WO2022264667A1 - 塊成鉱の製造方法、還元鉄の製造方法、塊成鉱、焼結機及びペレット焼成炉 - Google Patents
塊成鉱の製造方法、還元鉄の製造方法、塊成鉱、焼結機及びペレット焼成炉 Download PDFInfo
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- WO2022264667A1 WO2022264667A1 PCT/JP2022/017432 JP2022017432W WO2022264667A1 WO 2022264667 A1 WO2022264667 A1 WO 2022264667A1 JP 2022017432 W JP2022017432 W JP 2022017432W WO 2022264667 A1 WO2022264667 A1 WO 2022264667A1
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- reduction
- ore
- sintering
- iron
- agglomerate
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 138
- 238000005245 sintering Methods 0.000 title claims abstract description 98
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 80
- 239000008188 pellet Substances 0.000 title claims description 95
- 238000010304 firing Methods 0.000 title claims description 57
- 230000009467 reduction Effects 0.000 claims abstract description 119
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims abstract description 109
- 239000002994 raw material Substances 0.000 claims abstract description 86
- 229910052742 iron Inorganic materials 0.000 claims abstract description 37
- 238000000034 method Methods 0.000 claims description 31
- 239000002028 Biomass Substances 0.000 claims description 18
- 239000000701 coagulant Substances 0.000 claims description 17
- 239000000446 fuel Substances 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 136
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 32
- 239000001257 hydrogen Substances 0.000 abstract description 31
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 29
- 238000006722 reduction reaction Methods 0.000 description 121
- 235000013980 iron oxide Nutrition 0.000 description 44
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 30
- 229910002091 carbon monoxide Inorganic materials 0.000 description 30
- 230000000052 comparative effect Effects 0.000 description 12
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 6
- 239000003345 natural gas Substances 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 4
- 239000003830 anthracite Substances 0.000 description 4
- 238000001354 calcination Methods 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000002803 fossil fuel Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- 235000013162 Cocos nucifera Nutrition 0.000 description 1
- 244000060011 Cocos nucifera Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000002801 charged material Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000009770 conventional sintering Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000003780 insertion Methods 0.000 description 1
- 230000037431 insertion Effects 0.000 description 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-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
- 238000011068 loading method Methods 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 230000032258 transport Effects 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 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
- C21B13/10—Making spongy iron or liquid steel, by direct processes in hearth-type furnaces
- C21B13/105—Rotary hearth-type furnaces
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0046—Making spongy iron or liquid steel, by direct processes making metallised agglomerates or iron oxide
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/16—Sintering; Agglomerating
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/16—Sintering; Agglomerating
- C22B1/20—Sintering; Agglomerating in sintering machines with movable grates
-
- 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
-
- 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
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
-
- 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
- Y02P10/20—Recycling
Definitions
- the present invention relates to an agglomerated ore manufacturing method, a reduced iron manufacturing method, an agglomerated ore, a sintering machine, and a pellet firing furnace.
- Methods for producing iron by reducing raw materials containing iron oxide include the blast furnace method, which uses coke as a reducing agent to produce hot metal, and the vertical furnace method, which uses reducing gas as a reducing agent. ), a method in which fine ore is reduced in a fluidized bed with reducing gas, and a method in which raw material agglomeration and reduction are integrated (rotary kiln method).
- a reducing gas mainly composed of carbon monoxide (CO) or hydrogen (H 2 ) produced by reforming natural gas or coal is used as a reducing agent.
- the raw material used and charged into the furnace is heated by convective heat transfer with the reducing gas and reduced, and then discharged out of the furnace.
- Oxidized gases such as water (H 2 O) and carbon dioxide (CO 2 ), and H 2 gas and CO gas that did not contribute to the reduction reaction are discharged from the furnace.
- the raw material (mainly Fe 2 O 3 ) charged into the furnace undergoes reduction reactions represented by the following equations (1) and (2) from CO gas and H 2 gas, which are reducing gases.
- Fe 2 O 3 + 3CO ⁇ 2Fe + 3CO 2 (1)
- Iron ore and agglomerated ore obtained by agglomerating fine-grained iron ore are mainly used as raw materials charged into the furnace.
- the agglomerated ore for example, sintered ore produced by sintering fine-grained iron ore using a sintering machine, and pellets obtained by granulating fine-grained iron ore into spherical shapes and firing the pellets are used.
- the temperature In the process of producing these agglomerates, the temperature must normally be 1200° C. or higher. Therefore, in the sintering manufacturing process, finely powdered coal or coke is charged together with iron ore as a coagulant, and the heat of combustion is utilized.
- combustion heat of fossil fuels such as coal and natural gas is used to raise the temperature of the atmosphere.
- Equation (2) the amount of reduction reaction by H 2 shown in Equation (2) should be increased.
