CN104053791A - Method and system for production of direct reduced iron using synthesis gas with high carbon monoxide content - Google Patents
Method and system for production of direct reduced iron using synthesis gas with high carbon monoxide content Download PDFInfo
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- CN104053791A CN104053791A CN201280066978.7A CN201280066978A CN104053791A CN 104053791 A CN104053791 A CN 104053791A CN 201280066978 A CN201280066978 A CN 201280066978A CN 104053791 A CN104053791 A CN 104053791A
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- CN
- China
- Prior art keywords
- gas
- carbon monoxide
- top gas
- monoxide conversion
- described top
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Classifications
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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 present invention provides methods and systems for the production of direct reduced iron, including: removing a top gas from a direct reduction furnace; carbon monoxide shifting the top gas using a carbon monoxide shift reactor to form a carbon monoxide shifted top gas having a reduced carbon monoxide content; adding one of a coal gas, a synthesis gas, and an export gas to at least a portion of the carbon monoxide shifted top gas to form a combined gas; removing carbon dioxide from the combined gas using a carbon dioxide removal unit to form a carbon dioxide lean combined gas; and providing the carbon dioxide lean combined gas to the direct reduction furnace as a reducing gas for producing direct reduced iron after heating to reduction temperature.
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 for using the method and system of synthetic (syn) gas production DRI with high carbon monoxide (CO) content.
Background of invention
By the synthetic gas of the generations such as coal gasifying process, contain a large amount of CO, appropriate hydrogen (H
2) and oxygenant, as water vapour (H
2o) and carbonic acid gas (CO
2).The technique that oxidant level can be used according to generation synthetic gas changes.For example, if use smelting furnace-gasifier to generate synthetic gas, thereby produce molten pig as product or by product, use the intermediate product of smelting furnace gas generation pre-reduced iron and supplied with melt back furnace, and output is used for other purposes, CO from the waste gas of prereduction unit
2content can very high (> 25%).This synthetic gas can have the CO content of > 40% and approximately 15% H
2content.In order to use this synthetic gas for direct-reduction (DR), H
2/ CO ratio should approach 1.0 and CO
2be less than approximately 5%.
Used and there is about 54%CO, 30%H
2, and 11%CO
2coal gas or synthetic gas.This synthetic gas has been added to the recirculation top gas from DR stove, has carried out afterwards CO
2remove, moistening, be heated to approach reduction temperature and reaction or conversion (CO+H in the reactor of the direct upstream of DR stove
2o<=>CO
2+ H
2).Obtain having about 43%H
2with 41%CO, H
2/ CO is than the reducing gas that is 1.05, and it is applicable to the DR of iron.Adversely, Restore All gas need to flow through conversion reactor, and this needs relatively large conversion reactor.Needed high conversion reaction actuator temperature (approximately 800 degrees Celsius) has also increased equipment cost significantly.
Additive method and system conversion directly, from the high CO content output gas of smelting furnace-gasifier, are used gas afterwards in DR equipment loop (DR plant circuit).By CO
2before removing, conversion output gas in one or two reactor.At CO
2before removing, the recirculation top gas of in the future white DR stove is added to the output gas of conversion, or can be by it at CO
2after removing, add.About these method and systems, hope be at CO
2after removing, obtain having the approximately H between 2/1 to 20/1
2the gas composition of/CO ratio.First step conversion reactor is approximately 490 degrees Celsius of operations, and second stage conversion reactor moves between approximately 360 to 390 degrees Celsius.
Other method and system has been instructed similar technique, except in the future white CO
2remove the load C O of unit
2tail gas with acting on the fuel of the required steam of T.G Grammar reactor.Directly the output gas from smelting furnace-gasifier is used to conversion reactor.
Invention summary
In a plurality of exemplary, the invention provides for using and there is the coal gas of high CO content or improving one's methods and system of synthetic gas production DRI.The reducing gas obtaining has approximately 1.0 H when it enters DR stove
2/ CO ratio.Advantageously, the minimized in size of the conversion reactor using, has caused lower equipment and catalyzer cost.This is by making as realizing at the required H of DR stove
2/ CO than and the amount of the air-flow that must be converted minimizes to realize.
Conversion, from top gas or the recycle gas of DR stove, causes than the lower flow to conversion reactor relevant to existing method and system.This lower flow can be realized all above objects.Process analysis shows, for example, depends on a nitrogen content of synthetic gas, and using the volume of the gas of top gas or recycle gas conversion can be only be the approximately 60-90% of the air-flow changed when changing fresh synthetic gas.This significant reduction that means conversion reactor size and cost and catalyst volume and cost.
