CN102925666B - Method for fluidized pre-reduction of aluminum and iron paragenetic mineral - Google Patents
Method for fluidized pre-reduction of aluminum and iron paragenetic mineral Download PDFInfo
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- CN102925666B CN102925666B CN201210408366.3A CN201210408366A CN102925666B CN 102925666 B CN102925666 B CN 102925666B CN 201210408366 A CN201210408366 A CN 201210408366A CN 102925666 B CN102925666 B CN 102925666B
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Abstract
The invention discloses a method for fluidized pre-reduction of aluminum and iron paragenetic mineral. The method comprises the following steps that: aluminum and iron paragenetic mineral powder is charged into a first stage of fluidized bed in a multi-stage fluidized bed reactor through a spiral material charging device, and high-temperature reducing coal gas is introduced from the bottom of the last stage of fluidized bed, wherein the Al2O3 content in the aluminum and iron paragenetic mineral powder is 5 to 30 percent, the TFe content in the aluminum and iron paragenetic mineral powder is 30 to 70 percent, and the particle size is 0.01 to 8mm; the high-temperature reducing coal gas which is obtained by mixing and regulating high-temperature reducing coal gas generated in a final reducing furnace and returned tail gas, and the mineral powder respectively flow through the fluidized beds in opposite directions for performing fluidized pre-reduction; and the mineral powder flows out of the last stage of fluidized bed, wherein the reduction degree can be over 50 percent; and besides, after being subjected to dust removal, washed and subjected to CO2 removal, the reducing tail gas returns and is charged into coal gas at the outlet of the final reducing furnace for regulating the coal gas so as to be recycled. The method is simple in technological operation and high in production efficiency, the aluminum and iron paragenetic mineral can be continuously treated on a large scale, the high-temperature coal gas is recycled, the aluminum and iron paragenetic mineral is comprehensively utilized, and energy-saving and emission reducing effects are achieved.
Description
Technical field
The present invention relates to ferro-aluminum mineral intergrowth field of comprehensive utilization, particularly a kind of method of pre-reduced iron in ferro-aluminum mineral intergrowth iron aluminium integrated extraction technique.
Background technology
The fast development of China's Iron And Steel Industry is very huge to the demand of iron ore, and China's iron ore deposit lean ore is many, and rich ore is few, and association component is many, and smelting condition is poor, and iron ore average grade only has 33%.Therefore, China's iron ore external dependence degree increases year by year, reaches about 70%, becomes the major hidden danger of China's Iron And Steel Industry economic security.In addition, along with aluminum oxide industry and other fast developments with bauxite industry, the shortage of bauxite resource, particularly high-quality resource, fully displays.The imbalance between supply and demand of current high-quality bauxite is very outstanding, and dilution trend has appearred in mine all in various degree, and numerous enterprises is tried to be the first and rushed to purchase limited high-quality resource.And " dull " ferro-aluminum mineral intergrowth of China is more than 1,500,000,000 tons, due to Iron grade and aluminium grade low and for being fully used.Therefore, reformed by Technology, make full use of this part ferro-aluminum mineral intergrowth, the imbalance between supply and demand of China's iron ore imports pressure and bauxite can be alleviated, significant to the Sustainable development of China's Iron And Steel Industry and aluminum i ndustry.