- Reduction reactions with CO and H 2 differ in the amount of heat generated or absorbed during the reaction. That is, the heat of reduction reaction by CO is +6710 kcal/kmol (Fe 2 O 3 ), while the heat of reduction reaction by H 2 is ⁇ 22800 kcal/kmol (Fe 2 O 3 ). That is, the former is an exothermic reaction, whereas the latter is an endothermic reaction.
- Patent Document 1 discloses a method of preheating raw materials charged from above to 100°C or higher and 627°C or lower in advance.
- Patent Document 1 requires equipment for preheating raw materials, which increases manufacturing costs.
- a method of raising the temperature of the reducing gas instead of preheating the raw material is also conceivable, but excessively raising the temperature of hydrogen, which burns at a high speed and in a wide concentration range, poses a high safety risk.
- an excessive temperature rise of the reducing gas induces deterioration of gas permeability in the furnace and dischargeability of raw materials due to melting of charged materials in the reducing furnace. Therefore, there is a limit to thermal compensation due to the temperature rise of the reducing gas.
- the present invention has been made in view of the above problems, and an object of the present invention is to provide an agglomerate ore that can efficiently produce reduced iron by hydrogen reduction without preheating the raw material or raising the temperature of the reducing gas.
- the gist and configuration of the present invention are as follows.
- a method for producing an agglomerate ore comprising sintering a sintering raw material containing an iron-containing raw material and a cohesive agent in a sintering machine to form a sintered cake, and crushing the sintered cake to obtain an agglomerate ore.
- a reducing gas is passed through the sintered cake on the sintering machine to reduce the iron oxide contained in the sintered cake, and the iron oxide contained in the agglomerate ore after crushing is reduced to 50%.
- the sintering machine includes a sintering unit that sinters the sintering raw material to form the sintered cake, and a reducing unit that circulates the reducing gas through the sintered cake.
- a method for producing an agglomerate ore comprising granulating an iron-containing raw material into raw pellets and firing the raw pellets in a pellet sintering furnace to obtain an agglomerate ore, On the pellet firing furnace, reducing gas is circulated through the pellets before reduction after firing to reduce the iron oxide contained in the iron-containing raw material, and the reduction rate of iron oxide contained in the agglomerate ore after reduction is determined.
- Reduced iron is obtained by reducing iron oxide contained in the agglomerate ore produced by the method for producing agglomerate ore according to any one of [1] to [7] above. Production method.
- a sintering unit for sintering a sintering raw material containing an iron-containing raw material and a cohesive material to form a sintered cake; a reduction unit for reducing iron oxide contained in the sintered cake by circulating a reducing gas through the sintered cake; a sintering machine.
- a sintering unit that sinteres raw pellets containing an iron-containing raw material to obtain pre-reduction pellets; a reduction unit that reduces iron oxide contained in the iron-containing raw material by circulating a reducing gas through the pre-reduction pellets; a pellet firing furnace.
- BRIEF DESCRIPTION OF THE DRAWINGS It is a figure which shows the outline
- BRIEF DESCRIPTION OF THE DRAWINGS It is a figure which shows the outline
- the present invention provides a process for reducing agglomerate ore as a pre-process of obtaining reduced iron by introducing a reducing gas containing hydrogen as a main component into a reducing furnace and reducing iron oxide contained in the agglomerate ore with the reducing gas. It relates to a manufacturing method.
- the present inventors diligently studied a technique for reducing the amount of CO 2 emitted when producing agglomerate ore for producing reduced iron.
- the present inventors have solved the problem of the endothermic reaction of the iron ore reduction reaction with hydrogen by a method that does not preheat the agglomerate ore in order to efficiently produce reduced iron from the agglomerate ore using hydrogen.
- pellets made by baking fine ore into a spherical shape are used.
- agglomerates called sintered ore obtained by sintering raw materials with a device called a sintering machine may also be used.
- firing pellets the temperature is generally raised to 1300° C.
- sintering sintered ore the temperature is generally raised to around 1250° C.
- the pellets and sintered ore are collectively referred to as "agglomerate ore".
- the agglomerate ore produced as described above must be transported to the facility (site) where it will be used.
- the temperature of agglomerate ore is about 1260° C. for pellets and 800 to 1200° C. for sintered ore. Therefore, when the agglomerate ore is conveyed by a belt conveyor or the like, the belt may be burned. Therefore, conventionally, produced agglomerates such as pellets or sintered ores are charged into a device called a cooler, the sensible heat of the agglomerates is recovered, and then transported to the site. The recovered sensible heat is used, for example, in boilers.
- the inventors of the present invention conceived of using the sensible heat of the agglomerate ore after production, which was conventionally recovered by a cooler, as a heat source for the reduction reaction with H 2 , and completed the present invention. of.
