CN101397606A - Fine iron pre-reduction technology suitable for wide grain size distribution and apparatus thereof - Google Patents
Fine iron pre-reduction technology suitable for wide grain size distribution and apparatus thereof Download PDFInfo
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- CN101397606A CN101397606A CNA2007100463234A CN200710046323A CN101397606A CN 101397606 A CN101397606 A CN 101397606A CN A2007100463234 A CNA2007100463234 A CN A2007100463234A CN 200710046323 A CN200710046323 A CN 200710046323A CN 101397606 A CN101397606 A CN 101397606A
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Abstract
The invention relates to a prereducing technology of iron powdered ore suitable for wide particle size distribution, which comprises the following steps: a) the iron powdered ore with particle size smaller than 8mm is added into a cylindrical fluidized bed from a bin and coal gas is introduced from the bottom of the cylindrical fluidized bed; the temperature in a reactor is 650 to 950 DEG C, pressure is 0.2 to 1.0Mpa and gas speed in the cylindrical fluidized bed is 3 to 25m/s; b) the iron powdered ore with particle size smaller than 0.5mm leaves the cylindrical fluidized bed along with the coal gas and enters a pyramid type fluidized bed at the upper part, the iron powdered ore is separated from the coal gas and back mixed to the lower part of the fluidized bed, while the iron powdered ore with the particle size smaller than 0.05mm enters a hot cyclone separator along with the coal gas for separation and returns to the fluidized bed or enters a next fluidized bed reactor; and c) the iron powdered ore after reaction enters the next fluidized bed reactor or a melting gasification furnace. In the technology of the invention, the layering of the iron powdered ore with various particle sizes in the fluidized bed can obtain high-quality fluidizaton, thus improving the chemical reaction kinetics conditions in the fluidized bed reactor and the reaction efficiency of the fluidized bed.
Description
Technical field
The present invention relates to ironmaking technique of fusion and reduction in the ironmaking field, particularly a kind of fine iron pre-reduction technology and device thereof that is fit to wide size-grade distribution.
Background technology
The sintering powder iron ore of multistage fluidized bed prereduction granularity＜8mm is one of main prereduction technology of two step method ironmaking technique of fusion and reduction.For size-grade distribution wide especially (maximum particle diameter is 8mm, the sintering powder iron ore fluidized reduction technology of minimum grain size＜0.1mm), fluidization quality is poor in traditional cylinder shape fluidized-bed reactor, has a large amount of than small grain size powder iron ore elutriation.The cylinder shape fluidized-bed is the fluidized bed type of using always, simple in structure, make easily, volume of equipment utilization ratio height, because cylinder shape fluidized-bed internal diameter homogeneous, for even-grained reaction mass, in fluidized-bed, can obtain uniform fluidisation, but reaction mass for wide size-grade distribution, in order to guarantee the reaction mass fluidisation of volume particle size, need the operating gas velocity of fluidized-bed very high, under this operating gas velocity condition, produce a large amount of fine particle elutriations, increased the pressure of tornado dust collector, reduced raw material availability.The pyramid type fluidized-bed can partly solve wide grain fluidized of size-grade distribution, high gas speed in the fluidized-bed bottom can guarantee coarse grained fluidization, the low gas velocity at top can suppress fine grain elutriation simultaneously, reduces the dust rate, can obtain fluidization quality preferably under than the low gas velocity condition.But in single pyramid type fluidized-bed reactor, for the wide raw material of size-grade distribution, single tapering fluidized-bed is difficult to satisfy the requirement of high quality fluidisation, and if consider that the total high factor of fluidized-bed, the height of pyramid type fluidized-bed design also very difficulty.
Summary of the invention
The objective of the invention is to develop a kind of fine iron pre-reduction technology and device thereof that is fit to wide size-grade distribution, can effectively guarantee the powder iron ore raw material high quality fluidised formization of wide size-grade distribution, thereby strengthen the heating and the reaction of powder iron ore in the fluidized-bed.
