US20020124690A1 - Process of producing a mixture of iron ore and low-temperature coke - Google Patents
Process of producing a mixture of iron ore and low-temperature coke Download PDFInfo
- Publication number
- US20020124690A1 US20020124690A1 US10/037,482 US3748202A US2002124690A1 US 20020124690 A1 US20020124690 A1 US 20020124690A1 US 3748202 A US3748202 A US 3748202A US 2002124690 A1 US2002124690 A1 US 2002124690A1
- Authority
- US
- United States
- Prior art keywords
- low
- iron ore
- granular
- reactor
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 24
- 239000000203 mixture Substances 0.000 title claims abstract description 16
- 239000000571 coke Substances 0.000 title claims abstract description 13
- 238000000034 method Methods 0.000 title claims description 11
- 239000007789 gas Substances 0.000 claims abstract description 15
- 238000003763 carbonization Methods 0.000 claims abstract description 14
- 239000003245 coal Substances 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 11
- 238000011946 reduction process Methods 0.000 claims abstract description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 4
- 230000003647 oxidation Effects 0.000 claims abstract description 4
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 4
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 4
- 239000001301 oxygen Substances 0.000 claims abstract description 4
- 239000000155 melt Substances 0.000 claims abstract description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
Definitions
- This invention relates to a process of producing a hot, granular mixture of iron ore and low-temperature coke.
- this object is solved in that granular coal and preheated granular iron ore is charged into a low-temperature carbonization reactor, in which temperatures in the range from 800 to 1050° C. are produced by supplying gas containing oxygen and by partial oxidation of the components of the coal, the granular solids being maintained in a turbulent movement and being supplied from the upper region of the reactor to a solids separator, from which a hot exhaust gas is withdrawn, that the granular iron ore is preheated by means of the hot exhaust gas, and that a hot granular mixture of iron ore and low-temperature coke is withdrawn as product from the reactor and/or from the separator.
- the low-temperature carbonization reactor may be designed e.g. as fluidized-bed reactor or as pneumatic conveyor section.
- the pressure in the low-temperature carbonization reactor lies in the range from 1 to 10 bar and preferably 2 to 7 bar.
- coal also lignite
- the coal may also contain water.
- the coal supplied to the low-temperature carbonization reactor has grain sizes up to about 10 mm and preferably up to not more than about 6 mm; the grain sizes of the iron ore lie in the range up to 10 mm and preferably up to 6 mm.
- the weight ratio Fe:C usually lies in the range from 1:1 to 2:1.
- a low-temperature carbonization reactor ( 1 ) To a low-temperature carbonization reactor ( 1 ) granular coal is supplied through line ( 2 ) and preheated granular iron ore is supplied through line ( 3 ). Air for the partial oxidation in the reactor ( 1 ) and for the fluidization and transport of the solids is supplied via line ( 5 ) and enters the reactor ( 1 ) through a distributor ( 6 ). Secondary air is supplied via line ( 4 ). In the reactor, temperatures in the range from 800 to 1050° C. and mostly 850 to 1000° C. are provided. The dwell times for the solids in the reactor ( 1 ) lie in the range from about 2 to 20 sec.
- the solids are supplied from the upper region of the reactor ( 1 ) through the passage ( 8 ) to a separator ( 9 ) designed as cyclone.
- the hot exhaust gases largely free of solids flow upwards in a suspension heat exchanger ( 10 ), to which granular iron ore is supplied from the outside through line (11).
- This iron ore is preheated in direct contact with the hot exhaust gas and supplied through line ( 12 ) to a cyclone separator ( 13 ), from where the preheated iron ore is recirculated to the reactor ( 1 ) through line ( 3 ).
- Exhaust gas is withdrawn via line ( 14 ) and is supplied to a gas cleaning not represented.
- Ore-coke mixture produced is withdrawn on the one hand from the cyclone separator ( 9 ) through line ( 15 ) and on the other hand from the lower region of the reactor ( 1 ) through line ( 16 ).
- line ( 16 ) contains coarser-grained mixture than line ( 15 ).
- a syphon ( 15 a ) expediently serves as pressure barrier.
- the solids mixture can be supplied to the further use, e.g. in a melt reduction process.
- melt reduction process is described e.g. in the U.S. Pat. Nos. 6,083,296 and 6,143,054.