- the sensible heat obtained during the production of the agglomerate ore to be charged into the reduction furnace is also used for the reduction reaction of iron oxide in the process of producing the agglomerate ore. If the agglomerate ore thus produced is reduced with hydrogen in a reducing furnace, reduced iron can be efficiently produced by hydrogen reduction without the need for preheating the raw material and raising the temperature of the reducing gas.
- FIG. 1 shows an outline of a sintering machine 100. As shown in FIG. As shown in FIG. 1 , the sintering machine 100 has a sintering section 10 and a reducing section 11 .
- the sintering raw material obtained by mixing the iron-containing raw material and the coagulant is charged onto the pallet 12 of the sintering section 10 via the charging hopper 14 and the drum feeder 15 .
- the charged sintering raw material forms a raw material charged layer on the pallet 12 .
- the sintering raw material in the raw material charging layer begins to be sintered when the coagulant in the uppermost layer is ignited by the ignition furnace, forming a combustion zone.
- the combustion zone descends in the raw material charging layer as the pallet 12 moves. Then, the sintering raw material is sintered in the combustion zone to form a lump of sintered ore called a sinter cake.
- a reducing section 11 is provided downstream of a sintering section 10 that sinters the sintered cake, and reducing gas is circulated in the reducing section 11 to reduce iron oxide contained in the sintered cake.
- the sensible heat of the sintered cake is used to increase the reduction rate of iron oxide contained in the sintered cake so that the reduction rate of iron oxide in the agglomerated ore to be a product is 50% or more.
- the sintered cake is discharged out of the sintering machine 100, and after being crushed, the sintered cake is appropriately sized to obtain an agglomerated ore as a product.
- the produced agglomerate ore is conveyed to a reducing furnace for production of reduced iron, and iron oxide contained in the agglomerate ore is reduced to obtain reduced iron.
- the iron oxide contained in the sintered cake is reduced by introducing the reducing gas, so that the reduction rate of the iron oxide contained in the produced agglomerate ore is 50% or more.
- reduced iron can be efficiently produced by hydrogen reduction without preheating the agglomerate ore as a raw material and raising the temperature of the reducing gas.
- the “reduction rate of iron oxide contained in the agglomerate ore” refers to the case where it is assumed that all of the total iron (T.Fe) contained in the agglomerate ore is Fe 2 O 3 is an index representing the ratio of the amount of oxygen (% by mass) derived from iron oxide contained in the agglomerate ore to the amount (% by mass) of oxygen derived from Fe 2 O 3 in the agglomerate ore.
- the type of reducing gas is not particularly limited, it is preferably a gas containing hydrogen as a main component.
- a gas containing hydrogen as a main component means a gas in which the content of hydrogen in the reducing gas is 50% by volume or more.
- the content of H 2 contained in the reducing gas is preferably 70% by volume or more.
- the reducing gas it is preferable to circulate the reducing gas from the bottom side of the sintered cake. Since the raw material charging layer is sintered from the upper layer, and the bottom layer is sintered on the most downstream side of the sintering unit 10, the temperature is higher on the lower side (pallet 12 side) than the upper side of the sintered cake. is assumed. Therefore, by circulating the reducing gas from the lower side of the sintered cake, the iron oxide in the sintered cake can be reduced more efficiently. In the example of FIG. 1, it is preferable to pass the reducing gas through the sintered cake from the bottom of the pallet 12 .
- the sensible heat of the sintered cake is used for reduction, so there is no need to preheat the reducing gas to be introduced.
- the temperature of the reducing gas to be introduced is not particularly limited, but in one example, it can be 0° C. or higher and 100° C. or lower.
- the temperature of the reducing gas is measured, for example, by a thermometer installed at the inlet of the reducing gas.
- the introduction amount of the reducing gas is not particularly limited as long as the above reduction rate can be achieved, but can be, for example, 280 Nm 3 /t-agglomerate or more.
- the upper limit of the introduction amount of reducing gas is preferably 560 Nm 3 /t-agglomerate or less from the viewpoint of production cost.
- the introduction amount of the reducing gas is measured by, for example, a gas flow meter installed at the reducing gas introduction port.
- the upper limit of the residence time is not particularly limited, but from the viewpoint of productivity, the residence time is preferably 3600 seconds or less.
- the residence time can be calculated by dividing the length of the reducing section 11 on the sintering machine 100 in the moving direction of the pallet 12 by the moving speed of the pallet 12 .
- the reducing gas used to reduce the sintered cake may optionally be collected above the sintered cake.
- the recovered reducing gas is subjected to dehydration, dust removal, CO 2 removal, etc., optionally added with additional reducing gas, and then recirculated from the bottom of the pallet to the sintered cake.
- the coagulant is not particularly limited, and biomass raw materials, anthracite coal, coke, etc. can be used.
- the coagulant preferably contains a biomass raw material.
