CN104204244A - Process and apparatus for producing hardened granules from iron-containing particles - Google Patents
Process and apparatus for producing hardened granules from iron-containing particles Download PDFInfo
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- CN104204244A CN104204244A CN201380015110.9A CN201380015110A CN104204244A CN 104204244 A CN104204244 A CN 104204244A CN 201380015110 A CN201380015110 A CN 201380015110A CN 104204244 A CN104204244 A CN 104204244A
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- fluidized
- bed reactor
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- technique
- iron
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 91
- 239000002245 particle Substances 0.000 title claims abstract description 46
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 38
- 239000008187 granular material Substances 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000004519 manufacturing process Methods 0.000 claims abstract description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 23
- 239000000203 mixture Substances 0.000 claims description 23
- 238000002156 mixing Methods 0.000 claims description 10
- 208000034189 Sclerosis Diseases 0.000 claims description 9
- 239000012298 atmosphere Substances 0.000 claims description 7
- 239000000446 fuel Substances 0.000 claims description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 238000010992 reflux Methods 0.000 claims description 2
- 238000009736 wetting Methods 0.000 claims 2
- 239000003153 chemical reaction reagent Substances 0.000 claims 1
- 238000011143 downstream manufacturing Methods 0.000 abstract description 3
- 239000011230 binding agent Substances 0.000 abstract description 2
- 238000005299 abrasion Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 16
- 239000000463 material Substances 0.000 description 13
- 239000000428 dust Substances 0.000 description 12
- 235000019580 granularity Nutrition 0.000 description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 239000003245 coal Substances 0.000 description 9
- 239000012141 concentrate Substances 0.000 description 9
- 230000002349 favourable effect Effects 0.000 description 9
- 239000011859 microparticle Substances 0.000 description 8
- 238000012545 processing Methods 0.000 description 8
- 230000002829 reductive effect Effects 0.000 description 8
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 7
- 238000005453 pelletization Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 description 5
- 239000011707 mineral Substances 0.000 description 5
- 235000010755 mineral Nutrition 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000000654 additive Substances 0.000 description 3
- 230000000996 additive effect Effects 0.000 description 3
- 239000000853 adhesive Substances 0.000 description 3
- 230000001070 adhesive effect Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001465 metallisation Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 239000013590 bulk material Substances 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000006185 dispersion Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 239000006148 magnetic separator Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000012299 nitrogen atmosphere Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 239000011435 rock Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 238000011282 treatment Methods 0.000 description 2
- 206010039509 Scab Diseases 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 239000002734 clay mineral Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- -1 excess (excess) Substances 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229910052595 hematite Inorganic materials 0.000 description 1
- 239000011019 hematite Substances 0.000 description 1
- 238000009830 intercalation Methods 0.000 description 1
- 230000002687 intercalation Effects 0.000 description 1
- 235000013980 iron oxide Nutrition 0.000 description 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 description 1
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 1
- YDZQQRWRVYGNER-UHFFFAOYSA-N iron;titanium;trihydrate Chemical compound O.O.O.[Ti].[Fe] YDZQQRWRVYGNER-UHFFFAOYSA-N 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 238000007885 magnetic separation Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229910052901 montmorillonite Inorganic materials 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- 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
- C22B1/242—Binding; Briquetting ; Granulating with binders
-
- 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
- C22B1/22—Sintering; Agglomerating in other sintering apparatus
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Carbon And Carbon Compounds (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
In the production of hardened granules from iron-containing particles, the iron-containing particles are mixed with at least one binder and water to obtain a mix, the mix is formed to granules, and the granules are introduced into a fluidized-bed reactor for hardening. To reduce the abrasion in the downstream processing stages, the still moist granules are introduced into the fluidized-bed reactor at the hottest point of the fluidized bed.
Description
The present invention relates to produce hardened granules (granule) by iron dust containing, wherein iron dust containing is mixed to obtain mixture with at least one tackiness agent and water, by mixture forming particle, particle is incorporated in fluidized-bed reactor for sclerosis, and makes the reduction of hardened granules experience.
