removing
2the gas composition of/CO ratio.First step conversion reactor is about 490 degrees Celsius of operations, and second stage conversion reactor runs between about 360 to 390 degrees Celsius.
Other method and system teaches similar technique, except white CO in future
2remove the load C O of unit
2tail gas be used as the fuel of steam needed for T.G Grammar reactor.Directly conversion reactor is used to the output gas from smelting furnace-gasifier.
Invention summary
In multiple exemplary, the invention provides for using the coal gas with high CO content or synthetic gas to produce improving one's methods and system of DRI.The reducing gas obtained has the H of about 1.0 when it enters DR stove
2/ CO ratio.Advantageously, the minimized in size of the conversion reactor used, result in lower equipment and catalyzer cost.This is the H by making as realizing needed for DR stove
2/ CO ratio and the amount of the air-flow that must be converted minimize to realize.
Change the top gas from DR stove or recycle gas, cause than the lower flow to conversion reactor relevant to existing method and system.This lower flow makes all above objects to realize.Process analysis shows, such as, depends on a nitrogen content of synthetic gas, uses the volume of the gas of top gas or recycle gas conversion can be only the about 60-90% of the air-flow changed when changing fresh synthetic gas.This significant reduction meaning conversion reactor size and cost and catalyst body sum cost.
In an exemplary embodiment, the invention provides the method for the production of direct-reduced iron, described method comprises: from direct-reduction stove, remove top gas; Carbon monoxide conversion reactor is used to carry out carbon monoxide conversion to described top gas, to form the top gas through carbon monoxide conversion of the carbon monoxide content with reduction; And provide the described top gas through carbon monoxide conversion, as the reducing gas for the preparation of direct-reduced iron to described direct-reduction stove.Described method uses water cooler/washer to cool before being also included in and carrying out carbon monoxide conversion to described top gas and cleans described top gas.Described method uses top gas described in compressor compresses before being included in further and carrying out carbon monoxide conversion to described top gas.Optionally, described method uses carbonic acid gas to remove unit before being included in and carrying out carbon monoxide conversion to described top gas and remove carbonic acid gas from described top gas.Described method uses top gas described in vapor preheater preheating before being still included in further and carrying out carbon monoxide conversion to described top gas.Steam is added to described top gas before being still included in further and carrying out carbon monoxide conversion to described top gas by described method.Described method uses carbonic acid gas to remove unit and remove carbonic acid gas from described top gas at least partially after being still included in further and carrying out carbon monoxide conversion to described top gas.After described method is still included in further and carries out carbon monoxide conversion to described top gas, coal gas, synthetic gas and the one exported in gas are joined at least partially in described top gas.Described method uses top gas described in reducing gas heater heats after being still included in further and carrying out carbon monoxide conversion to described top gas.Finally, oxygen is added to described top gas after being included in and carrying out carbon monoxide conversion to described top gas and is used for extra heating by described method.
In another exemplary embodiment, the invention provides the method for the production of direct-reduced iron, described method comprises: from direct-reduction stove, remove top gas; Carbon monoxide conversion reactor is used to carry out carbon monoxide conversion to described top gas, to form the top gas through carbon monoxide conversion of the carbon monoxide content with reduction; By coal gas, synthetic gas and to export in gas a kind of join described in the top gas of carbon monoxide conversion at least partially, to form composition gas; Use carbonic acid gas to remove unit and from described composition gas, remove carbonic acid gas, to form poor carbonic acid gas composition gas; And after being heated to reduction temperature, described poor carbonic acid gas composition gas is provided to described direct-reduction stove, as the reducing gas for the preparation of direct-reduced iron.Optionally, described method uses carbonic acid gas to remove unit before being included in and carrying out carbon monoxide conversion to described top gas and remove carbonic acid gas from described top gas.