Ferro-aluminum mineral intergrowth essential mineral consists of gibbsite, pyrrhosiderite, rhombohedral iron ore and kaolinite, wherein Al
2o
3content 20 ~ 30%, Fe
2o
3content 30 ~ 48%, SiO
2content 4 ~ 20%, alumina silica ratio 2 ~ 3.5.Although ore Iron grade and aluminium grade all lower, the total content of aluminum oxide and ferric oxide reaches about 70%, has the value of comprehensive utilization." first smelting after choosing ", " after first aluminium iron " and " after first iron aluminium " three kinds of general plannings are had at present for the comprehensive utilization of ferro-aluminum mineral intergrowth.For " first smelting after choosing " scheme, patent 200410010400.7 and 200610017376.9 discloses the method that the magnetic separation of Iron In Iron-rich Containing Bauxite aluminium is separated, but because iron-bearing mineral in ore and the tight symbiosis of aluminum-containing mineral, disseminated grain size are superfine, monomer is difficult to dissociate, and ferro-aluminum separating effect is difficult to reach re-set target.And patent 201010195045.0 discloses the method being realized ferro-aluminum separation by magnetizing roasting, but owing to there is Fe in ore
3+and Al
3+lattice mutually replace, isomorph phenomenon is obvious, and magnetizing roasting is difficult to be dissociated.For " after first aluminium iron " scheme, no matter sintering process, Bayer process or integrated process all require ore Al
2o
3content is greater than 60%, Fe
2o
3content is less than 10%, and ferric oxide on stream not with alkali reaction, iron red mud content is large, and low to the utilization ratio of iron red mud, and its bulk deposition causes severe contamination to environment.Therefore, " after first iron aluminium " scheme is favored gradually, and patent 200510200493.4 discloses carries iron by sintering and blast-furnace smelting, and from calcium aluminate slag, puies forward the ferro-aluminum mineral intergrowth method of comprehensive utilization of aluminium, due to ore Al
2o
3content is high, and cause slag melting rising, viscosity increase, make slag sluicing system difficulty, the capacity factor of a blast furnace reduces.In order to reduce the aluminium content in ore, patent 200710034845.2 discloses and leaches Al in ore by high-temperature roasting and NaOH solution
2o
3method, its objective is as obtaining high-grade iron ore concentrate for blast-furnace smelting, and complex process, energy consumption is high, does not meet the requirement of comprehensive utilization of resources and energy-conserving and environment-protective.
Summary of the invention
Technology of the present invention is dealt with problems: overcome the deficiencies in the prior art, the method of the efficient pre-reduced iron of a kind of ferro-aluminum mineral intergrowth is provided, utilize the coal gas of high temperature reduction breeze of reduction generation eventually in non-blast furnace smelting process, both the high restriction to blast-furnace smelting of alumina content can have been broken away from, all right energy-conserving and environment-protective, realize the comprehensive utilization to ferro-aluminum mineral intergrowth.
Technical scheme of the present invention: a kind of method of ferro-aluminum mineral intergrowth fluidized pre-reduction, its feature is: first sieved by ferro-aluminum mineral intergrowth, and it is that the ferro-aluminum symbiosis breeze of 0.01 ~ 8mm is as raw material that sieve gets size range; Then with feeding screw the ferro-aluminum symbiosis breeze that filters out sent into the first step fluidized-bed in multistage fluidized bed reactor, every grade of fluidized-bed is furnished with cyclonic separator; Simultaneously reductibility coal gas of high temperature passes into from last step fluidized-bed bottom, described reductibility coal gas of high temperature be the reductibility coal gas of high temperature that produced by end reducing furnace and through dedusting, wash and remove CO
2the tail gas Mixed adjustment returned after operation and obtaining, described reductibility coal gas of high temperature reducing component CO%+H
2the volume content of % is 50 ~ 98%; Described reductibility coal gas of high temperature and the countercurrent flow of ferro-aluminum symbiosis breeze, reversely successively flow through fluidized-bed at different levels and cyclonic separator; Ferro-aluminum symbiosis breeze goes downstream due to self gravitation effect, successively through fluidized-bed at different levels, and after every grade of cyclonic separator gas solid separation, entered next stage fluidized-bed by tremie pipe by the tiny breeze that gas is taken away, ferro-aluminum symbiosis breeze contacts with described reductibility coal gas of high temperature is reverse, carry out Reduction on Fluidized Bed, wherein fluidizing gas velocity is 0.1 ~ 0.6m/s, described multistage fluidized bed internal pressure hold-in range is 0.1 ~ 1.0MPa, in fluidized-bed, reduction temperature is 500 ~ 950 DEG C, and the time of Reduction on Fluidized Bed is 30 ~ 90min; Finally, ferro-aluminum symbiosis breeze is discharged from last step fluidized-bed, and reduction degree can reach more than 50%, smelts for end reducing furnace.