- biomass which is a carbon-neutral fuel
- the biomass raw material used as the coagulant is not particularly limited, examples thereof include charcoal and coconut shell charcoal.
- the coagulant preferably contains 50% by mass or more of the biomass raw material.
- the coagulant may contain 100% by mass of biomass raw material.
- the iron-containing raw material is not particularly limited, but may be, for example, iron ore, sintered return ore, blast furnace dust, steelmaking dust, rolling scale, and the like.
- the iron - containing raw material may include SiO2 , Al2O3 , CaO, MgO, etc., as well as iron oxides such as Fe2O3 and FeO.
- the mixing ratio of the iron-containing raw material and the coagulant is not particularly limited, either, and may be as known.
- the sintering machine 100 used in the method for producing agglomerate ore according to the present embodiment sinters a sintering raw material containing an iron-containing raw material and a cohesive material to form a sintered cake. and a reduction unit 11 for reducing iron oxide contained in the sintered cake by circulating a reducing gas through the sintered cake.
- the sintering unit 10 includes a charging hopper 14 for charging the sintering raw material, a drum feeder 15, a pallet 12 for conveying and sintering the sintering raw material, and loading the sintering raw material on the pallet 12.
- An igniter that ignites the upper end of the charged raw material layer, a wind box 17 that sucks air in the raw material charged layer charged in the pallet 12 downward, and the like can be provided.
- the reduction section 11 is provided downstream of the sintering section 10 .
- the reducing section 11 is provided downstream of the sintering section 10, so that the reduction of the sintered cake on the sintering machine 100 is made possible.
- the sintered cake is loaded into the reducing section 11 on a continuous pallet 12 .
- the reducing section 11 has a reducing gas introducing section 13 for circulating the reducing gas into the sintered cake on the pallet 12 . It is preferable that the reducing gas introduction part 13 is provided at the lower part of the pallet 12 in order to allow the reducing gas to flow from the lower side of the sintered cake. In order to sufficiently reduce the iron oxide in the sintered cake, it is preferable that a plurality of reducing gas inlets 13 are provided below the pallet 12 . Moreover, the reducing section 11 preferably includes a reducing gas recovery section 16 in order to recover the reducing gas used for reducing the sintered cake. In addition, as described above, since the reduction section 11 performs reduction using the sensible heat of the sintered cake, the reduction section 11 does not need to be provided with a heating device.
- FIG. 2 shows an outline of the method for producing agglomerate ore using a pellet kiln, particularly an outline of the pellet production process by the straight grate method.
- Raw pellets obtained by granulating the iron-containing raw material in advance are charged from the charging hole 22 onto the traveling grate 23 of the firing section 20 of the pellet firing furnace 200 .
- the raw pellets after charging move in the furnace together with the traveling grate 23 .
- the firing gas is gradually passed through the raw pellets to dry and fire the raw pellets.
- the pre-reduced pellets after firing are cooled on the downstream side of the firing section 20 and discharged out of the furnace.
- reducing gas is circulated in the pre-reduction pellets after sintering in the reduction unit 21 provided downstream of the sintering unit 20, thereby reducing the iron oxide contained in the agglomerate ore after sintering.
- the agglomerate ore is discharged out of the pellet firing furnace 200 to obtain a product.
- the type of reducing gas to be circulated to the pre-reduction pellets is not particularly limited, and can be the same as in the first embodiment.
- the reducing gas can be circulated from above or below the pellets before reduction. This is because, unlike the first embodiment, the pre-reduction pellets are uniformly heated in the present embodiment. Note that FIG. 2 shows an example in which the reducing gas is introduced from below the pellets before reduction. As in the first embodiment, optionally the circulated reducing gas may be recovered and circulated again.
- the sensible heat of the pellets before reduction is used for reduction, so there is no need to preheat the reducing gas to be introduced.
- the temperature of the reducing gas to be introduced is not particularly limited, but in one example, it can be 0° C. or higher and 100° C. or lower.
- the temperature of the reducing gas is measured, for example, by a thermometer installed at the inlet of the reducing gas.
- the introduction amount of the reducing gas is not particularly limited as long as the above reduction rate can be achieved, but can be, for example, 280 Nm 3 /t-agglomerate or more.
- the term “Nm 3 /t-agglomerate” is a unit indicating the introduction amount (Nm 3 ) of reducing gas per unit weight (ton) of agglomerate.
- the upper limit of the introduction amount of the reducing gas is preferably 560 Nm 3 /t-agglomerate or less from the viewpoint of production cost.
- the introduction amount of the reducing gas is measured by, for example, a gas flow meter installed at the reducing gas introduction port.
- the residence time is not particularly limited, but from the viewpoint of productivity, the residence time is preferably (3600 s or less). can be calculated by dividing by the moving speed of the traveling grate 23.
- the iron-containing raw material for forming the raw pellets is not particularly limited, and can be the same as in Embodiment 1.