For obtaining some reducing process of metallization iron, iron-bearing materials is introduced with fine granularity particulate (fine-grained particle) form.The example of such technique is so-called SL/RN technique, and it is the combination of Stelco-Lurgi technique and Republic Steel-National Lead technique (RN).Stelco-Lurgi technique is direct-reduction technique, and it produces and be rich in the use of the ore of iron at first for the steel stove of sponge iron.Republic Steel-National Lead technique is also direct-reduction technique, wherein iron ore is resolved into their component metals iron and gangue after reduction.In this connection, gangue is understood to the nonferrous rock existing in iron ore.By by two kinds of technique combinations, in 1964, developed SL/RN technique, wherein use solid reductant reducing iron oxides in rotary kiln.In stove, by ore or so-called green-ball (green pellets) and the excessive reductive agent that is introduced as of coal (particularly brown coal), and introduce rhombspar for desulfurization.Stove output is cooling in tubular cooler indirect, after this through sieving, magneticseparation be divided into sponge iron, excess (excess), coal and ash content separated with mineral coal.
In SL/RN technique, conventionally adopt the lump ore of granularity 5-18mm or the pelletizing of 9-16mm (pellets).Also use granularity to be preferably greater than iron sand or the ilmenite of 160 μ m.The particulate of diameter <63 μ m is not suitable for SL/RN technique, because they cause the formation that sticks (sticking) and cause thus kliner coating in rotary kiln (crusts), they can cause operation interrupted.
In order still to make this technique that is suitable for of small particle more, can form the particle with desired diameter by much technique.For example, due to processing and additive (tackiness agent), this particle can so design so that the formation of their production period dust keeps lower (<10wt-%) herein.
The particle of having known fine granularity iron ore part from WO 98/49352A1 forms, and for example wherein uses wilkinite as adhesive material.Wilkinite is the rock of the mixture that contains various clay minerals, and montmorillonite is most important component (60 to 80wt-%).
US 6,024, and 790 have described that by the cationic ion-exchange with intercalation, to activate this adhesive material wilkinite can be favourable for its desired use.The wilkinite of activation has better swelling capacity and higher thermostability conventionally.US 6,024, the activating process of describing in 790 must carry out a few hours to time of several days to guarantee enough ion-exchange.
From JP 63103851, known and added a small amount of sodium hydroxide to wilkinite, thus activated clay material.
DE 25 175 43 has disclosed the technique of agglomerate metallurgical dust, wherein metallurgical dust and 2 to 20wt-% tackiness agents and approximately 0.5 is mixed to 5wt-% material, this mixture is formed to pelletizing or particle and with post-hardening.Add further additive is also known in tackiness agent, for example the sodium hydroxide of about 3wt-% quantity, sodium carbonate and sodium bicarbonate.
From EP 1 290 232B1, known by tackiness agent by carefully produce the technique of metallization iron agglomerate containing iron granules, wherein by cellulosic fibre as tackiness agent.When forming particulate, cellulosic fibre works as tackiness agent, and still, due to their high-carbon content, they also can be used as the reductive agent in the reducing process of downstream.
EP 0 916 742 has also disclosed a kind of technique, wherein in iron content particle, introduces reductive agent.For this object, the starting material that contain ferriferous oxide are mixed with carbonaceous material, organic binder bond and inorganic coagulant, mix with water subsequently.Provide dispersion agent, the dry and reduction subsequently by thus obtained pelletizing.As dispersion agent, also can use for example sodium hydroxide solution.
Yet, due to the processing in rotary kiln, together with solid reductant and the quite long residence time, when using green-ball, in the further processing in all these techniques, particularly SL/RN technique, observed the formation of the tiny wearing and tearing that increase.High wearing and tearing just require high processing charges to can reclaim these dust, producing value product from them.Otherwise the material containing in dust has just lost.