The reduction tail gas that cyclonic separator in first step fluidized-bed in described multistage fluidized bed reactor is discharged through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.
Described multistage fluidized bed reactor is 2 ~ 4 grades.
Containing mass percent in described ferro-aluminum mineral intergrowth is the Al of 5 ~ 30%
2o
3, the TFe of 30 ~ 70%, preferred Al
2o
3content is 15 ~ 30%, TFe content 30 ~ 55%;
The size range of described ferro-aluminum symbiosis breeze is 0.05 ~ 1mm.
Described reductibility coal gas of high temperature reducing component CO%+H
2the volume content of % is preferably 70 ~ 98%.
Described fluidizing gas velocity is 0.2 ~ 0.4m/s.
Described multistage fluidized bed internal pressure hold-in range is 0.4 ~ 0.8MPa.
In described fluidized-bed, reduction temperature is 650 ~ 950 DEG C.
The time of described Reduction on Fluidized Bed is 50 ~ 90min.
The present invention's advantage is compared with prior art:
(1) method of the efficient pre-reduced iron of ferro-aluminum mineral intergrowth of the present invention, utilize the coal gas of high temperature reduction breeze of reduction generation eventually in non-blast furnace smelting process, both can break away from the high restriction to blast-furnace smelting of alumina content, all right energy-conserving and environment-protective, realize the comprehensive utilization to ferro-aluminum mineral intergrowth.
(2) in the present invention, fluidization directly can utilize breeze, and mass transfer, heat transfer efficiency are high.Meanwhile, in ferro-aluminum mineral intergrowth, the aluminum oxide of high-content can avoid the generation of bonding defluidization, can realize in enormous quantities, continuous prodution.
(3) in the present invention first step cyclonic separator discharge reduction tail gas through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.
(4) method of ferro-aluminum mineral intergrowth fluidization gas base of the present invention prereduction, technological operation is simple, production efficiency is high, can serialization mass disposal ferro-aluminum mineral intergrowth, and recycle coal gas of high temperature, while the comprehensive utilization of ferro-aluminum mineral intergrowth, realize energy-saving and emission-reduction.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
Embodiment
The present invention is introduced in detail below in conjunction with drawings and the specific embodiments.But following embodiment is only limitted to explain the present invention, and protection scope of the present invention should comprise the full content of claim, is not limited only to the present embodiment.
First filtering out the ferro-aluminum symbiosis breeze that granularity is less than 8.00mm is raw material, then with feeding screw ferro-aluminum symbiosis breeze sent into the first step fluidized-bed in multistage fluidized bed reactor, reductibility coal gas of high temperature passes into from last step fluidized-bed bottom simultaneously, with breeze countercurrent flow, reversely successively flow through fluidized-bed at different levels and cyclonic separator, breeze goes downstream, successively through fluidized-bed at different levels due to self gravitation effect, contact with reductibility coal gas of high temperature is reverse, carry out fluidized reduction; Finally, breeze is discharged from last step fluidized-bed, and reduction degree reaches more than 50%, smelts for end reducing furnace, and reduction tail gas returns to be blended in end reducing furnace outlet coal gas and carries out Gas adjustment, realizes recycle.