- a high-temperature firing gas is introduced into the raw pellets.
- the firing gas for example, a mixture of the combustion gas of the firing fuel and air can be used.
- the firing fuel for adjusting the ambient temperature of the firing gas is not particularly limited, and a biomass raw material, natural gas, or the like can be used.
- the firing fuel preferably contains a biomass raw material.
- fossil fuels such as natural gas and coal have been used as firing fuels, and a certain amount of CO 2 has been emitted.
- CO 2 emissions can be further suppressed by using biomass, which is a carbon-neutral fuel, as the firing fuel.
- biomass raw material those exemplified in the first embodiment can be used.
- the firing fuel preferably contains 50% by mass or more of the biomass raw material.
- the firing fuel may contain 100% by mass of biomass raw material.
- the pellet firing furnace 200 used in the method for producing an agglomerate ore according to the present embodiment includes a firing section 20 that transports and fires raw pellets containing iron-containing raw materials to obtain pre-reduction pellets. and a reduction section 21 for reducing iron oxide contained in the iron-containing raw material by circulating a reducing gas through the pellets before reduction.
- the sintering unit 20 like a known pellet sintering machine, includes an insertion hole 22 for inserting raw pellets, a traveling grate 23 for conveying and sintering the raw pellets, and a gas for sintering to flow through the raw pellets.
- a firing gas introduction unit, a firing gas recovery unit for recovering and reintroducing the firing gas, a firing gas heating unit for heating the firing gas, and the like may be provided.
- the reduction section 21 is provided downstream of the baking section 20 .
- the pre-reduced pellets after sintering are cooled downstream of the sintering section 20 and discharged out of the furnace.
- the pellets before reduction on the pellet burning furnace 200 can be reduced.
- Pellets are preferably introduced into the reduction section 21 on a continuous traveling grate 23 .
- the reduction section 21 has a reduction gas introduction section for circulating the reduction gas into the pellets before reduction on the traveling grate 23 .
- the reducing section 21 preferably includes a reducing gas recovery section. Further, as described above, since the reduction section 21 performs reduction using the sensible heat of the pellets before reduction, the reduction section 21 does not need to be provided with a heating device. Between the firing section 20 and the reducing section 21, a partition may be provided to appropriately separate the atmosphere.
- the reduction rate of iron oxide contained in the agglomerate produced by the present agglomerate production method is 50% or more.
- reduced iron can be efficiently produced by hydrogen reduction without preheating the agglomerate ore as a raw material and raising the temperature of the reducing gas.
- the reduction rate of iron oxide contained in the agglomerate ore is preferably 50% or more, more preferably 55% or more.
- the upper limit of the reduction rate of the iron oxide contained in the agglomerate ore is not particularly limited. can be:
- Reduced iron can be obtained by reducing the iron oxide contained in the agglomerate ore produced by the method for producing agglomerate ore described above.
- a known reducing furnace can be used for reducing the iron oxide contained in the agglomerate ore.
- the type of the reducing furnace is not particularly limited, and it may be a shaft furnace or a blast furnace.
- FIG. 3 shows an overview of the production of reduced iron using a shaft furnace. As shown in FIG.
- a raw material charging device 30 for charging an agglomerate ore is arranged in the upper part of the shaft furnace 300 .
- a raw material charging device 30 supplies the agglomerate ore to the upper part of the furnace.
- a reducing gas is introduced into the furnace.
- the agglomerate ore charged into the furnace is heated by heat exchange with the reducing gas, and the iron oxide contained in the agglomerate ore is reduced to become reduced iron.
- the reduced agglomerate ore is discharged out of the furnace from the lower part of the furnace.
- the reduction rate of iron oxide contained in the agglomerate ore produced using the agglomerate ore production method described above is 50% or more. Therefore, even if a gas containing hydrogen as a main component is used as the reducing gas to be introduced into the reducing furnace, the effect of heat absorption due to the hydrogen reduction reaction is small, and reduced iron can be efficiently produced.
- a gas containing hydrogen as a main component means a gas in which the content of hydrogen in the reducing gas is 50% by volume or more.
- the content of H 2 contained in the reducing gas is preferably 70% by volume or more. Since a hydrogen-based gas can be used as the reducing gas, CO2 emissions can also be reduced.
- the present method for producing reduced iron preheating of the agglomerate ore as a raw material and raising of the temperature of the reducing gas introduced into the furnace are not required. Therefore, according to the present method for producing reduced iron, reduced iron can be produced safely without increasing the production cost.
- the iron oxide contained in the product reduced iron is reduced by hydrogen reduction without preheating the raw material agglomerate ore and without raising the temperature of the reducing gas introduced into the furnace.
- the percentage can be 90% or more, preferably 95% or more.