Therefore, target of the present invention is to provide technology and equipment, to produce particle for further processing, they have such hardness to such an extent as to even in Downstream processing step, also noticeable wear can not occur.
According to the present invention, by the feature of claim 1, solved this target.Ultra-fine Fe concentrate (concentrate) is fed in mixed cell and at this place and is mixed with at least one tackiness agent and water.In addition, in this mixed cell, also can add further aggregate (aggregates).Then thus obtained mixture is formed in miniature distiller (microcoagulator) to particle.Subsequently particle is incorporated in the fluidized-bed of preferred cycle, this hottest point place that is introduced in fluidized-bed carries out.This unexpected variation of temperature caused short grained Fast Sintering and enough granule strengths of therefore causing for subsequently in the reduction of rotary kiln.In circulating fluidized bed, due to high flow rate, heat exchange especially well to such an extent as to further accelerated sintering process.
This technique is inconsistent with conventional operation, according to common process, it is to carry out in the region that material is not exposed to high thermograde that the material that will process is introduced fluidized-bed, because particularly for larger particulate, the high temperature difference can cause stress in material and breaking and being out of shape subsequently.In addition,, owing to introducing at hottest point place, just must higher requirement be proposed to the material of supply line.Therefore feed in raw material and also become more expensive.
The hottest point of fluidized-bed is positioned at burning origination point or hot gas inlet point.
In addition, found that it is favourable containing iron granules, having at least iron level of 30wt-%, preferably at least 50 to 80wt-%, to make processing charges keep economical.
Favourable aspect restriction (provide that) Fe concentrate of the present invention has maximum 5wt-% and is coarser than the granularity that 100 μ m and approximately 55 to 60wt-% are less than 32 μ m, because mean diameter is larger, directly processing may be more favourable economically.
Ultra-fine concentrate can be used as filter cake or exists as dry powder in bulk material (bulk material).The specific surface area of particulate is 1600 and 4000cm
2between/g, depend on mineralogy or the mineral composition of the iron ore concentrate that uses.Preprocessing (for example form to pulverize) may be favourable for more uniform granularity.
As tackiness agent, inorganic adhesive (for example, as wilkinite) is best suited for because thus between available hardening period the unexpected rising of temperature get rid of undesirable side reaction.According to the present invention, the addition of this tackiness agent should 0.25 and 1.5wt-% between, it depends on mineral composition and the specific surface area of iron ore concentrate in principle.
The mixture that forms particle in microparticle shaper advantageously should have 0.1 and 6mm between granularity, because this granularity has guaranteed that in fact whole particulate is homogeneous heating during being incorporated into the hottest stage of reactor, between individual particles, there is no obvious thermograde.
In addition, found that 8 to 14wt-% water-content is particularly advantageous, it depends on corresponding mineral composition in principle.
Best stiffening temperature, between 850 and 1050 ℃, equally also depends on mineral composition within the scope of this.Experiment shows, in technique according to the present invention, during heat embrittlement, the particle of maximum about 5wt-% obtains as wearing and tearing, and wherein granularity part <100 μ m is defined as wearing and tearing herein.
As the fuel of hardening process, Sweet natural gas or light-weight fuel oil can directly burnings in fluidized-bed reactor or hot gas generator.If use hot gas generator, is just supplied to fluidized-bed reactor by hot gas.
Alternatively, can use coal as fuel, wherein the temperature between 650 and 950 ℃ in independent reactor by coal, using carbonization gas as fuel, be incorporated in sclerous reaction device, and hot carbonization coke is incorporated into the downstream process stage as reductive agent, be preferably incorporated in the reduction of carrying out in rotary kiln.
Also it is favourable finding to make to be hardened in oxidizing atmosphere, the oxygen level in preferred cycle fluidized-bed 2 and 10wt-% between.As a result, the iron of oxidation stage 2 has been oxidized to the iron of oxidation stage 3 and has discharged more heat energy.Thereby can reduce the heat input in reactor.