- the iron ore in lines ( 15 ) and ( 16 ) is already partly reduced as compared to the ore of line ( 11 ), where usually 10 to 40% of the oxygen contained in the original iron ore have already been removed.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Dispersion Chemistry (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture Of Iron (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
Granular coal and preheated granular iron ore are charged into a low-temperature carbonization reactor, in which temperatures in the range from 800 to 1050 ° C. are produced by supplying gas containing oxygen and by partial oxidation of the components of the coal. In the low-temperature carbonization reactor, the granular solids are maintained in a turbulent movement. From the upper region of the reactor, hot exhaust gas is supplied to a solids separator. The granular iron ore is preheated by means of the hot exhaust gas and hot, granular mixture of iron ore and low-temperature coke is withdrawn as product from the reactor and/or from the separator. The low-temperature carbonization reactor may be designed as fluidized-bed reactor or as pneumatic conveyor section. The granular mixture of iron ore and low-temperature coke is suitable e.g. for a melt reduction process.
Description
- This invention relates to a process of producing a hot, granular mixture of iron ore and low-temperature coke.
- It is the object underlying the invention to produce the above-mentioned mixture in an inexpensive way. The ore-coke mixture should be suitable in particular for use in a subsequent melt reduction process.
- In accordance with the invention, this object is solved in that granular coal and preheated granular iron ore is charged into a low-temperature carbonization reactor, in which temperatures in the range from 800 to 1050° C. are produced by supplying gas containing oxygen and by partial oxidation of the components of the coal, the granular solids being maintained in a turbulent movement and being supplied from the upper region of the reactor to a solids separator, from which a hot exhaust gas is withdrawn, that the granular iron ore is preheated by means of the hot exhaust gas, and that a hot granular mixture of iron ore and low-temperature coke is withdrawn as product from the reactor and/or from the separator.
- The low-temperature carbonization reactor may be designed e.g. as fluidized-bed reactor or as pneumatic conveyor section. Usually, the pressure in the low-temperature carbonization reactor lies in the range from 1 to 10 bar and preferably 2 to 7 bar.
- Expediently, highly volatile coal, also lignite, is supplied to the low-temperature carbonization reactor. The coal may also contain water. The coal supplied to the low-temperature carbonization reactor has grain sizes up to about 10 mm and preferably up to not more than about 6 mm; the grain sizes of the iron ore lie in the range up to 10 mm and preferably up to 6 mm. In the product of iron ore and low-temperature coke, the weight ratio Fe:C usually lies in the range from 1:1 to 2:1.
- Embodiments of the process will be explained with reference to the drawing. The drawing shows a flow diagram of the process.
- To a low-temperature carbonization reactor ( 1) granular coal is supplied through line (2) and preheated granular iron ore is supplied through line (3). Air for the partial oxidation in the reactor (1) and for the fluidization and transport of the solids is supplied via line (5) and enters the reactor (1) through a distributor (6). Secondary air is supplied via line (4). In the reactor, temperatures in the range from 800 to 1050° C. and mostly 850 to 1000° C. are provided. The dwell times for the solids in the reactor (1) lie in the range from about 2 to 20 sec.
- Entrained by hot exhaust gas, the solids are supplied from the upper region of the reactor ( 1) through the passage (8) to a separator (9) designed as cyclone. The hot exhaust gases largely free of solids flow upwards in a suspension heat exchanger (10), to which granular iron ore is supplied from the outside through line (11). This iron ore is preheated in direct contact with the hot exhaust gas and supplied through line (12) to a cyclone separator (13), from where the preheated iron ore is recirculated to the reactor (1) through line (3). Exhaust gas is withdrawn via line (14) and is supplied to a gas cleaning not represented.
- Ore-coke mixture produced is withdrawn on the one hand from the cyclone separator ( 9) through line (15) and on the other hand from the lower region of the reactor (1) through line (16). Usually, line (16) contains coarser-grained mixture than line (15). A syphon (15 a) expediently serves as pressure barrier. Via line (16 a), the solids mixture can be supplied to the further use, e.g. in a melt reduction process. Such melt reduction process is described e.g. in the U.S. Pat. Nos. 6,083,296 and 6,143,054. The iron ore in lines (15) and (16) is already partly reduced as compared to the ore of line (11), where usually 10 to 40% of the oxygen contained in the original iron ore have already been removed.