In other exemplary, the invention provides the system for the production of direct-reduced iron, described system comprises: direct-reduction stove, described direct-reduction stove is for receiving ferric oxide, described ferric oxide is exposed to reducing gas, thus be reducing metal iron by described iron oxide reduction, wherein said direct-reduction stove generates top gas; And carbon monoxide conversion reactor, described carbon monoxide conversion reactor is communicated with described direct-reduction stove fluid, for carrying out carbon monoxide conversion to described top gas, to form the top gas through carbon monoxide conversion of the carbon monoxide content with reduction; Wherein the described top gas through carbon monoxide conversion is recycled to described direct-reduction stove, as the described reducing gas for the preparation of described reducing metal iron at least partially.Described system also comprises water cooler/washer, and described water cooler/washer is used for cooling before carrying out carbon monoxide conversion to described top gas and cleaning described top gas.Described system comprises compressor further, and described compressor is used for compressing described top gas before carrying out carbon monoxide conversion to described top gas.Optionally, described system comprises carbonic acid gas and removes unit, and described carbonic acid gas removes unit for removing carbonic acid gas before carrying out carbon monoxide conversion to described top gas from described top gas.Described system still comprises vapor preheater further, and described vapor preheater is used for top gas described in preheating before carrying out carbon monoxide conversion to described top gas.Described system still comprises vapour source further, and described vapour source is used for, before carrying out carbon monoxide conversion to described top gas, steam is added to described top gas.Described system still comprises carbonic acid gas further and removes unit, and described carbonic acid gas removes unit for removing carbonic acid gas after carrying out carbon monoxide conversion to described top gas from described top gas at least partially.Described system still comprises extraneous gas source further, and described extraneous gas source is used for coal gas, synthetic gas and the one exported in gas being joined after carrying out carbon monoxide conversion to described top gas at least partially in described top gas.Described system still comprises reducing gas well heater further, and described reducing gas well heater is used for described top gas being carried out to top gas described in the post-heating of carbon monoxide conversion.Finally, described system comprises source of oxygen, and described source of oxygen is used for oxygen being added to described top gas after carrying out carbon monoxide conversion to described top gas and is used for extra heating.
Accompanying drawing is sketched
In this article, by referring to multiple accompanying drawing, illustrate and describe the present invention, wherein, as required, identical Reference numeral is used in reference to identical method steps/system component, and wherein:
Fig. 1 illustrates the schematic diagram for using the coal gas with high CO content or synthetic gas to produce an exemplary of the method and system of DRI of the present invention.
Detailed Description Of The Invention
With reference to Fig. 1, in an exemplary of the present invention, for using the method and system 10 of coal gas or the synthetic gas production DRI with high CO content to comprise DR stove 12 known to a person of ordinary skill in the art, as
dR shaft furnaces etc., wherein use primarily of CO and H
2the adverse current of the reducing gas of composition comes reducing iron oxides pellet, fritter and/or agglomerate.This reducing gas can by Sweet natural gas or other geseous fuel, solid fuel as coal, liquid fuel as heavy fuel oil (HFO) or other export gas manufacture.DRI is lowered through DR stove 12 as motion packed bed (moving packed bed) by gravity.DR stove 12 has to converge discharges section, and DRI is constantly discharged by it.
Before being compressed by compressor 18, top gas 14 leaves DR stove 12 at the near top of DR stove 12, and is passed to and cools and clean the water cooler/washer 16 of top gas.
Optionally, the top gas 14 cooling, clean and compress then is passed to unwanted CO
2the CO removed from stream
2remove unit 20.CO
2removing unit 20 can be chemotype CO
2remove unit, as monoethanolamine (MEA) or hot salt of wormwood CO
2remove unit, or it can be molecular sieve type CO
2remove unit, as pressure-variable adsorption (PSA) or Vacuum Pressure Swing Adsorption (VPSA) CO
2remove unit.
Then the top gas 14 that thermal pretreatment is crossed in vapor preheater 22 grade, and add steam 24 with auxiliary CO conversion reaction.In CO conversion reactor 26, by equation (CO+H
2o<=>CO
2+ H
2), the CO in the top gas 14 crossed by steam conversion process, to produce more H
2and CO
2, and less CO and H
2o.This process is known to a person of ordinary skill in the art, but its be positioned at present DR/ top gas circulation in be not known to a person of ordinary skill in the art.
The top gas 28 of CO conversion is then passed to CO
2remove unit 30, there, coal gas, synthetic gas (Finex waste gas etc.) etc. 32 is at CO
2first the top gas 28 changed with CO before removing mixes.Similarly, CO
2removing unit 30 can be chemotype CO
2remove unit, as MEA or hot salt of wormwood CO
2remove unit, or it can be molecular sieve type CO
2remove unit, as PSA or VPSACO
2remove unit.Optionally, the top gas 28,29 of a part of CO conversion is at CO
2shunting before removing unit 30, and at CO
2with poor CO after removing unit 30
2stream mixing.
CO is conversion, poor CO
2top gas/synthetic gas 34 is then passed to reducing gas well heater 36, there, the stream obtained is heated to about 600 degrees Celsius in the first step be made up of indirect-type well heater etc., and in the second stage be made up of oxygen injection type well heater 44 grade, be heated to about 800 to 1, between 000 degree Celsius subsequently.Optionally, a part of coal gas or synthetic gas 32,38 are at CO
2shunting before removing unit 30, and be used alone or combinationally use with top gas fuel 40, to light reducing gas well heater 36.
Optionally, then oxygen 45 is added to this heating, CO conversion, poor CO
2top gas/synthetic gas 42 for extra heating, and is delivered to DR stove 12 as reducing gas 46.Similarly, in DR stove 12, use the adverse current of reducing gas 46 to come reducing iron oxides pellet, fritter and/or agglomerate, described reducing gas 46 is primarily of CO and H
2composition, but there is the favourable H of about 1.0
2/ CO ratio.DRI is lowered through DR stove 12 as motion packed bed (moving packed bed) by gravity.DR stove 12 has to converge discharges section, and DRI is constantly discharged by it.