Between the hardening period in oxygen-containing atmosphere, there is following reaction:
2Fe
3o
4+ 1/2O
2→ 3Fe
2o
3(magnetite is oxidized to rhombohedral iron ore)
Fe
2o
3x H
2o → Fe
2o
3+ H
2o (for example removal of the crystal water of pyrrhosiderite)
If, just only there is the removal that second reaction is crystal water in oxygen-free gas in atmosphere.
Subsequently the microparticle of sclerosis is processed with the reduction of coal experience in rotary kiln, wherein oxygen decomposition and the iron of ferriferous oxide are entered into metallographic phase.Ratio (C between carbon and iron
fix: Fe) be 0.3-0.7:1.Between reduction period, there is following reaction:
Fe
2O
3+CO→2FeO+CO
2
CO
2+C→2CO
FeO+CO→Fe
met+CO
2
Aspect technology realizes, seem particularly advantageously the hot particle of sclerosis not add cooling being incorporated into rotary kiln from fluidized-bed reactor.By this way, on the one hand can save energy, stove volume can be reduced on the other hand, thereby its cost of investment can be reduced.When packing particle under hot condition, just optional for the furnace length that the desired particle heating of rotary kiln is original required.Can rotary kiln be designed shortlyer or can increase the throughput of existing rotary kiln.In existing return bend system, can introduce and increase throughput by heat.Can utilize the hot waste gas of fluidized-bed reactor to carry out the essential process gas of preheating (process air) or produce steam.
Although improved sclerosis, in order to provide in fluidized-bed and reduction the dust that produces for economic use, found via dust separation system these dust are separated and to be recycled in mixed cell or particle forming unit be favourable from fluidized-bed and/or reduction phase.
Particularly under more on a small scale, for example, as in laboratory and pilot experiment, for security reason is cooled to the temperature lower than 30 ℃ by stove output, be favourable, wherein this coolingly preferably should for example, carry out under inert atmosphere (nitrogen atmosphere).The material of cooling mistake (it is the mixture of sponge iron, charcoal (char) and ash content) is encased in magnetic separator so that by sponge iron and carbon and ash separation.
In addition, the present invention includes the equipment with claim 9 feature, described equipment is suitable for implementing according to technique of the present invention.Such equipment comprises for mixing containing iron granules and at least one tackiness agent and water to obtain the device of mixture.After this device, be for mixture is carried out to the device that particle becomes particle.After this device, it is the reactor with circulating fluidized bed for hardened granules.Fluidized-bed reactor so design also leads to the hottest point place of fluidized-bed thus so that the supply line of particle leads to the lower region of fluidized-bed reactor.The feed way providing for the material of this object, particularly this supply line and this place must be designed so that it forever stands these temperature.
In research and development of the present invention, with hot gas charging fluidized-bed, particle supply line is opened in this feed pipe region, because also do not lose any heat energy to fluidized-bed at this hot gas.
When providing by the reducing apparatus in fluidized-bed reactor and/or downstream at least one reflux line of the device for mixing and/or the device that forms for microparticle, be also favourable.
According to technique of the present invention advantage on the one hand, be, up to the present only can use the pelletizing that forms and also there is in addition suitable major diameter (9 and 16mm between) by magnetite and hematite concentrate.According to technique of the present invention, also can use other Ultra-fine concentrate and other granularities, and can not obtain unmanageable dust loop.
In addition, the microparticle hardening according to the present invention has the porosity larger than lump ore, thereby can also reduce better sooner than lump ore and classical burning pelletizing (in the sclerosis over 1300 ℃).
In addition,, by combining according to sclerous reaction device of the present invention and SL/RN stove, the hot output of self-hardening stove is directly encased in rotary kiln under hot condition in the future.Thereby saved heat energy and increased the specific throughput of rotary kiln.
Finally, according to technique of the present invention, also make produced all dust, wet or dry, can be recycled to microparticle and form in technique, thereby guarantee complete totally enclosed material circulation.