- In a plant corresponding to the drawing, 170 t/h granular iron ore are supplied through line ( 11), and 142 t/h granular coal with 25.4 wt-% volatile components and 17 wt-% humidity are supplied through line (2). Through lines (4) and (5) a total of 114000 Nm3/h air enter the low-temperature carbonization reactor (1), by means of which the temperature is maintained at 950° C. Through line (16 a), 210 t/h mixture of ore and low-temperature coke are withdrawn, which mixture comprises 16 wt-% Fe2O3, 49 wt-% FeO, 28 wt-% carbon and 7 wt-% ash. The process gas withdrawn via line (14) has a temperature of 518° C. and the
composition CO 11 vol-% CO 211 vol-% H2O 22 vol-% H 215 vol-% CH 41 vol-% N2 40 vol-%
Claims (6)
1. A process of producing a hot, granular mixture of iron ore and low-temperature coke, characterized in that granular coal and preheated granular iron ore are charged into a low-temperature carbonization reactor, in which temperatures in the range from 800 to 1050° C. are produced by supplying gas containing oxygen and by partial oxidation of the components of the coal, the granular solids being maintained in a turbulent movement and being supplied from the upper region of the reactor to a solids separator from which a hot exhaust gas is withdrawn, that the granular iron ore is preheated by means of the hot exhaust gas, and that a hot, granular mixture of iron ore and low-temperature coke is withdrawn as product from the reactor and/or from the separator.
2. The process as claimed in claim 1 , characterized in that the low-temperature carbonization reactor is designed as fluidized-bed reactor or as pneumatic conveyor section.
3. The process as claimed in claim 1 or 2, characterized in that the pressure in the low-temperature carbonization reactor lies in the range from 1 to 10 bar.
4. The process as claimed in claim 1 or any of the preceding claims, characterized in that highly volatile coal is supplied to the low-temperature carbonization reactor.
5. The process as claimed in claim 1 or any of the preceding claims, characterized in that the product of iron ore and low-temperature coke has a weight ratio Fe:C of 1:1 to 2:1.
6. The process as claimed in claim 1 or any of the preceding claims, characterized in that the granular mixture of iron ore and low-temperature coke is introduced into a melt reduction process.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE10101157.1 | 2001-01-12 | ||
| DE10101157A DE10101157A1 (en) | 2001-01-12 | 2001-01-12 | Process for producing a mixture of iron ore and smoldering coke |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US20020124690A1 true US20020124690A1 (en) | 2002-09-12 |
Family
ID=7670337
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US10/037,482 Abandoned US20020124690A1 (en) | 2001-01-12 | 2002-01-04 | Process of producing a mixture of iron ore and low-temperature coke |
Country Status (4)
| Country | Link |
|---|---|
| US (1) | US20020124690A1 (en) |
| AU (1) | AU1013702A (en) |
| DE (1) | DE10101157A1 (en) |
| WO (1) | WO2002055744A2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080124253A1 (en) * | 2004-08-31 | 2008-05-29 | Achim Schmidt | Fluidized-Bed Reactor For The Thermal Treatment Of Fluidizable Substances In A Microwave-Heated Fluidized Bed |
| US20100263487A1 (en) * | 2007-12-12 | 2010-10-21 | Outotec Oyj | Process and plant for producing char and fuel gas |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10260737B4 (en) | 2002-12-23 | 2005-06-30 | Outokumpu Oyj | Process and plant for the heat treatment of titanium-containing solids |
| DE10260741A1 (en) | 2002-12-23 | 2004-07-08 | Outokumpu Oyj | Process and plant for the heat treatment of fine-grained solids |
| DE10260738A1 (en) | 2002-12-23 | 2004-07-15 | Outokumpu Oyj | Process and plant for conveying fine-grained solids |
| DE10260734B4 (en) * | 2002-12-23 | 2005-05-04 | Outokumpu Oyj | Process and plant for the production of carbon coke |
| DE10260731B4 (en) | 2002-12-23 | 2005-04-14 | Outokumpu Oyj | Process and plant for the heat treatment of iron oxide-containing solids |
| DE10260739B3 (en) | 2002-12-23 | 2004-09-16 | Outokumpu Oy | Process and plant for producing metal oxide from metal compounds |
| DE10260733B4 (en) | 2002-12-23 | 2010-08-12 | Outokumpu Oyj | Process and plant for the heat treatment of iron oxide-containing solids |
| CN101250419B (en) * | 2008-03-21 | 2011-05-25 | 西安建筑科技大学 | A kind of coal gas internal heat low-temperature dry distillation method |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2742353A (en) * | 1954-11-01 | 1956-04-17 | Exxon Research Engineering Co | Iron ore reduction process |