In an exemplary, the invention provides the method for the production of direct-reduced iron, described method comprises: from direct-reduction stove, remove top gas; Use carbon monoxide conversion reactor 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 to described direct-reduction stove, as the reducing gas for the preparation of direct-reduced iron.Described method is also included in carries out using before carbon monoxide conversion water cooler/washer cooling and clean described top gas to described top gas.Described method is further included in carries out using before carbon monoxide conversion top gas described in compressor compresses to described top gas.Optionally, described method is included in and described top gas is carried out to use carbonic acid gas to remove unit before carbon monoxide conversion from described top gas, removes carbonic acid gas.Described method is still further included in carries out using before carbon monoxide conversion top gas described in vapor preheater preheating to described top gas.Described method is still further included in carries out, before carbon monoxide conversion, steam is added to described top gas to described top gas.Described method is still further included in carries out using carbonic acid gas to remove unit after carbon monoxide conversion to described top gas remove carbonic acid gas from top gas described at least a portion.Described method is still further included in carries out after carbon monoxide conversion a kind of in coal gas, synthetic gas and output gas to join described at least a portion in top gas to described top gas.Described method is still further included in carries out using after carbon monoxide conversion top gas described in reducing gas heater heats to described top gas.Finally, described method is included in described top gas is carried out, after carbon monoxide conversion, oxygen is added to described top gas for extra heating.
In another exemplary, the invention provides the method for the production of direct-reduced iron, described method comprises: from direct-reduction stove, remove top gas; Use carbon monoxide conversion reactor 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; A kind of in coal gas, synthetic gas and output gas joined described at least a portion in the top gas of carbon monoxide conversion, to form composition gas; Use carbonic acid gas to remove unit and remove carbonic acid gas from described composition 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 is included in and described top gas is carried out to use carbonic acid gas to remove unit before carbon monoxide conversion from described top gas, removes carbonic acid 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 used for receiving ferric oxide, described ferric oxide is exposed to reducing gas, thereby by described iron oxide reduction, be reducing metal iron, 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 described top gas is carried out to carbon monoxide conversion, 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 at least a portion of the described reducing gas for the preparation of described reducing metal iron.Described system also comprises water cooler/washer, and described water cooler/washer is for cooling before described top gas is carried out to carbon monoxide conversion and clean described top gas.Described system further comprises compressor, and described compressor for compressing described top gas before described top gas is carried out to carbon monoxide conversion.Optionally, described system comprises that carbonic acid gas removes unit, and described carbonic acid gas removes unit for removed carbonic acid gas from described top gas before described top gas is carried out to carbon monoxide conversion.Described system still further comprises vapor preheater, and described vapor preheater is for top gas described in preheating before described top gas is carried out to carbon monoxide conversion.Described system still further comprises vapour source, and described vapour source for being added to described top gas by steam before described top gas is carried out to carbon monoxide conversion.Described system still further comprises that carbonic acid gas removes unit, and described carbonic acid gas removes unit for remove carbonic acid gas from top gas described at least a portion after described top gas being carried out to carbon monoxide conversion.Described system still further comprises extraneous gas source, described extraneous gas source for after described top gas being carried out to carbon monoxide conversion by coal gas, synthetic gas and a kind of the joining described at least a portion in top gas of exporting gas.Described system still further comprises reducing gas well heater, and described reducing gas well heater for heating described top gas after described top gas being carried out to carbon monoxide conversion.Finally, described system comprises source of oxygen, and described source of oxygen for being added to described top gas for extra heating by oxygen after described top gas being carried out to carbon monoxide conversion.
Accompanying drawing summary
In this article, by with reference to a plurality of accompanying drawings, illustrate and described the present invention, wherein, as required, identical Reference numeral is used in reference to identical method steps/system component, and wherein:
Fig. 1 is that explanation is of the present invention for using the schematic diagram with the coal gas of high CO content or an exemplary of the method and system that synthetic gas is produced DRI.
Detailed Description Of The Invention
With reference to Fig. 1, in an exemplary of the present invention, for using, there is the coal gas of high CO content or synthetic gas and produce the method and system 10 of DRI and comprise DR stove 12 known to a person of ordinary skill in the art, as
dR shaft furnaces etc., wherein use mainly by CO and H
2the adverse current of the reducing gas forming is come reducing iron oxides pellet, fritter and/or agglomerate.This reducing gas can be manufactured as heavy fuel oil (HFO) or other output gas as coal, liquid fuel by Sweet natural gas or other geseous fuel, solid fuel.DRI declines through DR stove 12 by gravity as motion packed bed (moving packed bed).DR stove 12 has to converge discharges section, and DRI is constantly discharged by it.