Explain in detail the present invention with exemplary with reference to the accompanying drawings subsequently.All features self of describing and/or illustrating or be combined to form theme of the present invention with any, and their comprise (inclusion) or the returning of they not relying in claim drawn (back-reference).
Unique accompanying drawing has shown for implementing the schema of the equipment of technique according to the present invention.
Fine-grained iron ore is incorporated in mixing device 1.In addition at least one supply line 2 leads in this mixing device 1, introduces the mixture being at least comprised of tackiness agent and water via this pipeline.Certainly for every kind of independent additive provides supply line separately, be also possible.
Via pipeline 3, the mixture so producing is incorporated into granulated apparatus for converting 4 from mixing device 1.By mixture, formed there the particle (microparticle forms) of median size 0.1 to 6mm, via pipeline 5, be introduced in fluidized-bed reactor 10.Via pipeline 11, fluidizing agent is injected in the fluidized-bed reactor 10 that is preferably designed for circulating fluidized bed, to form circulating fluidized bed 14 on siege (grate) 13.Slightly surpassing above siege 13, hot gas enters via pipeline 12, by this hot gas heated fluidized bed 14.Also fuel can be incorporated in fluidized-bed reactor 10 via pipeline 12 or extra unaccounted pipeline, rather than supply hot gas in internally fired reactor.Particle supply line 5 ends at the direct neighbor place of supply line 12.
Via pipeline 15, the hardened granules that contains ferriferous oxide is fed to reduction phase, particularly, in rotary kiln 16, for example by SL/RN technique, they are reduced therein.Via pipeline 17, thereby for example coal is incorporated in rotary kiln 16 as reductive agent.
Via pipeline 20, the dust being produced by fluidized-bed reactor 10 is incorporated in cyclonic separator 21, therein described dust and air-flow are separated.Via pipeline 22, solids component is recycled in mixing device 1 and/or in granulated apparatus for converting 4 to be again processed into particle.
Via pipeline 30, the gas being extracted by fluidized-bed reactor 10 is supplied to exhaust after-treatment 31.Then purified gases can be discharged into atmosphere and/or as process gas via pipeline 32.
Embodiment
Particle forms:
To pulverize and be processed into the magnetite concentrate containing 69wt-% iron of pelletizing fineness (pelletizing fineness) (<100 μ m), mix with the water of 0.5wt-% wilkinite and aequum, and carry out subsequently particle formation, the amount of required water is determined by desirable particle water capacity.The water capacity of thus obtained particle should be about 10wt-%; The granularity of particle is 0.1 to 3mm.
Sclerosis:
Subsequently thus obtained particle is hardened in continuous operation mode in approximately 980 ℃ in fluidized-bed reactor, be then cooled to approximately 30 ℃.The throughput of the equipment using is about 14kg/h.Between the hardening period of carrying out, magnetite is oxidized to rhombohedral iron ore in oxygen-containing atmosphere, to discharge in addition heat energy.
The reduction of the microparticle of sclerosis in short rotary kiln:
The coal of the sclerosis microparticle of 60kg and 40kg is mixed and is encased in stove.C
fix: Fe
totratio is 0.60.1020 to 1050 ℃ of processing, pack thing into approximately 4 hours.After cooling under nitrogen atmosphere, average sample is also encased in feeble field magnetic separator so that separated remaining coal and ash content.Magnetic product sponge iron has following analytical results:
Fe
total:80.0wt-％
Fe
2+:2.6wt-％
Fe
met:76.8wt-％
Degree of metalization: 96wt-%
In magnetic product, the amount of the particulate of diameter <0.1mm is about 4.5wt-%.