Similarly, an above-mentioned CO
2the use (before CO conversion) removing unit 20 is optional.Use this CO
2remove unit 20 and require that whole system 10 has two CO
2remove unit 20 and 30, but be to provide even less CO conversion reactor 26, it has to process less flow volume.
Usually, method and system 10 of the present invention is particularly useful for high pressure DR shaft furnace and runs, because in such a situa-tion, a large amount of CO processed by method and system 10 of the present invention are easy to cause the carbon laydown problem in DR stove 12 and overheated.According to method and system 10 of the present invention, reducing gas 46 has lower CO content, and carbon laydown minimizes under such as high pressure, and avoid overheated.Exemplary temperature and content are between about 800 to 1,000 degree Celsius and H
2/ CO ratio is about 1.0.
Although illustrate and describe the present invention with reference to preferred embodiment and specific embodiment thereof in this article, will it is evident that for those of ordinary skills, other embodiments and example can play similar function and/or obtain similar result.All within the spirit and scope of the present invention, thus it is expection for this type of equivalent embodiments all and example, and intention is required to cover by following patent.
Claims (18)
1., for the production of a method for direct-reduced iron, described method comprises:
Top gas is removed from direct-reduction stove;
Use carbon monoxide conversion reactor to carry out carbon monoxide conversion to described top gas, to form the top gas through carbon monoxide conversion, the described top gas through carbon monoxide conversion has the carbon monoxide content of reduction;
A kind of in coal gas, synthetic gas and output gas is joined at least partially described in the top gas of carbon monoxide conversion to form composition gas;
Use carbonic acid gas to remove unit and from described composition gas, remove carbonic acid gas to form poor carbonic acid gas composition gas; And
Described poor carbonic acid gas composition gas is provided, as the reducing gas for the preparation of direct-reduced iron to described direct-reduction stove.
2. method according to claim 1, described method uses water cooler/washer to cool before being also included in and carrying out carbon monoxide conversion to described top gas and cleans described top gas.
3. method according to claim 1, described method uses top gas described in compressor compresses before being also included in and carrying out carbon monoxide conversion to described top gas.
4. method according to claim 1, described method uses carbonic acid gas to remove unit before being also included in and carrying out carbon monoxide conversion to described top gas and remove carbonic acid gas from described top gas.
5. method according to claim 1, described method uses top gas described in vapor preheater preheating before being also included in and carrying out carbon monoxide conversion to described top gas.
6. method according to claim 1, steam is added in described top gas before being also included in and carrying out carbon monoxide conversion to described top gas by described method.
7. method according to claim 1, described method also comprises poor carbonic acid gas composition gas described in use reducing gas heater heats.
8. method according to claim 1, described method also comprises oxygen to be added in described poor carbonic acid gas composition gas and is used for extra heating.
9., for the production of a method for direct-reduced iron, described method comprises:
Top gas is removed from direct-reduction stove;
Use carbon monoxide conversion reactor to carry out carbon monoxide conversion to described top gas, to form the top gas through carbon monoxide conversion, the described top gas through carbon monoxide conversion has the carbon monoxide content of reduction;
A kind of in coal gas, synthetic gas and output gas is joined described in the top gas of carbon monoxide conversion at least partially, to form composition gas;
Use carbonic acid gas to remove unit and from described composition gas, remove carbonic acid gas, to form poor carbonic acid gas composition gas; And
After being heated to reduction temperature, described poor carbonic acid gas composition gas is supplied to described direct-reduction stove, as the reducing gas for the preparation of direct-reduced iron.
10. method according to claim 9, described method uses carbonic acid gas to remove unit before being also included in and carrying out carbon monoxide conversion to described top gas and remove carbonic acid gas from described top gas.
11. 1 kinds of systems for the production of direct-reduced iron, described system comprises:
Direct-reduction stove, described ferric oxide, for receiving ferric oxide, is exposed to reducing gas by described direct-reduction stove, thus is reducing metal iron by described iron oxide reduction, and wherein said direct-reduction stove produces top gas;
Carbon monoxide conversion reactor, described carbon monoxide conversion reactor is communicated with described direct-reduction stove fluid, for carrying out carbon monoxide conversion to described top gas, to form the top gas through carbon monoxide conversion, the described top gas through carbon monoxide conversion has the carbon monoxide content of reduction;
Extraneous gas source, described extraneous gas source be used for after carrying out carbon monoxide conversion to described top gas, the one in coal gas, synthetic gas and output gas being joined at least partially in described top gas to form composition gas; And
Carbonic acid gas removes unit, and described carbonic acid gas removes unit for removing carbonic acid gas to form poor carbonic acid gas composition gas after carrying out carbon monoxide conversion to described top gas from described composition gas;
Wherein described poor carbonic acid gas composition gas is recycled to described direct-reduction stove, as the described reducing gas for the preparation of described reducing metal iron at least partially.