Before by compressor 18 compression, top gas 14 is left DR stove 12 near the top of DR stove 12, and is passed to cooling and cleans the water cooler/washer 16 of top gas.
Optionally, cooling, clean and the top gas 14 of compression is then passed to unwanted CO
2the CO removing 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 grades, and add steam 24 to assist CO conversion reaction.In CO conversion reactor 26, by equation (CO+H
2o<=>CO
2+ H
2), the CO in the top gas 14 of crossing by steam conversion process, to produce more H
2and CO
2, and CO still less and H
2o.This process is known to a person of ordinary skill in the art, but to be positioned at present in DR/ top gas circulation be not known to a person of ordinary skill in the art for it.
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 are at CO
2before removing, first mix with the top gas 28 of CO conversion.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
2before removing unit 30, shunt, and at CO
2remove after unit 30 and poor CO
2stream mixes.
CO is conversion, poor CO
2top gas/synthetic gas 34 is then passed to reducing gas well heater 36, there, the stream obtaining is heated to approximately 600 degrees Celsius in the first step being comprised of indirect-type well heater etc., and in the second stage being formed by oxygen injection type well heater 44 etc., be heated between approximately 800 to 1,000 degree Celsius subsequently.Optionally, a part of coal gas or synthetic gas 32,38 are at CO
2before removing unit 30, shunt, and use separately or be used in combination 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 is for extra heating, and is delivered to DR stove 12 as reducing gas 46.Similarly, in DR stove 12, by the adverse current of reducing gas 46, come reducing iron oxides pellet, fritter and/or agglomerate, described reducing gas 46 is mainly by CO and H
2form, but there is approximately 1.0 favourable H
2/ CO ratio.DRI declines through DR stove 12 by gravity as motion packed bed (moving packed bed).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) that removes unit 20 is optional.Use this CO
2removing unit 20 requires whole system 10 to have two CO
2remove unit 20 and 30, but be to provide even less CO conversion reactor 26, it has to process less flow volume.
Conventionally, method and system 10 of the present invention is particularly useful for high pressure DR shaft furnace operation, because under such condition, a large amount of CO that processed by method and system 10 of the present invention are easy to cause carbon laydown problem in DR stove 12 and overheated.The method according to this invention and system 10, reducing gas 46 has lower CO content, and carbon laydown is for example minimizing under high pressure, and has avoided overheated.Exemplary temperature and content are between approximately 800 to 1,000 degree Celsius and H
2/ CO ratio is approximately 1.0.
Although illustrate and described 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 be brought into play similar function and/or obtain similar result.All within the spirit and scope of the present invention, thereby it expects for all these type of equivalent embodiments and example, and intention is covered by following claim.
Claims (22)
1. for the production of a method for direct-reduced iron, described method comprises:
From direct-reduction stove, remove top gas;
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; And
To described direct-reduction stove, provide the described top gas through carbon monoxide conversion, as the reducing gas for the preparation of direct-reduced iron.
2. method according to claim 1, described method is also included in carries out using before carbon monoxide conversion water cooler/washer cooling and clean described top gas to described top gas.
3. method according to claim 1, described method is also included in carries out using before carbon monoxide conversion top gas described in compressor compresses to described top gas.
4. method according to claim 1, described method is also included in carries out using carbonic acid gas to remove unit before carbon monoxide conversion to described top gas remove carbonic acid gas from described top gas.
5. method according to claim 1, described method is also included in carries out using before carbon monoxide conversion top gas described in vapor preheater preheating to described top gas.
6. method according to claim 1, described method is also included in carries out before carbon monoxide conversion, steam being added in described top gas to described top gas.
7. method according to claim 1, described method is also included in carries out using carbonic acid gas to remove unit after carbon monoxide conversion to described top gas remove carbonic acid gas from top gas described at least a portion.
8. method according to claim 1, described method is also included in carries out after carbon monoxide conversion a kind of in coal gas, synthetic gas and output gas to join described at least a portion in top gas to described top gas.
9. method according to claim 1, described method is also included in carries out using after carbon monoxide conversion top gas described in reducing gas heater heats to described top gas.
10. method according to claim 1, described method is also included in carries out after carbon monoxide conversion, oxygen being added in described top gas for extra heating to described top gas.