Reference numerals list:
1 mixing device
2,3 pipelines
4 granulated apparatus for converting
5 pipelines
10 fluidized-bed reactors
11,12 pipelines
13 sieges
14 fluidized-beds
15 pipelines
16 reduction phases (rotary kiln)
17 pipelines
20 pipelines
21 cyclonic separators
22 pipelines
30 pipelines
31 off gas treatments
32 pipelines
Claims (12)
1. for the technique by containing iron granules production hardened granules, wherein by described, containing iron granules, mix to obtain mixture with at least one tackiness agent and water, by described mixture forming particle, and described particle is incorporated in fluidized-bed reactor for sclerosis, it is characterized in that, the hottest point place by still wetting particle at fluidized-bed is incorporated in described fluidized-bed reactor.
2. technique according to claim 1, it is characterized in that, described wetting particle is incorporated into the lower region of described fluidized-bed reactor, also hot gas is introduced in the lower region of this fluidized-bed reactor or in the lower region of fluidized-bed reactor, carried out the burning of fuel.
3. technique according to claim 1 and 2, is characterized in that, described containing iron granules have the iron level of 30wt-% at least and/or at most 5wt-% be coarser than the granularity of 0.1mm.
4. according to technique in any one of the preceding claims wherein, it is characterized in that, described tackiness agent is inorganic bond reagent.
5. according to technique in any one of the preceding claims wherein, it is characterized in that, described particle have 0.1 and 6mm between granularity and/or 8 to 14wt-% water-content.
6. according to technique in any one of the preceding claims wherein, it is characterized in that, the temperature in described fluidized-bed reactor is between 850 and 1050 ℃.
7. according to technique in any one of the preceding claims wherein, it is characterized in that, be hardened in oxidizing atmosphere described in described fluidized-bed reactor and carry out.
8. according to technique in any one of the preceding claims wherein, it is characterized in that, described hardened granules is directly supplied to downstream reduction phase.
9. according to technique in any one of the preceding claims wherein, it is characterized in that, by iron dust containing recirculation, for mixing and/or particle formation, described iron dust containing is to produce in described fluidized-bed reactor and/or in the reduction phase in the downstream of described fluidized-bed reactor.
10. for implementing the equipment of technique described in aforementioned claim any one, described equipment belt has for mixing to obtain the device (1) of mixture containing iron granules and at least one tackiness agent and water, be used for described mixture to carry out particle formation to obtain the device (4) of particle, and the fluidized-bed reactor (10) of the described particle that is used for hardening, it is characterized in that, the supply line of particle (5) leads in the lower region of described fluidized-bed reactor (10).
11. equipment according to claim 10, described equipment is with the supply line (11) of hot gas or fuel, it is characterized in that, the supply line of described particle (5) is opened the region that enters into described fluidized-bed reactor (10) at the supply line (11) of described hot gas or fuel.
12. according to the equipment described in claim 10 or 11, it is characterized in that, from the reduction phase (16) in described fluidized-bed reactor (10) and/or downstream, draw at least one reflux line (20,22) to the device for mixing (1) and/or for granuloplastic device (4).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102012005454.8A DE102012005454B4 (en) | 2012-03-20 | 2012-03-20 | Method and device for producing hardened granules from iron-containing particles |
| DE102012005454.8 | 2012-03-20 | ||
| PCT/EP2013/054558 WO2013139606A1 (en) | 2012-03-20 | 2013-03-07 | Process and apparatus for producing hardened granules from iron-containing particles |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104204244A true CN104204244A (en) | 2014-12-10 |