- the “reduction rate of iron oxide contained in product reduced iron” is Fe 2 O 3 when it is assumed that all of the total iron content (T.Fe) contained in product reduced iron is Fe 2 O 3 It is an index representing the ratio of the amount of oxygen (% by mass) derived from iron oxide contained in product reduced iron to the amount (% by mass) of oxygen derived from iron oxide.
- an agglomerate ore is produced using a sintering machine and a pellet sintering furnace, and reduced iron is produced in a shaft furnace using the agglomerate ore as a raw material. manufactured.
- the reducing gas used in the pre-reduction was pure H 2 .
- the shaft furnace as shown in Fig. 3, the agglomerate ore was charged from the top of the furnace without preheating, and pure H2 was used as the reducing gas.
- the temperature of pure H2 was set to the same level as in the case of using a mixed gas of CO and H2 as the reducing gas.
- Table 1 shows a list of results of operations performed to confirm the effectiveness of the method for producing agglomerate ore according to the present embodiment.
- Table 1 shows a list of results of operations performed to confirm the effectiveness of the method for producing agglomerate ore according to the present embodiment.
- CO 2 emissions ratio the ratio of CO 2 emissions in each operation to the CO 2 emissions of Comparative Example 1 is indicated as "CO 2 emissions ratio”.
- Table 2 shows the composition of the agglomerate before charging into the shaft furnace and the pre-reduction rate in each example.
- the product reduction rate and the reduction rate of the agglomerate ore (pre-reduction rate) in Tables 1 and 2 are all derived from Fe 2 O 3 in the product reduced iron or the total amount of iron in the agglomerate ore in each operation.
- the ratio of the amount of oxygen derived from iron oxide actually contained in the product reduced iron or agglomerate ore to the amount of oxygen derived from Fe 2 O 3 is expressed as a percentage.
- all iron is T.I. Fe
- metallic iron is M.I. It is called Fe.
- the results of each operation are briefly explained below.
- Comparative Examples 1 and 2 are the results of operations using agglomerates produced by conventional methods. That is, in Comparative Example 1, sintered ore produced with a conventional sintering machine was used as agglomerate ore, and in Comparative Example 2, pellets produced with a conventional pellet firing furnace were charged into a shaft furnace as agglomerate ore, and hydrogen This is the result of an operation in which reduced iron was produced by reduction. As shown in Table 1, Comparative Examples 1 and 2 emitted a certain amount of CO 2 because anthracite coal or natural gas was used as the coagulant in the sintering machine or as the firing fuel in the pellet firing furnace.
- Examples 1 and 2 are the results of operations using the agglomerate ore produced by the method for producing agglomerate ore according to the present embodiment. That is, in Example 1, sintered ore produced by a method of pre-reduction by circulating reducing gas after sintering in a sintering machine was used as agglomerated ore, and in Example 2, reducing gas was circulated after sintering in a pellet calcining furnace. Agglomerate ore is pellets produced by pre-reduction method. Each agglomerate ore was charged into a shaft furnace and reduced iron was produced by hydrogen reduction. At that time, the operation was performed so that the pre-reduction rate of the agglomerate ore was 50%.
- Examples 3 and 4 are results of operations using the agglomerate ore produced by the agglomerate production method according to the present embodiment. That is, in Example 3, sintered ore produced by a method of pre-reduction by circulating reducing gas after sintering in a sintering machine was used as agglomerated ore, and in Example 4, reducing gas was circulated after sintering in a pellet calcining furnace. The agglomerate ore was produced by pre-reducing the pellets. Each produced agglomerate ore was charged into a shaft furnace to produce reduced iron by hydrogen reduction.
- Example 3 and 4 the operation was performed so that the reduction rate of iron oxide contained in the agglomerate ore was 50%.
- anthracite and natural gas were used as the coagulant in the sintering machine or as the firing fuel in the pellet firing furnace, so more CO 2 was emitted than in Examples 1 and 2. did.
- the reduction rate of the product reduced iron was 95%, which was higher than the standard value, and it was confirmed that the shaft furnace could be operated using pure H2 as the reducing gas.
- Comparative Examples 3 and 4 are the results of operations in which agglomerate ore was produced by adopting only some of the production conditions of the method for producing agglomerate ore according to the present embodiment, and the agglomerate ore was used. That is, in Comparative Example 3, sintered ore produced by a method of pre-reduction by circulating reducing gas after sintering in a sintering machine was used as agglomerated ore, and in Comparative Example 4, reducing gas was circulated after sintering in a pellet calcining furnace. This is the result of an operation in which pellets produced by a method of pre-reduction were charged as agglomerate ore into a shaft furnace, and reduced iron was produced by hydrogen reduction.