12. systems according to claim 11, described system also comprises water cooler/washer, and described water cooler/washer is used for cooling before carrying out carbon monoxide conversion to described top gas and cleaning described top gas.
13. systems according to claim 11, described system also comprises compressor, and described compressor is used for compressing described top gas before carrying out carbon monoxide conversion to described top gas.
14. systems according to claim 11, described system also comprises carbonic acid gas and removes unit, and described carbonic acid gas removes unit for removing carbonic acid gas before carrying out carbon monoxide conversion to described top gas from described top gas.
15. systems according to claim 11, described system also comprises vapor preheater, and described vapor preheater is used for top gas described in preheating before carrying out carbon monoxide conversion to described top gas.
16. systems according to claim 11, described system also comprises vapour source, and described vapour source is used for being added in described top gas by steam before carrying out carbon monoxide conversion to described top gas.
17. systems according to claim 11, described system also comprises reducing gas well heater, and described reducing gas well heater is for heating described poor carbonic acid gas composition gas.
18. systems according to claim 11, described system also comprises source of oxygen, and described source of oxygen is used for oxygen to be added in described poor carbonic acid gas composition gas to be used for extra heating.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/US2012/025244 WO2013122583A1 (en) | 2012-02-15 | 2012-02-15 | Method and system for the production of direct reduced iron using a synthesis gas with a high carbon monoxide content |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104053791A CN104053791A (en) | 2014-09-17 |
| CN104053791B true CN104053791B (en) | 2015-09-30 |
Family
ID=48984559
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201280066978.7A Active CN104053791B (en) | 2012-02-15 | 2012-02-15 | The synthetic gas with high carbon monoxide content is used to produce the method and system of direct-reduced iron |
Country Status (4)
| Country | Link |
|---|---|
| KR (1) | KR20140115350A (en) |
| CN (1) | CN104053791B (en) |
| WO (1) | WO2013122583A1 (en) |
| ZA (1) | ZA201404565B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT202100030047A1 (en) * | 2021-11-29 | 2023-05-29 | Next Generation Venture S R L | PROCESS FOR THE PREPARATION OF A CATALYST USEFUL IN THE PRODUCTION OF SYNGAS |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4756750A (en) * | 1987-04-27 | 1988-07-12 | Air Products And Chemicals, Inc. | Process for the direct reduction of iron ore |
| US5676732A (en) * | 1995-09-15 | 1997-10-14 | Hylsa, S.A. De C.V. | Method for producing direct reduced iron utilizing a reducing gas with a high content of carbon monoxide |
| US6149859A (en) * | 1997-11-03 | 2000-11-21 | Texaco Inc. | Gasification plant for direct reduction reactors |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2012898A4 (en) * | 2006-04-07 | 2010-02-10 | Thermal Kinetics Systems Llc | Production of dry alcohol |
| US7608129B2 (en) * | 2006-04-24 | 2009-10-27 | Hyl Technologies S.A. De C.V. | Method and apparatus for producing direct reduced iron |
| US20100162852A1 (en) * | 2007-05-25 | 2010-07-01 | Jorge Octavio Becerra-Novoa | Method and apparatus for the direct reduction of iron ores utilizing syngas |
| SE532975C2 (en) * | 2008-10-06 | 2010-06-01 | Luossavaara Kiirunavaara Ab | Process for the production of direct-reduced iron |
-
2012
- 2012-02-15 WO PCT/US2012/025244 patent/WO2013122583A1/en active Application Filing
- 2012-02-15 KR KR1020147022821A patent/KR20140115350A/en not_active Application Discontinuation
- 2012-02-15 CN CN201280066978.7A patent/CN104053791B/en active Active
-
2014
- 2014-06-20 ZA ZA2014/04565A patent/ZA201404565B/en unknown
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4756750A (en) * | 1987-04-27 | 1988-07-12 | Air Products And Chemicals, Inc. | Process for the direct reduction of iron ore |
| US5676732A (en) * | 1995-09-15 | 1997-10-14 | Hylsa, S.A. De C.V. | Method for producing direct reduced iron utilizing a reducing gas with a high content of carbon monoxide |
| US6149859A (en) * | 1997-11-03 | 2000-11-21 | Texaco Inc. | Gasification plant for direct reduction reactors |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104053791A (en) | 2014-09-17 |
| KR20140115350A (en) | 2014-09-30 |
| ZA201404565B (en) | 2015-05-27 |
| WO2013122583A1 (en) | 2013-08-22 |
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