| CN104204244B CN104204244B (en) | 2017-03-01 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201380015110.9A Active CN104204244B (en) | 2012-03-20 | 2013-03-07 | By the technique and the equipment that produce hardened granules containing iron granules |
Country Status (7)
| Country | Link |
|---|---|
| CN (1) | CN104204244B (en) |
| AU (1) | AU2013234571B2 (en) |
| DE (1) | DE102012005454B4 (en) |
| EA (1) | EA025984B1 (en) |
| IN (1) | IN2014MN01929A (en) |
| WO (1) | WO2013139606A1 (en) |
| ZA (1) | ZA201406402B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3984229A (en) * | 1970-04-20 | 1976-10-05 | Boliden Aktiebolag | Method for producing coarse powder, hardened iron oxide material from finely divided raw material substantially consisting of hematite and/or magnetite |
| WO1982002061A1 (en) * | 1980-12-08 | 1982-06-24 | Olle Bostroem | The manufacture of a product to be sintered from fine-grain ironoxide material |
| CN102149831A (en) * | 2008-09-11 | 2011-08-10 | 西门子Vai金属科技有限责任公司 | Process for producing agglomerates of finely particulate iron carriers |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1262311B (en) | 1962-06-30 | 1968-03-07 | Metallgesellschaft Ag | Method and device for reducing iron oxides (concentrates) to sponge iron |
| DE2517543C2 (en) | 1975-04-21 | 1985-12-12 | Board Of Control Of Michigan Technological University, Houghton, Mich. | Process for producing hardened agglomerates from metallurgical dust |
| JPS63103851A (en) | 1986-10-21 | 1988-05-09 | 電気化学工業株式会社 | Binder for fine powder iron ore solidification |
| DE4437549C2 (en) | 1994-10-20 | 1996-08-08 | Metallgesellschaft Ag | Process for producing metallic iron from fine-grained iron ore |
| GB9604927D0 (en) | 1996-03-08 | 1996-05-08 | Allied Colloids Ltd | Activation of swelling clays and processes of using the activated clays |
| DE19718136C2 (en) | 1997-04-30 | 2003-02-13 | Outokumpu Oy | Process for the thermal treatment of granular iron ore before reduction |
| CA2251339A1 (en) | 1997-10-30 | 1999-04-30 | Hidetoshi Tanaka | Method of producing iron oxide pellets |
| US6802886B2 (en) | 2000-06-05 | 2004-10-12 | Midrex Technologies, Inc. | Method of producing a metallized briquette |
| DE102007030394A1 (en) | 2007-06-29 | 2009-01-08 | Outotec Oyj | Thermal treatment of sulfide ores such as molybdenite to produce molybdenum trioxide, by roasting enriched ore concentrate in first reactor, separating the solids in separator, and converting the solid to metallic oxide in second reactor |
-
2012
- 2012-03-20 DE DE102012005454.8A patent/DE102012005454B4/en active Active
-
2013
- 2013-03-07 AU AU2013234571A patent/AU2013234571B2/en active Active
- 2013-03-07 CN CN201380015110.9A patent/CN104204244B/en active Active
- 2013-03-07 WO PCT/EP2013/054558 patent/WO2013139606A1/en active Application Filing
- 2013-03-07 IN IN1929MUN2014 patent/IN2014MN01929A/en unknown
- 2013-03-07 EA EA201491633A patent/EA025984B1/en not_active IP Right Cessation
-
2014
- 2014-09-01 ZA ZA2014/06402A patent/ZA201406402B/en unknown
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3984229A (en) * | 1970-04-20 | 1976-10-05 | Boliden Aktiebolag | Method for producing coarse powder, hardened iron oxide material from finely divided raw material substantially consisting of hematite and/or magnetite |
| WO1982002061A1 (en) * | 1980-12-08 | 1982-06-24 | Olle Bostroem | The manufacture of a product to be sintered from fine-grain ironoxide material |
| CN102149831A (en) * | 2008-09-11 | 2011-08-10 | 西门子Vai金属科技有限责任公司 | Process for producing agglomerates of finely particulate iron carriers |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2013139606A1 (en) | 2013-09-26 |
| DE102012005454A1 (en) | 2013-09-26 |
| DE102012005454B4 (en) | 2020-06-18 |
| CN104204244B (en) | 2017-03-01 |
| EA025984B1 (en) | 2017-02-28 |
| EA201491633A1 (en) | 2015-03-31 |
| ZA201406402B (en) | 2015-12-23 |
| IN2014MN01929A (en) | 2015-07-10 |
| AU2013234571A1 (en) | 2014-09-18 |
| AU2013234571B2 (en) | 2015-09-10 |
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