Embodiment 1
See Fig. 1, first by TFe content 31.13%, Al
2o
3the ferro-aluminum mineral intergrowth of content 26.51% sieves, and choosing granularity is that the breeze of 0.074 ~ 0.150mm is as raw material.The ferro-aluminum symbiosis breeze of screening enters the first step fluidized-bed R1 of 4 grades of fluidized-bed reactors by feeding screw, pass into reductibility coal gas of high temperature by bottom fourth stage fluidized-bed R4 simultaneously.The tail gas that the reductibility coal gas of high temperature that reductibility coal gas of high temperature is produced by end reducing furnace and first step cyclonic separator S1 discharge through dedusting, wash and remove CO
2mixed adjustment after operation and obtaining, its reducing component CO% is 90%.Coal gas of high temperature gas after the gas solid separation of fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges passes into third stage fluidized-bed R3, coal gas of high temperature gas after the gas solid separation of third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges passes into second stage fluidized-bed R2, second stage fluidized-bed R2 discharge coal gas of high temperature gas after the gas solid separation of second stage cyclonic separator S2 pass into first step fluidized-bed R1, first step fluidized-bed R1 discharge coal gas of high temperature after the gas solid separation of the first step cyclonic separator S1 gas through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze entering first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of first step cyclonic separator S1 gas solid separation also enters second stage fluidized-bed R2 by tremie pipe simultaneously; The breeze entering second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze entering third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze entering fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads after coal gas of high temperature fluidized reduction, and the breeze of fourth stage cyclonic separator S4 gas solid separation is also discharged by tremie pipe simultaneously, obtains the breeze of high reduction degree, for end reducing furnace.Fluidizing gas velocity is 0.23m/s, and fluidized-bed internal pressure is 0.5MPa, and in fluidized-bed, reduction temperature is 900 DEG C, and the recovery time is 50min.Bonding defluidization phenomenon is there is not, breeze reduction degree 52.64% after reduction, degree of metalization 28.96% in whole reduction process.
Embodiment 2
See Fig. 1, first by TFe content 31.13%, Al
2o
3the ferro-aluminum mineral intergrowth of content 26.51% sieves, and choosing granularity is that the breeze of 0.074 ~ 0.150mm is as raw material.The ferro-aluminum symbiosis breeze of screening enters the first step fluidized-bed R1 of 4 grades of fluidized-bed reactors by feeding screw, pass into high-temperature reductibility coal gas by bottom fourth stage fluidized-bed R4 simultaneously.The tail gas that the reductibility coal gas of high temperature that reductibility coal gas of high temperature is produced by end reducing furnace and first step cyclonic separator S1 discharge through dedusting, wash and remove CO
2mixed adjustment after operation and obtaining, its reducing component CO% is 90%.Coal gas of high temperature gas after the gas solid separation of fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges passes into third stage fluidized-bed R3, coal gas of high temperature gas after the gas solid separation of third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges passes into second stage fluidized-bed R2, second stage fluidized-bed R2 discharge coal gas of high temperature gas after the gas solid separation of second stage cyclonic separator S2 pass into first step fluidized-bed R1, first step fluidized-bed R1 discharge coal gas of high temperature after the gas solid separation of the first step cyclonic separator S1 gas through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze entering first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of first step cyclonic separator S1 gas solid separation also enters second stage fluidized-bed R2 by tremie pipe simultaneously; The breeze entering second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze entering third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze entering fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads after coal gas of high temperature fluidized reduction, and the breeze of fourth stage cyclonic separator S4 gas solid separation is also discharged by tremie pipe simultaneously, obtains the breeze of high reduction degree, for end reducing furnace.Fluidizing gas velocity is 0.27m/s, and fluidized-bed internal pressure is 0.58MPa, and in fluidized-bed, reduction temperature is 800 DEG C, and the recovery time is 60min.Bonding defluidization phenomenon is there is not, breeze reduction degree 53.85% after reduction, degree of metalization 30.78% in whole reduction process.