For achieving the above object, technical scheme of the present invention is,
A kind of combined fluidized bed reactor and processing requirement following steps that are fit to wide size-grade distribution powder iron ore fluidization reaction:
A kind of fine iron pre-reduction technology that is fit to wide size-grade distribution adopts combined fluidized bed reactor, and this combined fluidized bed reactor is combined by the pyramid type fluidized-bed on cylinder shape fluidized-bed that is positioned at the bottom and top; It comprises the steps:
A) the powder iron ore of granularity＜8mm is added in the cylinder shape fluidized-bed by feed bin, feeds from cylinder shape fluidized-bed bottom as the coal gas of reaction medium and fluidizing medium; Granularity〉the powder iron ore of 2mm forms turbulence state at the cylinder shape fluidized-bed; Temperature remains on 650-950 ℃ in the combined fluidized bed reactor, and pressure is at 0.2-1.0Mpa, and cylinder shape fluidized-bed gas speed is 3-25m/s;
B) the powder iron ore of granularity＜0.5mm continues to rise to certain altitude along with the coal gas band enters the pyramid type fluidized-bed on top from the cylinder shape fluidized-bed in the pyramid type fluidized-bed; Along with the reduction of pyramid type fluidized-bed upper gas speed, pyramid type fluidized-bed upper end gas speed＜0.5m/s; The powder iron ore separates back mixing to the fluidized-bed bottom with coal gas, the powder iron ore of granularity＜0.05mm separates and turns back in the fluidized-bed or enter the next stage fluidized-bed reactor along with coal gas enters hot cyclone separator;
C) reacted powder iron ore enters next stage fluidized-bed reactor or melting gasification furnace by tremie pipe.
Further, described combined fluidized bed reactor is combined by the cylinder shape fluidized-bed of bottom and the pyramid type fluidized-bed on top, and the two is connected or freely connected by gas distribution grid.
Powder iron ore largest particle diameter and smallest particles diameter ratio〉8.
The middle coal gas effective constituent H that feeds
2%+CO%〉50%.
By the iron ore fine powder in the hot cyclone separator recovery fluidized-bed.
In addition, a kind of combined fluidized bed reactor that is used for fine iron pre-reduction technology of the present invention comprises cylinder shape fluidized-bed and pyramid type fluidized-bed; The pyramid type fluidized-bed is positioned at cylinder shape fluidized-bed top, and the two is connected or freely connected by gas distribution grid.
Described pyramid type fluidized-bed upper end maximum inner diameter and cylinder shape fluidized-bed internal diameter ratio〉1.5.
Described pyramid type fluidized-bed part height and cylinder shape fluidized bed height ratio＜6.
The tapering of described pyramid type fluidized-bed is 10 °～60 °.
The cylinder shape fluidized-bed keeps gas speed 3-25m/s, guaranteed granularity〉the macrobead powder iron ore turbulence state of 2mm, the powder iron ore of granularity＜0.5mm enters the pyramid type fluidized-bed on top rapidly from (or through gas distributor) from cylinder shape fluidized-bed band, the powder iron ore of other granularity is in combined fluidized bed middle part layer distributed, on pyramid type fluidized-bed top because the reduction of gas speed, arrive pyramid type fluidized-bed upper end gas speed＜0.5m/s, most of powder iron ore falls back mixing after rise, and the fine powder iron ore of＜0.05mm enters the hot cyclone separator separation with coal gas and turns back in the fluidized-bed.
The high gas speed that the cylinder shape fluidized bed type of combined fluidized bed reactor lower part becomes can guarantee that oarse-grained reaction mass keeps the turbulence fluidized state, and the gas velocity on combined fluidized bed reactor top descends and then strengthens the back mixing of the small-particle powder carried secretly in the fluidized-bed.The wide powder iron ore fluidization of size-grade distribution that reaches 8mm for maximum particle diameter is reacted, and can effectively reduce and carry secretly and elutriation, reduces the fluidized-bed height overall, keeps the turbulence of the close bed part in fluidized-bed bottom violent simultaneously, prevents that effectively the generation of fluidized-bed bottom from boning.The fluidized-bed reactor that combines by cylinder shape fluidized-bed and pyramid type fluidized-bed, the comprehensive simple advantage of cylinder shape fluidized-bed structure, guarantee the fluidization quality of raw material under the wide granularity condition simultaneously, compare with the pyramid type fluidized-bed, combined fluidized bed design is more flexible, to the raw material that different grain size is formed, combined fluidized bed can the adjustment more flexibly, control fluidized-bed height overall.
Under certain condition, the connection of cylinder shape fluidized-bed and pyramid type fluidized-bed can be saved gas distribution grid, simplifies the structure of fluidized-bed, has reduced the crushing of gas by gas distributor.
Beneficial effect of the present invention
Technology of the present invention is for the powder iron ore raw material of wide size-grade distribution, because powder iron ore layering in fluidized-bed of various granularities, the powder iron ore of each granularity can both obtain high-quality fluidization, has improved the chemical kinetics condition in the fluidized-bed reactor, has improved the reaction efficiency of fluidized-bed.Single relatively pyramid type fluidized-bed, the pyramid type fluidized-bed design on combined fluidized bed top is more flexible, is guaranteeing that fluidized bed height can reduce greatly under the same fluidization quality condition.
The drawing explanation
Fig. 1 is the schematic flow sheet of technology first embodiment of the present invention;
Fig. 2 is the schematic flow sheet of technology second embodiment of the present invention;
Fig. 3 is the schematic flow sheet of technology the 3rd embodiment of the present invention.
Embodiment
Referring to Fig. 1, powder iron ore 1 and flux 2 raw materials are mixed in the feed bin 3, and (granularity＜8mm) is added the bottom of cylinder shape fluidized-bed 4, coal gas 7 (reduction degree H to raw material
2%+CO%〉50%) feed from cylinder fluidized-bed 4 bottoms, gas speed is 4m/s in the cylinder shape fluidized-bed 4, the macrobead raw material of 2mm keeps the turbulence state in cylinder shape fluidized-bed 4, the small grain size raw material is with step by step from cylinder shape fluidized-bed 4, layering fluidization in pyramid type fluidized-bed 5 (tapering is 20 °), because along with highly rising, the sectional area of pyramid type fluidized-bed 5 increases, gas speed is also corresponding to be reduced, pyramid type fluidized-bed 5 upper end gas speed＜0.5m/s, a large amount of fine ore raw material back mixing is in the close bed of bottom, and granularity＜0.05mm enters in the hot cyclone separator 6, isolating fine powder raw material also back mixing in the close bed of bottom.In the fluidization process, the fluidized-bed internal pressure remains on 0.3MPa, and temperature remains on 670 ℃, powder iron ore and coal gas generation reduction reaction, and reacted powder iron ore reduction degree reaches 10-25%, and further reduces to the next stage fluidized-bed by tremie pipe 8.Reacted coal gas is through gas cleaning device 9 decontamination cycle utilizations or be used for other purposes such as generating, manufacturing Chemicals.
Referring to Fig. 2, reactant feed (bottom of granularity＜8mm) add cylinder shape fluidized-bed 4 to, coal gas 7 (reduction degree H by upper level fluidized-bed tremie pipe 10
2%+CO%〉60%) feed from cylinder shape fluidized-bed 4 bottoms, gas speed is 24m/s in the cylinder shape fluidized-bed 4, the macrobead raw material of 2mm keeps the turbulence state in cylinder shape fluidized-bed 4, the small grain size raw material is with step by step from cylinder shape fluidized-bed 4, layering fluidization in pyramid type fluidized-bed 5 (tapering is 50 °), because along with highly rising, the sectional area of pyramid type fluidized-bed 5 increases, gas speed is also corresponding to be reduced, pyramid type fluidized-bed 5 upper end gas speed＜0.5m/s, a large amount of fine ore raw material back mixing is in the close bed of bottom, and granularity＜0.05mm enters in the hot cyclone separator 6, isolating fine powder raw material also back mixing in the close bed of bottom.In the fluidization process, the fluidized-bed internal pressure remains on 1.0MPa, temperature remains on 900 ℃, powder iron ore and coal gas generation reduction reaction, reacted powder iron ore reduction degree reaches 20-50%, and further reduce to the next stage fluidized-bed by tremie pipe 10 ', reacted coal gas 7 ' enters in the upper level fluidized-bed as reaction medium and fluidizing medium.
Embodiment 3
Referring to Fig. 3, reactant feed (bottom of granularity＜8mm) add cylinder shape fluidized-bed 4 to, coal gas 7 (reduction degree H by upper level fluidized-bed tremie pipe 10
2%+CO%〉80%) feed from cylinder shape fluidized-bed 3 bottoms, gas speed is 10m/s in the cylinder shape fluidized-bed 3, the macrobead raw material of 2mm keeps the turbulence state in cylinder shape fluidized-bed 3, the small grain size raw material is with step by step from cylinder shape fluidized-bed 3, layering fluidization in pyramid type fluidized-bed 5 (tapering is 55 °), because along with highly rising, the sectional area of pyramid type fluidized-bed 5 increases, gas speed is also corresponding to be reduced, pyramid type fluidized-bed 5 upper end gas speed＜0.5m/s, a large amount of fine ore raw material back mixing is in the close bed of bottom, and granularity＜0.05mm enters in the hot cyclone separator 6, isolating fine powder raw material also back mixing in the close bed of bottom.In the fluidization process, the fluidized-bed internal pressure remains on 0.9MPa, temperature remains on 700 ℃, powder iron ore and coal gas generation reduction reaction, reacted powder iron ore reduction degree reaches 60-95%, and passing through tremie pipe 10 ' to the whole reducing and smelting molten iron of melting gasification furnace, reacted coal gas 7 ' enters in the upper level fluidized-bed as reaction medium and fluidizing medium.
Embodiment 3 with the difference of embodiment 1,2 is: the fluidized-bed raw material among the embodiment 3 is a upper level fluidized-bed reaction product, reducing gas is the higher coal gas of reduction degree that melting gasification furnace produces, and adds whole reducing and smelting molten iron in the melting gasification furnace after the powder iron ore reduces in fluidized-bed to.
In sum, technology of the present invention is for the powder iron ore raw material of wide size-grade distribution, because powder iron ore layering in fluidized-bed of various granularities, the powder iron ore of each granularity can both obtain high-quality fluidization, improve the chemical kinetics condition in the fluidized-bed reactor, improved the reaction efficiency of fluidized-bed.Single relatively pyramid type fluidized-bed, the pyramid type fluidized-bed design on combined fluidized bed top is more flexible, is guaranteeing that fluidized bed height can reduce greatly under the same fluidization quality condition.
Claims (12)
1. a fine iron pre-reduction technology that is fit to wide size-grade distribution adopts combined fluidized bed reactor, and this combined fluidized bed reactor is combined by the pyramid type fluidized-bed on cylinder shape fluidized-bed that is positioned at the bottom and top; It comprises the steps:
A) the powder iron ore of granularity＜8mm is added in the cylinder shape fluidized-bed by feed bin, feeds from cylinder shape fluidized-bed bottom as the coal gas of reaction medium and fluidizing medium; Granularity〉the powder iron ore of 2mm forms turbulence state at the cylinder shape fluidized-bed; Temperature remains on 650-950 ℃ in the combined fluidized bed reactor, and pressure is at 0.2-1.0Mpa, and cylinder shape fluidized-bed gas speed is 3-25m/s;
B) the powder iron ore of granularity＜0.5mm continues to rise to certain altitude along with the coal gas band enters the pyramid type fluidized-bed on top from the cylinder shape fluidized-bed in the pyramid type fluidized-bed; Along with the reduction of pyramid type fluidized-bed upper gas speed, pyramid type fluidized-bed upper end gas speed＜0.5m/s; The powder iron ore separates back mixing to the fluidized-bed bottom with coal gas, the powder iron ore of granularity＜0.05mm separates and turns back in the fluidized-bed or enter the next stage fluidized-bed reactor along with coal gas enters hot cyclone separator;
C) reacted powder iron ore enters next stage fluidized-bed reactor or melting gasification furnace by tremie pipe.
2. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 1, it is characterized in that, described combined fluidized bed reactor is combined by the cylinder shape fluidized-bed of bottom and the pyramid type fluidized-bed on top, and the two is connected or freely connected by gas distribution grid.
3. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 1 is characterized in that, powder iron ore largest particle diameter and smallest particles diameter ratio〉8.
4. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 1 is characterized in that the coal gas effective constituent H of middle feeding
2%+CO%〉50%.
5. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 1 is characterized in that, described pyramid type fluidized-bed upper end maximum inner diameter and cylinder shape fluidized-bed internal diameter ratio〉1.5.
6. as claim 1 or the 5 described fine iron pre-reduction technologies that are fit to wide size-grade distribution, it is characterized in that described pyramid type fluidized-bed part height and cylinder shape fluidized bed height ratio＜6.
7. as claim 1 or the 5 described fine iron pre-reduction technologies that are fit to wide size-grade distribution, it is characterized in that the tapering of described pyramid type fluidized-bed is 10 °～60 °.
8. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 1 is characterized in that, by the iron ore powder particle size＜0.05mm in the hot cyclone separator recovery fluidized-bed.
9. one kind is used for the described combined fluidized bed reactor that is fit to the fine iron pre-reduction technology of wide size-grade distribution of claim 1, it is characterized in that, comprises cylinder shape fluidized-bed and pyramid type fluidized-bed; The pyramid type fluidized-bed is positioned at cylinder shape fluidized-bed top, and the two is connected or freely connected by gas distribution grid.
10. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 9 is characterized in that, described pyramid type fluidized-bed upper end maximum inner diameter and cylinder shape fluidized-bed internal diameter ratio〉1.5.
11. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 9 is characterized in that, described pyramid type fluidized-bed part height and cylinder shape fluidized bed height ratio＜6.
12. the fine iron pre-reduction technology that is fit to wide size-grade distribution as claimed in claim 9 is characterized in that the tapering of described pyramid type fluidized-bed is 10 °～60 °.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104308170A (en) * | 2014-10-31 | 2015-01-28 | 辽宁工程技术大学 | Superfine iron powder preparation method |
| CN105586462A (en) * | 2014-11-07 | 2016-05-18 | 株式会社Posco | Vertical pipe draining device for draining molten ion manufacturing equipment |
| CN109047789A (en) * | 2018-09-06 | 2018-12-21 | 攀钢集团攀枝花钢铁研究院有限公司 | Reduction prepares the device and preparation method of iron powder |
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| DE3145652A1 (en) * | 1981-11-17 | 1983-06-23 | Moskovskij institut stali i splavov, Moskva | Fluidised-bed apparatus |
| KR970003636B1 (en) * | 1994-12-31 | 1997-03-20 | 포항종합제철 주식회사 | A furnace for reduction fine coal in the manufacture of iron melts |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104308170A (en) * | 2014-10-31 | 2015-01-28 | 辽宁工程技术大学 | Superfine iron powder preparation method |
| CN105586462A (en) * | 2014-11-07 | 2016-05-18 | 株式会社Posco | Vertical pipe draining device for draining molten ion manufacturing equipment |
| CN109047789A (en) * | 2018-09-06 | 2018-12-21 | 攀钢集团攀枝花钢铁研究院有限公司 | Reduction prepares the device and preparation method of iron powder |
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