11. 1 kinds of methods for the production of direct-reduced iron, described method comprises:
From direct-reduction stove, remove top gas;
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 joined described at least a portion in the top gas of carbon monoxide conversion, to form composition gas;
Use carbonic acid gas to remove unit and remove carbonic acid gas from described composition gas, to form poor carbonic acid gas composition gas; And
After being heated to reduction temperature, described poor carbonic acid gas composition gas is offered to described direct-reduction stove, as the reducing gas for the preparation of direct-reduced iron.
12. methods according to claim 11, described method is also included in carries out using carbonic acid gas to remove unit before carbon monoxide conversion to described top gas remove carbonic acid gas from described top gas.
13. 1 kinds of systems for the production of direct-reduced iron, described system comprises:
Direct-reduction stove, described direct-reduction stove is used for receiving ferric oxide, and described ferric oxide is exposed to reducing gas, thereby is reducing metal iron by described iron oxide reduction, and wherein said direct-reduction stove produces top gas; And
Carbon monoxide conversion reactor, described carbon monoxide conversion reactor is communicated with described direct-reduction stove fluid, for described top gas is carried out to carbon monoxide conversion, to form the top gas through carbon monoxide conversion, the described top gas through carbon monoxide conversion has the carbon monoxide content of reduction;
Wherein the described top gas through carbon monoxide conversion is recycled to described direct-reduction stove, as at least a portion of the described reducing gas for the preparation of described reducing metal iron.
14. systems according to claim 13, described system also comprises water cooler/washer, described water cooler/washer is for cooling before described top gas is carried out to carbon monoxide conversion and clean described top gas.
15. systems according to claim 13, described system also comprises compressor, described compressor for compressing described top gas before described top gas is carried out to carbon monoxide conversion.
16. systems according to claim 13, described system also comprises that carbonic acid gas removes unit, described carbonic acid gas removes unit for removed carbonic acid gas from described top gas before described top gas is carried out to carbon monoxide conversion.
17. systems according to claim 13, described system also comprises vapor preheater, described vapor preheater is for top gas described in preheating before described top gas is carried out to carbon monoxide conversion.
18. systems according to claim 13, described system also comprises vapour source, described vapour source for being added to described top gas by steam before described top gas is carried out to carbon monoxide conversion.
19. systems according to claim 13, described system also comprises that carbonic acid gas removes unit, described carbonic acid gas removes unit for remove carbonic acid gas from top gas described at least a portion after described top gas being carried out to carbon monoxide conversion.
20. systems according to claim 13, described system also comprises extraneous gas source, described extraneous gas source for after described top gas being carried out to carbon monoxide conversion by coal gas, synthetic gas and a kind of the joining described at least a portion in top gas of exporting gas.
21. systems according to claim 13, described system also comprises reducing gas well heater, described reducing gas well heater for heating described top gas after described top gas being carried out to carbon monoxide conversion.
22. systems according to claim 13, described system also comprises source of oxygen, described source of oxygen for being added to described top gas for extra heating by oxygen after described top gas being carried out to carbon monoxide conversion.
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 true CN104053791A (en) | 2014-09-17 |
| CN104053791B 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 (7)
| 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 |
| US20070238906A1 (en) * | 2006-04-07 | 2007-10-11 | Brown Christopher J | Production of dry alcohol |
| US20070245855A1 (en) * | 2006-04-24 | 2007-10-25 | Eugenio Zendejas-Martinez | 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 |
| US20110247457A1 (en) * | 2008-10-06 | 2011-10-13 | Luossavaara-Kiirunavaara Ab | Process for production of direct reduced iron |
-
2012
- 2012-02-15 KR KR1020147022821A patent/KR20140115350A/en not_active Application Discontinuation
- 2012-02-15 CN CN201280066978.7A patent/CN104053791B/en active Active
- 2012-02-15 WO PCT/US2012/025244 patent/WO2013122583A1/en active Application Filing
-
2014
- 2014-06-20 ZA ZA2014/04565A patent/ZA201404565B/en unknown
Patent Citations (7)
| 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 |
| US20070238906A1 (en) * | 2006-04-07 | 2007-10-11 | Brown Christopher J | Production of dry alcohol |
| US20070245855A1 (en) * | 2006-04-24 | 2007-10-25 | Eugenio Zendejas-Martinez | 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 |
| US20110247457A1 (en) * | 2008-10-06 | 2011-10-13 | Luossavaara-Kiirunavaara Ab | Process for production of direct reduced iron |
Also Published As
| Publication number | Publication date |
|---|---|
| ZA201404565B (en) | 2015-05-27 |
| KR20140115350A (en) | 2014-09-30 |
| WO2013122583A1 (en) | 2013-08-22 |
| CN104053791B (en) | 2015-09-30 |
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