- REFERENCE SIGNS LIST 100 sintering machine 10 sintering section 11 reducing section 12 pallet 13 reducing gas introduction section 14 charging hopper 15 drum feeder 16 reducing gas recovery section 17 wind box 200 pellet firing furnace 20 firing section 21 reducing section 22 charging hole 23 traveling grate 300 shaft furnace 30 raw material charging device
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Abstract
Description
Fe2O3 + 3CO → 2Fe + 3CO2 … (1)
Fe2O3 + 3H2 → 2Fe + 3H2O … (2)
前記焼結機上にて前記焼結ケーキに還元ガスを流通させて、前記焼結ケーキに含まれる酸化鉄を還元し、破砕後の前記塊成鉱に含まれる酸化鉄の還元率を50%以上とする、塊成鉱の製造方法。
前記ペレット焼成炉上にて、焼成後の還元前ペレットに還元ガスを流通させて、前記鉄含有原料に含まれる酸化鉄を還元し、還元後の塊成鉱に含まれる酸化鉄の還元率を50%以上とする、塊成鉱の製造方法。
前記焼結ケーキに還元ガスを流通させて、前記焼結ケーキに含まれる酸化鉄を還元する還元部と、
を備える、焼結機。
前記還元前ペレットに還元ガスを流通させて前記鉄含有原料に含まれる酸化鉄を還元する還元部と、
を備える、ペレット焼成炉。
<実施形態1>
まず、本発明の実施形態1に係る塊成鉱の製造方法について説明する。本実施形態においては、鉄含有原料および凝結材を含む焼結原料を焼結する焼結機上にて、焼結時の顕熱を利用して、焼結ケーキを還元し、酸化鉄の還元率が50%以上となった塊成鉱を得る。図1は、焼結機100の概略を示している。図1に示すように、焼結機100は、焼結部10と、還元部11とを有する。
次に、本発明の実施形態2に係る塊成鉱の製造方法について説明する。本実施形態においては、鉄含有原料を造粒して得た生ペレットを焼成するペレット焼成機上にて、焼成時の顕熱を利用して、還元前ペレットを還元し、酸化鉄の還元率が50%以上となった塊成鉱を得る。図2に、ペレット焼成炉を用いた塊成鉱の製造方法の概要、特にストレートグレート法によるペレット製造工程の概略を示す。事前に鉄含有原料を造粒して得た生ペレットを、装入孔22からペレット焼成炉200の焼成部20のトラベリンググレート23上に装入する。装入後の生ペレットはトラベリンググレート23とともに炉内を移動する。その過程で、生ペレットに徐々に焼成用ガスを流通させて、生ペレットの乾燥及び焼成が行われる。
本塊成鉱の製造方法により製造される塊成鉱に含まれる酸化鉄の還元率は、50%以上である。これにより、原料となる塊成鉱の予熱の及び還元ガスの昇温を必要とせず、水素還元により還元鉄を効率的に製造することができる。塊成鉱に含まれる酸化鉄の還元率は、好ましくは50%以上、より好ましくは55%以上である。塊成鉱に含まれる酸化鉄の還元率の上限は特に限定されないが、塊成鉱製造工程において塊成鉱製造後の顕熱を使い切る以上に還元させることは効率が悪いという理由から、65%以下であり得る。
上述した塊成鉱の製造方法を用いて製造した塊成鉱に含まれる酸化鉄を還元して還元鉄を得ることができる。塊成鉱に含まれる酸化鉄の還元には、公知の還元炉を用いることができる。還元炉の種類は特に限定されず、シャフト炉の他、高炉であってもよい。上述したように、本製造方法によれば、塊成鉱に含まれる酸化鉄が部分還元されていることから、原料予熱の及び還元ガスの昇温を必要とせず、水素還元により還元鉄を効率的に製造することができる。図3に、シャフト炉を用いた還元鉄の製造の概要を示す。図3に示すように、シャフト炉300の上部には、塊成鉱を装入するための原料装入装置30が配設される。原料装入装置30は炉上部へと塊成鉱を供給する。還元ガスを炉内に導入する。炉内に装入後の塊成鉱は、還元ガスとの熱交換により昇温され、塊成鉱に含まれる酸化鉄が還元されて還元鉄となる。還元された塊成鉱は、炉下部から炉外へ排出される。
10 焼結部
11 還元部
12 パレット
13 還元ガス導入部
14 装入ホッパー
15 ドラムフィーダ
16 還元ガス回収部
17 ウインドボックス
200 ペレット焼成炉
20 焼成部
21 還元部
22 装入孔
23 トラベリンググレート
300 シャフト炉
30 原料装入装置
Claims (11)
- 鉄含有原料および凝結材を含む焼結原料を焼結機にて焼結して焼結ケーキとし、該焼結ケーキを破砕して塊成鉱を得る、塊成鉱の製造方法であって、
前記焼結機上にて前記焼結ケーキに還元ガスを流通させて、前記焼結ケーキに含まれる酸化鉄を還元し、破砕後の前記塊成鉱に含まれる酸化鉄の還元率を50%以上とする、塊成鉱の製造方法。 - 前記焼結機は、前記焼結原料を焼結して前記焼結ケーキとする焼結部と、前記焼結ケーキに前記還元ガスを流通させる還元部とを備える、請求項1に記載の塊成鉱の製造方法。
- 前記還元部にて、前記焼結ケーキの下側から前記還元ガスを導入する、請求項2に記載の塊成鉱の製造方法。
- 前記凝結材がバイオマス原料を含む、請求項1から3のいずれか1項に記載の塊成鉱の製造方法。
- 鉄含有原料を造粒して生ペレットとし、該生ペレットをペレット焼成炉にて焼成して塊成鉱を得る、塊成鉱の製造方法であって、