| SE384226B (en) * | 1974-05-20 | 1976-04-26 | Stora Kopparbergs Bergslags Ab | MAKE REDUCTION OF FINE DISTRIBUTED IRON OXIDE MATERIALS IN FLOAT BED |
| SE387366C (en) * | 1974-12-12 | 1980-04-14 | Stora Kopparbergs Bergslags Ab | SET FOR REDUCING FINALLY DISTRIBUTED METAL OXID CONTAINING MATERIAL |
| US4094665A (en) * | 1977-05-13 | 1978-06-13 | Stora Kopparbergs Bergslags Ab | Method for simultaneous combined production of electrical energy and crude iron |
| JPS5785911A (en) * | 1980-11-18 | 1982-05-28 | Ishikawajima Harima Heavy Ind Co Ltd | Direct reduction and melting method for iron oxide |
| DE3540541A1 (en) * | 1985-11-15 | 1987-05-21 | Metallgesellschaft Ag | METHOD FOR REDUCING HIGHER METAL OXIDS TO LOW METAL OXIDS |
| FI92223C (en) * | 1992-01-24 | 1994-10-10 | Ahlstroem Oy | Process for the reduction of solid phase metal oxide-containing material |
| CU23070A3 (en) * | 1999-01-12 | 2005-07-19 | Falconbridge Ltd | REDUCTION OF THE FLUDIZED LAYER OF LATERITE FINE WITH REDUCTION OF GASES GENERATED IN SITU. |
-
2001
- 2001-01-12 DE DE10101157A patent/DE10101157A1/en not_active Withdrawn
- 2001-12-18 WO PCT/EP2001/014978 patent/WO2002055744A2/en not_active Ceased
-
2002
- 2002-01-04 US US10/037,482 patent/US20020124690A1/en not_active Abandoned
- 2002-01-11 AU AU10137/02A patent/AU1013702A/en not_active Abandoned
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20080124253A1 (en) * | 2004-08-31 | 2008-05-29 | Achim Schmidt | Fluidized-Bed Reactor For The Thermal Treatment Of Fluidizable Substances In A Microwave-Heated Fluidized Bed |
| US20100263487A1 (en) * | 2007-12-12 | 2010-10-21 | Outotec Oyj | Process and plant for producing char and fuel gas |
| US9175226B2 (en) | 2007-12-12 | 2015-11-03 | Outotec Oyj | Process and plant for producing char and fuel gas |
| US9371487B2 (en) | 2007-12-12 | 2016-06-21 | Outotec Oyj | Process and plant for producing char and fuel gas |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2002055744A2 (en) | 2002-07-18 |
| AU1013702A (en) | 2002-07-18 |
| WO2002055744A3 (en) | 2004-01-08 |
| DE10101157A1 (en) | 2002-07-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU673921B2 (en) | Process for a direct reduction of iron oxide-containing materials to form FE3C | |
| US5720785A (en) | Method of reducing hydrogen cyanide and ammonia in synthesis gas | |
| US5674308A (en) | Spouted bed circulating fluidized bed direct reduction system and method | |
| US20020124690A1 (en) | Process of producing a mixture of iron ore and low-temperature coke | |
| NZ199930A (en) | A process for simultaneously producing fuel gas and process heat from carbonaceous materials | |
| US4298460A (en) | Process for processing sulfur-containing heavy oil | |
| SK279954B6 (en) | Process for decreasing n2o content in combustion gas | |
| AU679662B2 (en) | Reduction of iron oxide-containing materials with solid carbonaceous reducing agents | |
| CA2150456A1 (en) | Process and device for producing pig iron from iron ore or for thermally and/or chemically treating an easily decomposable material | |
| JPH0348245B2 (en) | ||
| AU2008252051B2 (en) | Process and plant for producing char and fuel gas | |
| AU672715B2 (en) | Process of roasting refractory gold ores | |
| AU732310B2 (en) | Method of adjusting circulating fluidized bed and use of the method | |
| AU2006201957A1 (en) | Process and plant for producing char and fuel gas | |
| US5382277A (en) | Process for reducing fine-grain iron oxide materials with a gas | |
| US6599374B1 (en) | Method for producing a mixture of iron carbide and granular, directly reduced iron | |
| AU765620B2 (en) | Process of reducing ilmenite | |
| US4416689A (en) | Process for the manufacture of crude iron and energy-rich gases | |
| AU699428B2 (en) | Direct reduction process for iron oxide-containing materials | |
| US4824655A (en) | Process for the preparation of sulphur dioxide | |
| ZA200503457B (en) | Process and plant for the heat treatment of solidscontaining titanium. | |
| AU2001265669B2 (en) | Device for directly reducing ore fine and installation for carrying out said method | |
| CN1225138A (en) | Process for producing a reduction gas for reduction of metal ore | |
| US6627171B2 (en) | Method for producing iron carbide from granulated sponge iron | |
| JPH09227875A (en) | Coal preheating method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| AS | Assignment |
Owner name: MG TECHNOLOGIES AG, GERMANY Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:ORTH, ANDREAS;HIRSCH, MARTIN;WEBER, PETER;REEL/FRAME:012556/0671 Effective date: 20020124 |
|
| STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |