CN100366757C - Process and plant for reducing solids containing iron oxide - Google Patents
Process and plant for reducing solids containing iron oxide Download PDFInfo
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- CN100366757C CN100366757C CNB2004800208324A CN200480020832A CN100366757C CN 100366757 C CN100366757 C CN 100366757C CN B2004800208324 A CNB2004800208324 A CN B2004800208324A CN 200480020832 A CN200480020832 A CN 200480020832A CN 100366757 C CN100366757 C CN 100366757C
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- 239000007787 solid Substances 0.000 title claims abstract description 58
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 37
- 230000008569 process Effects 0.000 title claims abstract description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 71
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 claims abstract description 43
- 239000001095 magnesium carbonate Substances 0.000 claims abstract description 42
- 235000014380 magnesium carbonate Nutrition 0.000 claims abstract description 42
- 229910000021 magnesium carbonate Inorganic materials 0.000 claims abstract description 42
- 229910052742 iron Inorganic materials 0.000 claims abstract description 34
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 22
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 22
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000010438 heat treatment Methods 0.000 claims abstract description 20
- 230000002829 reductive effect Effects 0.000 claims abstract description 19
- 238000010304 firing Methods 0.000 claims description 36
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims description 32
- 230000009467 reduction Effects 0.000 claims description 20
- 239000000428 dust Substances 0.000 claims description 12
- 238000011144 upstream manufacturing Methods 0.000 claims description 7
- 238000005469 granulation Methods 0.000 claims description 6
- 230000003179 granulation Effects 0.000 claims description 6
- 238000001465 metallisation Methods 0.000 claims description 5
- 239000003638 chemical reducing agent Substances 0.000 claims description 2
- 238000005304 joining Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 230000004907 flux Effects 0.000 claims 1
- 239000000463 material Substances 0.000 claims 1
- -1 iron ore Chemical compound 0.000 abstract 1
- 239000002912 waste gas Substances 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- 235000013980 iron oxide Nutrition 0.000 description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000000654 additive Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 230000006866 deterioration Effects 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 238000011946 reduction process Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000006872 improvement 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
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
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Classifications
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- 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
- C22B5/00—General methods of reducing to metals
- C22B5/02—Dry methods smelting of sulfides or formation of mattes
- C22B5/18—Reducing step-by-step
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/008—Use of special additives or fluxing agents
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0086—Conditioning, transformation of reduced iron ores
-
- 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
- C22B1/24—Binding; Briquetting ; Granulating
- C22B1/248—Binding; Briquetting ; Granulating of metal scrap or alloys
-
- 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
- C22B5/00—General methods of reducing to metals
- C22B5/02—Dry methods smelting of sulfides or formation of mattes
- C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
- C22B5/14—Dry methods smelting of sulfides or formation of mattes by gases fluidised 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Mechanical Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Dispersion Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Manufacture Of Iron (AREA)
Abstract
This invention relates to a process for reducing solids containing iron oxide, such as iron ore, in which fine-grained solids are heated and at least partly calcined in a pre heating stage (2, 9). In a first fluidized-bed reactor (14) downstream of the preheating stage (2, 9), the solids are prereduced and reduced further in a second fluidized-bed reactor (16). Downstream of the second reactor (16) a briquetting stage (20) is pro vided, in which the solids are briquetted at a temperature above 500 DEG C To increase the energy efficiency of the process and improve the flowability of the solids in the briquetting stage (20), magnesite is added to the preheating stage (2, 9) together with the solids containing iron oxide, which magnesite is at least partly calcined in the preheating stage (2, 9) to obtain magnesium oxide. Furthermore, the invention relates to a corresponding plant.
Description
Technical field
The present invention relates to the solid of reduction of iron oxide-containing; especially the method and apparatus of iron ore; wherein in preheating and/or firing section, heat also the solid of the meticulous granulation of roasting at least in part; tentatively reduction in the first class bed bioreactor in preheating and/or firing section downstream; in second fluidized-bed reactor, reduce, and in the briquetting section of second reactor downstream at the temperatures piece that is higher than 500 ℃.
Background technology
According to DE4410093C1, known direct-reduced iron ore obtains the method for sponge iron (DRI), wherein in having first reactor of circulating fluidized bed, is tentatively reducing under 550 to 650 ℃ temperature.In second reactor with classical fluidized-bed in downstream, the gas that wherein contains the heating of hydrogen is introduced in described second reactor as being used for fluidisation purpose reductive agent, further reduces solid, so that for example product has metallization degree greater than 90%.
In the transportation of sponge iron (DRI), because security reason, for example owing to the danger of catching fire with owing to handle the reason of (formation dust) better, Tie Tong is often by briquetting.Carry out this briquetting after the iron reduction, still red-hot sponge iron great majority cooling is supplied in the briquetting device simultaneously.Yet,, wish under for example about 700 ℃ quite high temperature, briquetting to take place in order to increase the intensity of briquet.But under this temperature, the sponge iron of meticulous granulation has the flowability of non-constant, and this makes and is difficult to briquetting more.In order to improve the mobile of sponge iron and to guarantee good workability, before briquetting, pressure feeder by the briquetting device upstream, the magnesium oxide (MgO) of about 0.5wt% is joined in the sponge iron, magnesium oxide does not have measurable negative impact to the intensity or the stability of sponge iron briquet, but because procedure of processing cost height, so its costliness, the manufacturing cost of sponge iron briquet also raises as a result.In addition, magnesium oxide moisture absorption and by very fine ground granulation, granularity is lower than 100 microns usually, so it is difficult to store and use.
According to DE-OS1458756, the method for being produced sponge iron by ferric oxide ore also is known, wherein should quite reduce under the high temperature.For fear of the effect that is called as depression (bogging) or fouling, wherein said effect generation and solids adhering or be welded together to form aggregate in the reductive process under such high temperature, fluidized-bed sinks in the reduction reactor as a result, proposes the oxide compound or the carbonate of the magnesium of the very fine pulverizing of the about 0.05wt% of interpolation.These additives quite subtly granulation and preferred size significantly less than 297 microns, especially less than 44 microns.Yet this also causes above-described problem in the process of storage or use additive.In addition, in this method, must before reduction section, additive be joined in the iron ore with for example pressure feeder.For the device that carries out this method, this causes the rising of cost of investment.Since lower in the reduction section temperature, therefore when the carbonate of magnesium joins in the reduction section, in this currently known methods, realize the roasting of being on duty mutually.This only can remedy by long retention time, yet this is non-required equally.On the other hand, when with magnesium oxide, rather than the carbonate of magnesium these problems do not occur when joining in the reduction section.Yet this involves the above-described expensive and magnesian shortcoming that is difficult to handling property.
Summary of the invention
Therefore, the purpose of this invention is to provide the solid method and apparatus of reduction of iron oxide-containing, it is characterized in that improved flowability of product and lower energy consumption.
According to the present invention, solve this purpose by above-mentioned method, wherein with magnesite (MgCO
3) join in preheating and/or the firing section with the solid that contains ferric oxide, wherein magnesite partial roasting at least in preheating and/or firing section obtains magnesium oxide.Compare with magnesium oxide, magnesite obtains with obviously lower cost, and the result can reduce the cost of being produced briquet by sponge iron.Because magnesite partial roasting at least obtains magnesium oxide, therefore the flowability of sponge iron is improved before briquetting.Therefore also briquetting can take place at high temperature, wherein at high temperature, the mobile deterioration usually of sponge iron.With this red-hot briquetting, to compare with cold pressing block at a lower temperature, the intensity of briquet increases.
Owing in preheating and/or firing section, heat magnesite and the solid that contains ferric oxide together, therefore do not need by the heat-flash reductive agent, for example hydrogen is guaranteed the heat supply of two reactors of solid of reduction of iron oxide-containing.Therefore, the energy efficiency of heat absorption method of reducing can increase, and has been heated in preheating and/or firing section under the desired temperature of reduction because contain the solid and the magnesite of ferric oxide.
This because containing the solid and the magnesite of ferric oxide, common supply arrives preheating and/or firing section, Gu needn't add extra magnesium oxide in this solid before the pressure feeder of reactor upstream.In such a way, also saved the magnesian cost of investment of supply independently commonly used.Magnesite usually contains impurity, for example ferric oxide and/or Wingdale, and these impurity do not disturb further procedure of processing, but for the further processing of iron, partly or even required.
The energy efficiency of the inventive method can further increase, because in preheating and/or firing section, and under 400-1250 ℃ temperature, especially roasting magnesite and the solid that contains ferric oxide together under 540-1000 ℃.According to the present invention, the temperature range of roasting also can be between 1000 to about 1250 ℃.Owing to compare with currently known methods, therefore especially high temperature in preheating and/or firing section does not need usually to carry out with the heat supply of hydrogen heat absorption reducing iron oxides as the hydrogen of reductive agent by heat-flash.
According to embodiment preferred of the present invention, with the solid that contains ferric oxide join in preheating and/or the firing section greater than 50%, the granularity of preferred about 90% magnesite is between 300 microns to 3 millimeters, especially between 400 microns to 1 millimeter.For method of the present invention, also can use granularity between 1.25 to 3 millimeters magnesite.Therefore the storage of magnesite and handling property are improved, and do not have the flowability of deterioration sponge iron.In the methods of the invention, the magnesite of coarse relatively granulation or magnesium oxide are pulverized in preheating and/or firing section or in the reactor that its downstream provides.In briquetting, use magnesian appropriate degree to increase, and do not have the handling property of deterioration additive.
When between 0.1 to 5wt%, especially the magnesite of about 0.5wt% in being fed to preheating and/or firing section before and/or during when being added in the solid that contains ferric oxide, to realize especially in the briquetting section the improved flowability of sponge iron and good workability according to the present invention.Be fed to solid the briquetting section from second reactor, for example contain between 0.1 to 5wt%, the magnesium oxide of especially about 0.5wt%, described magnesium oxide obtains by roasting magnesite in preheating and/or firing section.In order further to improve the solid workability that in the briquetting section, in second reactor, is reduced, this solid can be heated to above 600 ℃ temperature with magnesium oxide in the heating zone of briquetting section upstream, especially about 700 ℃ temperature, and it can be incorporated in the briquetting section under red-hot condition.This is convenient to further be reduced in the desired energy consumption of briquetting section internal shaping.
In order to avoid forming aggregate widely in reduction process in reactor, the solid that contains ferric oxide preferably is being lower than under 700 ℃ in first and second reactors, especially is reduced under about 630 ℃.Under these temperature, the phenomenon that prior art is called depression can not take place.As a result, be fed to magnesite in preheating and/or the firing section and do not require in forming magnesian reduction section, but the flowability of sponge iron can guarantee in being fed to briquetting device the time.Therefore in reduction process, the fluidisation degree of solid in first and second reactors that contains ferric oxide is especially high, the result can occur good heat transfer and with the sound response of reductive agent.The solid that contains ferric oxide is reduced in first and second reactors, obtains the metallization degree greater than 75%, especially greater than 90% metallic iron.
Adopt the solid device of reduction of iron oxide-containing further to solve purpose of the present invention, wherein said device comprises preheating and/or firing section, constitute first and second reactors of fluidized-bed reactor separately, with the briquetting section, it is characterized in that preheating section comprises that continuous or discontinuous introducing simultaneously contains the equipment of the solid of ferric oxide and magnesite and provides heating zone in the upstream of briquetting section.Because the solid and the magnesite that contain ferric oxide are introduced together, so they heat in preheating and/or firing section, and the result does not need to guarantee that by the heat-flash reductive agent heat absorption of ferric oxide subsequently reduces desired heat.Heating zone in briquetting section upstream also makes the sponge iron of drawing from reduction reactor can be heated to for example about 700 ℃ temperature with the magnesium oxide that is obtained by magnesite, and this temperature is best for briquetting.Can reduce under the low temperature relatively, be suppressed widely so that the ferric oxide roasting forms aggregate.
It can for example be to have fixed fluidized bed fluidized-bed reactor that two reactors that are connected in series of reductive take place within it.Yet for improved heat and mass transport is provided in reduction process, at least one in two reactors should preferably have the fluidized-bed reactor of circulating fluidized bed or annular fluidized bed.
According to a preferred embodiment of the invention, the gaseous reducing agent that first and/or second reactor has a plurality of nozzles or the opening that enters the mouth heats with supply, for example hydrogen.Reductive agent also can be used for fluidisation reductive solid in reactor.
Energy efficiency according to device of the present invention can be improved, because preheating and/or firing section comprise first preheater of first cyclonic separator with downstream, Venturi (Venturi) preheater for example, with second preheater (firing section) of second cyclonic separator with downstream, first and/or second cyclonic separator links to each other with the first Venturi preheater with the conduit that is used for circulating from the isolating dust of waste gas.Therefore the dust that heats in preheating and/or firing section is used for solid and the magnesite that preheating contains ferric oxide.
With the explanation subsequently of accompanying drawing, also can find out further improvement of the present invention, advantage and possible application according to an embodiment of the present invention.Described in the accompanying drawing and/or shown in all features itself or it is any in conjunction with forming theme of the present invention, and whether be included in claim or its additional note (backreference) irrelevant with them.
Description of drawings
Unique accompanying drawing shows the process flow sheet of method and apparatus according to embodiments of the present invention.
Embodiment
In the solid method of this reduction of iron oxide-containing shown in the drawings, for example Chao Shi iron ore and magnesite (MgCO
3) be incorporated in the Venturi preheater 2 with feed line 1, contain the solid and the magnesite of ferric oxide in this dry also heating.With conduit 3, the solid that contains ferric oxide is introduced in the cyclonic separator 4 with magnesite, and the waste gas that has been full of dust is separated at this and solid.
The waste gas that is full of dust is fed to strainer 6 with conduit 5, and for example in rod-curtain precipitator or the scrubber, dust is recycled in the preheating section through conduit 7 thus.
Isolating solid is fed in the firing section 9 or second preheater that wherein burner 9a is connected thereto through conduit 8 from waste gas in cyclonic separator 4, with the described firing section 9 or second preheater, most energy is fed in this technological process.In firing section 9, solid and magnesite are preheating to for example about 850 ℃ temperature.Because this high temperature firing section 9 in, thus magnesite by roasting with acquisition magnesium oxide, it is fed in second cyclonic separator 11 through conduit 10 with the solid that contains ferric oxide.At this separate solid from the waste gas that has been full of dust, described waste gas is fed in the first Venturi preheater 2 through conduit 12.As a result, the waste gas in second cyclonic separator 11, heating and dry solid and the magnesite that contains ferric oxide in the Venturi preheater 2.
The conduit 13 of isolating solid through having the pressure feeder is fed in first reactor 14 in second cyclonic separator 11, and described first reactor 14 comprises for example circulating fluidized bed.By supply of hydrogen, the ore that contains ferric oxide of heating is tentatively reduced in first reactor 14 and in conduit 15 was incorporated into second reactor 16, described second reactor 16 can be a fixed fluidized-bed reactor.Hydrogen as the heating of reductive agent also is introduced in second reactor 16, and ferric oxide is reduced in second reactor 16 as a result.
Sponge iron with height metalization is drawn from second reactor 16 with magnesium oxide and in conduit 17 is incorporated into heating zone 18, this heat solid to about 700 ℃ temperature and under the red-hot condition in conduit 19 is incorporated into briquetting section 20.
The circulation cyclonic separator can be provided in the downstream of reactor 14 and 16, from the gas that leaves reactor, separate at this dust-like solid.In off-gas treatment sections 21, these waste gas can clean in well heater 22 and heat, and are recycled to afterwards in the reactor 14,16.
Embodiment (reducing iron ore)
In device, will have the moist iron ore of 61.2t/h of 7.8% moisture and 300kg/h granularity and be fed in the Venturi preheater 2 through conduit 1 less than the magnesite of 1mm corresponding to accompanying drawing.Dry and heat iron ore and magnesite in Venturi preheater 2, and in cyclonic separator 4 is incorporated into firing section 9, in the temperature of this heating iron ore and magnesite to 850 ℃.
Separate the 2.6t/h dust in strainer 6, it comes the isolating waste gas that is full of dust in the comfortable cyclonic separator 4, and described dust contains the magnesium oxide of 25kg/h.This dust is recycled in the preheating section through conduit 7.
Become the conduit 13 of magnesian magnesite to be incorporated in the reactor 16 that reactor 14 and reactor 14 downstreams provide with the 150kg/h roasting at the iron ore of the 54.2t/h of preheater 9 internal heating to 850 ℃ through having the pressure feeder.Under about 630 ℃ temperature, 37t/h metallization degree is provided is 91% product in reduction in reactor 14 and 16.The magnesian product that contains the metallic iron of the 34t/h that has an appointment and 150kg/h is in conduit 17 is incorporated into further heating zone 18.At this section internal heating metal iron and magnesium oxide to 700 ℃, and under the red-hot condition in conduit 19 is incorporated into briquetting section 20.
Reference numerals list
1 conduit
2 (the first) Venturi preheaters
3 conduits
4 (the first) cyclonic separators
5 conduits
6 strainers
7 conduits
8 conduits
9 firing sections (second preheater)
The 9a burner
10 conduits
11 (the second) cyclonic separators
12 conduits
13 have the conduit of pressure feeder
14 (the first) reactors
15 conduits
16 (the second) reactors
17 conduits
18 heating zones
19 conduits
20 briquetting sections
21 off-gas treatment sections
22 well heaters
Claims (14)
1. the solid method of reduction of iron oxide-containing; wherein with the solid of meticulous granulation at preheating and/or firing section (2; 9) heating and roasting at least in part in; at preheating and/or firing section (2; 9) the interior prereduction of first class bed bioreactor (14) in downstream; reduction in second fluidized-bed reactor (16); and be higher than under 500 ℃ the temperature briquetting in the briquetting section (20) in second reactor (16) downstream; it is characterized in that; magnesite is joined preheating and/or firing section (2 with the solid that contains ferric oxide; 9) in, wherein with magnesite in preheating and/or firing section (2,9) at least partial roasting to obtain magnesium oxide.
2. the process of claim 1 wherein that the solid that contains ferric oxide is an iron ore.
3. the method for claim 1, it is characterized in that with magnesite with the solid that contains ferric oxide in preheating and/or firing section (2,9), at 400-1250 ℃ roasting temperature.
4. the method for claim 3, it is characterized in that with magnesite with the solid that contains ferric oxide in preheating and/or firing section (2,9), at 540-1000 ℃ roasting temperature.
5. claim 1 or 3 method, the granularity that it is characterized in that joining greater than 50% the solid with containing ferric oxide the magnesite in preheating and/or the firing section (2,9) is 300 microns to 3 millimeters.
6. the method for claim 1, it is characterized in that 0.1 to 5wt% magnesite before being fed in preheating and/or the firing section (2,9) and/or during be added in the solid that contains ferric oxide.
7. the method for claim 1 is characterized in that containing 0.1 to 5wt% magnesium oxide from the solid that second reactor (16) is fed to the briquetting section (20).
8. the method for claim 1, it is characterized in that providing heating zone (18) in briquetting section (20) upstream, in this heating zone (18), the solid that is reduced in second reactor (16) is heated to above 600 ℃ temperature with magnesium oxide, and is introduced under red-hot condition in the briquetting section (20).
9. the method for claim 1, the solid that it is characterized in that containing ferric oxide are being lower than in first and second reactors (14,16) under 700 ℃ the temperature and are being reduced, to obtain the metallization degree greater than 75% metallic iron.
10. magnesite is as the purposes of flux material, wherein in the method for the production sponge iron briquet of aforementioned any one claim, with magnesite with the solid charging that contains ferric oxide, so that the process that is fed to the briquetting section from reduction section, increase the flowability of red-hot sponge iron.
11. be used to carry out any one the device of method of claim 1-9, this device comprises preheating and/or firing section (2,9), constitute first and second reactors (14,16) and the briquetting section (20) of fluidized-bed reactor separately, it is characterized in that, preheating and/or firing section (2,9) comprise that being used for continuous or discontinuous introducing simultaneously contains the solid of ferric oxide and the equipment of magnesite (1) and provide heating zone (18) in the upstream of briquetting section (20).
12. the device of claim 11 is characterized in that in two reactors (14,16) at least one is the fluidized-bed reactor with circulating fluidized bed and/or annular fluidized bed.
13. the device of claim 12 is characterized in that first and second reactors (14,16) have the nozzle or the inlet opening of the gaseous reducing agent of a plurality of supply heating.
14. any one device of claim 11-13, it is characterized in that, preheating and/or firing section (2,9) comprise the first Venturi preheater (2) of first cyclonic separator (4) and have second preheater (9) of second cyclonic separator (11) in downstream with downstream, first and/or second cyclonic separator (4,11) link to each other with the first Venturi preheater (2) with the conduit (5,7) that is used for circulating from the isolating dust of degree gas.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE10336676.8 | 2003-08-09 | ||
| DE10336676A DE10336676C5 (en) | 2003-08-09 | 2003-08-09 | Process and plant for the reduction of iron oxide-containing solids |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1826416A CN1826416A (en) | 2006-08-30 |
| CN100366757C true CN100366757C (en) | 2008-02-06 |
Family
ID=34129525
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004800208324A Active CN100366757C (en) | 2003-08-09 | 2004-07-16 | Process and plant for reducing solids containing iron oxide |
Country Status (9)
| Country | Link |
|---|---|
| US (1) | US20070079666A1 (en) |
| CN (1) | CN100366757C (en) |
| AU (1) | AU2004262646A1 (en) |
| BR (1) | BRPI0413371A (en) |
| CA (1) | CA2534863A1 (en) |
| DE (1) | DE10336676C5 (en) |
| EA (1) | EA011430B1 (en) |
| WO (1) | WO2005014866A2 (en) |
| ZA (1) | ZA200600898B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102009038052B4 (en) | 2009-08-19 | 2012-09-27 | Wolfgang Krumm | Smelting process by using a pre-reduced Ilmeniterzstromes and / or Hematitezstromes |
| DE102015107433A1 (en) * | 2015-05-12 | 2016-11-17 | Outotec (Finland) Oy | Process and plant for the production of calcined petroleum coke |
| DE102016103349A1 (en) * | 2016-02-25 | 2017-08-31 | Outotec (Finland) Oy | Method and device for thermal treatment of a contaminated solid |
| CN109136539B (en) * | 2018-07-05 | 2020-06-23 | 沈阳化工大学 | Integrated process of fluidized bed two-stage gasification and flash light burning magnesite |
| CN115341061B (en) * | 2021-05-13 | 2024-01-02 | 中国科学院过程工程研究所 | Method for efficiently fluidizing and reducing vanadium titano-magnetite fine powder |
| DE102021205828A1 (en) * | 2021-06-09 | 2022-12-15 | Refratechnik Holding Gmbh | Process and apparatus for producing a calcined material |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2792298A (en) * | 1954-04-09 | 1957-05-14 | Freeman Horace | Iron oxide reduction |
| DE4410093C1 (en) * | 1994-03-24 | 1995-03-09 | Metallgesellschaft Ag | Process for the direct reduction of materials containing iron oxides |
| US6277324B1 (en) * | 1997-12-20 | 2001-08-21 | Pohang Iron & Steel Co. Ltd | Apparatus for manufacturing molten pig iron and reduced iron by utilizing a fluidized bed |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3393066A (en) * | 1964-09-21 | 1968-07-16 | Exxon Research Engineering Co | Process for reduction of iron ore in staged fluid beds without bogging |
| DE1458756A1 (en) * | 1964-09-21 | 1969-02-06 | Esso Res & Engineering Company | Process for the production of sponge iron from oxidic iron ores |
| AT404735B (en) * | 1992-10-22 | 1999-02-25 | Voest Alpine Ind Anlagen | METHOD AND INSTALLATION FOR THE PRODUCTION OF LIQUID PIPE IRON OR LIQUID STEEL PRE-PRODUCTS |
| EP0630975B1 (en) * | 1993-06-19 | 1997-07-23 | Metallgesellschaft Ag | Process for the direct reducing of material containing iron oxide |
-
2003
- 2003-08-09 DE DE10336676A patent/DE10336676C5/en not_active Expired - Lifetime
-
2004
- 2004-07-08 ZA ZA200600898A patent/ZA200600898B/en unknown
- 2004-07-16 WO PCT/EP2004/007904 patent/WO2005014866A2/en active Application Filing
- 2004-07-16 CN CNB2004800208324A patent/CN100366757C/en active Active
- 2004-07-16 BR BRPI0413371-4A patent/BRPI0413371A/en not_active IP Right Cessation
- 2004-07-16 EA EA200600389A patent/EA011430B1/en not_active IP Right Cessation
- 2004-07-16 US US10/567,821 patent/US20070079666A1/en not_active Abandoned
- 2004-07-16 AU AU2004262646A patent/AU2004262646A1/en not_active Abandoned
- 2004-07-16 CA CA002534863A patent/CA2534863A1/en not_active Abandoned
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2792298A (en) * | 1954-04-09 | 1957-05-14 | Freeman Horace | Iron oxide reduction |
| DE4410093C1 (en) * | 1994-03-24 | 1995-03-09 | Metallgesellschaft Ag | Process for the direct reduction of materials containing iron oxides |
| US6277324B1 (en) * | 1997-12-20 | 2001-08-21 | Pohang Iron & Steel Co. Ltd | Apparatus for manufacturing molten pig iron and reduced iron by utilizing a fluidized bed |
Non-Patent Citations (2)
| Title |
|---|
| 流化床内铁精矿还原过程的试验研究. 齐渊洪，李殷泰.东北工学院学报，第总55期. 1988 * |
| 铁精矿流态化预还原过程的研究. 胡宾生等.炼铁，第4期. 1989 * |
Also Published As
| Publication number | Publication date |
|---|---|
| US20070079666A1 (en) | 2007-04-12 |
| DE10336676B4 (en) | 2005-09-29 |
| CN1826416A (en) | 2006-08-30 |
| CA2534863A1 (en) | 2005-02-17 |
| DE10336676C5 (en) | 2011-03-31 |
| WO2005014866A3 (en) | 2005-03-31 |
| DE10336676A1 (en) | 2005-03-17 |
| EA200600389A1 (en) | 2006-08-25 |
| AU2004262646A1 (en) | 2005-02-17 |
| EA011430B1 (en) | 2009-02-27 |
| WO2005014866A2 (en) | 2005-02-17 |
| ZA200600898B (en) | 2007-05-30 |
| BRPI0413371A (en) | 2006-10-17 |
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