前記ペレット焼成炉上にて、焼成後の還元前ペレットに還元ガスを流通させて、前記鉄含有原料に含まれる酸化鉄を還元し、還元後の塊成鉱に含まれる酸化鉄の還元率を50%以上とする、塊成鉱の製造方法。 - 前記ペレット焼成炉は、前記生ペレットを焼成して前記還元前ペレットとする焼成部と、前記還元前ペレットに前記還元ガスを流通させる還元部とを備える、請求項5に記載の塊成鉱の製造方法。
- バイオマス原料を含む焼成用燃料により前記生ペレットを焼成する、請求項5または6に記載の塊成鉱の製造方法。
- 請求項1~7のいずれか1項に記載の塊成鉱の製造方法を用いて製造した塊成鉱に含まれる酸化鉄を還元して還元鉄を得る、還元鉄の製造方法。
- 酸化鉄の還元率が50%以上である、塊成鉱。
- 鉄含有原料および凝結材を含む焼結原料を焼結して焼結ケーキとする焼結部と、
前記焼結ケーキに還元ガスを流通させて、前記焼結ケーキに含まれる酸化鉄を還元する還元部と、
を備える、焼結機。 - 鉄含有原料を含有する生ペレットを焼成して還元前ペレットとする焼成部と、
前記還元前ペレットに還元ガスを流通させて前記鉄含有原料に含まれる酸化鉄を還元する還元部と、
を備える、ペレット焼成炉。
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CN202280039281.4A CN117413077A (zh) | 2021-06-17 | 2022-04-08 | 团块矿的制造方法、还原铁的制造方法、团块矿、烧结机以及球团焙烧炉 |
EP22824662.5A EP4324938A1 (en) | 2021-06-17 | 2022-04-08 | Method for producing agglomerated ore, method for producing reduced iron, agglomerated ore, sintering machine and pellet firing furnace |
AU2022292254A AU2022292254A1 (en) | 2021-06-17 | 2022-04-08 | Method for producing agglomerated ore, method for producing reduced iron, agglomerated ore, sintering machine and pellet firing furnace |
JP2022542313A JP7323075B2 (ja) | 2021-06-17 | 2022-04-08 | 塊成鉱の製造方法、還元鉄の製造方法、塊成鉱、焼結機及びペレット焼成炉 |
BR112023026090A BR112023026090A2 (pt) | 2021-06-17 | 2022-04-08 | Método para produzir minério aglomerado, método para produzir ferro reduzido, minério aglomerado, máquina de sinterização e forno de queima de pellet |
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Publication number | Priority date | Publication date | Assignee | Title |
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JPS61201739A (ja) * | 1985-03-04 | 1986-09-06 | Sumitomo Metal Ind Ltd | 焼結鉱の処理方法 |
JP2002097507A (ja) * | 2000-09-19 | 2002-04-02 | Mitsubishi Heavy Ind Ltd | 溶銑製造方法および溶銑製造装置 |
JP2003328044A (ja) * | 2002-05-09 | 2003-11-19 | Nippon Steel Corp | バイオマス炭化物を利用した焼結鉱製造方法及び下方吸引式焼結鉱製造装置 |
JP2020003123A (ja) * | 2018-06-27 | 2020-01-09 | 日本製鉄株式会社 | ドワイトロイド焼結機 |
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Publication number | Priority date | Publication date | Assignee | Title |
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JPS61201739A (ja) * | 1985-03-04 | 1986-09-06 | Sumitomo Metal Ind Ltd | 焼結鉱の処理方法 |
JP2002097507A (ja) * | 2000-09-19 | 2002-04-02 | Mitsubishi Heavy Ind Ltd | 溶銑製造方法および溶銑製造装置 |
JP2003328044A (ja) * | 2002-05-09 | 2003-11-19 | Nippon Steel Corp | バイオマス炭化物を利用した焼結鉱製造方法及び下方吸引式焼結鉱製造装置 |
JP2020003123A (ja) * | 2018-06-27 | 2020-01-09 | 日本製鉄株式会社 | ドワイトロイド焼結機 |
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