Embodiment 3
See Fig. 1, first by TFe content 31.13%, Al
2o
3the ferro-aluminum mineral intergrowth of content 26.51% sieves, and choosing granularity is that the breeze of 0.150 ~ 0.224mm is as raw material.The ferro-aluminum symbiosis breeze of screening enters the first step fluidized-bed R1 of 4 grades of fluidized-bed reactors by feeding screw, pass into high-temperature reductibility coal gas by bottom fourth stage fluidized-bed R4 simultaneously.The tail gas that the reductibility coal gas of high temperature that reductibility coal gas of high temperature is produced by end reducing furnace and first step cyclonic separator S1 discharge through dedusting, wash and remove CO
2mixed adjustment after operation and obtaining, its reducing component CO% is 98%.Coal gas of high temperature gas after the gas solid separation of fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges passes into third stage fluidized-bed R3, coal gas of high temperature gas after the gas solid separation of third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges passes into second stage fluidized-bed R2, second stage fluidized-bed R2 discharge coal gas of high temperature gas after the gas solid separation of second stage cyclonic separator S2 pass into first step fluidized-bed R1, first step fluidized-bed R1 discharge coal gas of high temperature after the gas solid separation of the first step cyclonic separator S1 gas through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze entering first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of first step cyclonic separator S1 gas solid separation also enters second stage fluidized-bed R2 by tremie pipe simultaneously; The breeze entering second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze entering third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze entering fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads after coal gas of high temperature fluidized reduction, and the breeze of fourth stage cyclonic separator S4 gas solid separation is also discharged by tremie pipe simultaneously, obtains the breeze of high reduction degree, for end reducing furnace.Fluidizing gas velocity is 0.23m/s, and fluidized-bed internal pressure is 0.5MPa, and in fluidized-bed, reduction temperature is 900 DEG C, and the recovery time is 60min.Bonding defluidization phenomenon is there is not, breeze reduction degree 54.68% after reduction, degree of metalization 32.02% in whole reduction process.
Embodiment 4
See Fig. 1, first by TFe content 31.13%, Al
2o
3the ferro-aluminum mineral intergrowth of content 26.51% sieves, and choosing granularity is that the breeze of 0.150 ~ 0.224mm is as raw material.The ferro-aluminum symbiosis breeze of screening enters the first step fluidized-bed R1 of 4 grades of fluidized-bed reactors by feeding screw, pass into high-temperature reductibility coal gas by bottom fourth stage fluidized-bed R4 simultaneously.The tail gas that the reductibility coal gas of high temperature that reductibility coal gas of high temperature is produced by end reducing furnace and first step cyclonic separator S1 discharge through dedusting, wash and remove CO
2mixed adjustment after operation and obtaining, its reducing component CO% is 98%.Coal gas of high temperature gas after the gas solid separation of fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges passes into third stage fluidized-bed R3, coal gas of high temperature gas after the gas solid separation of third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges passes into second stage fluidized-bed R2, second stage fluidized-bed R2 discharge coal gas of high temperature gas after the gas solid separation of second stage cyclonic separator S2 pass into first step fluidized-bed R1, first step fluidized-bed R1 discharge coal gas of high temperature after the gas solid separation of the first step cyclonic separator S1 gas through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze entering first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of first step cyclonic separator S1 gas solid separation also enters second stage fluidized-bed R2 by tremie pipe simultaneously; The breeze entering second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze entering third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze entering fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads after coal gas of high temperature fluidized reduction, and the breeze of fourth stage cyclonic separator S4 gas solid separation is also discharged by tremie pipe simultaneously, obtains the breeze of high reduction degree, for end reducing furnace.Fluidizing gas velocity is 0.23m/s, and fluidized-bed internal pressure is 0.5MPa, and in fluidized-bed, reduction temperature is 900 DEG C, and the recovery time is 90min.Bonding defluidization phenomenon is there is not, breeze reduction degree 62.87% after reduction, degree of metalization 44.30% in whole reduction process.
Embodiment 5
See Fig. 1, first by TFe content 30.71%, Al
2o
3the ferro-aluminum mineral intergrowth of content 21.30% sieves, and choosing granularity is that the breeze of 0.150 ~ 0.224mm is as raw material.The ferro-aluminum symbiosis breeze of screening enters the first step fluidized-bed R1 of 4 grades of fluidized-bed reactors by feeding screw, pass into high-temperature reductibility coal gas by bottom fourth stage fluidized-bed R4 simultaneously.The tail gas that the reductibility coal gas of high temperature that reductibility coal gas of high temperature is produced by end reducing furnace and first step cyclonic separator S1 discharge through dedusting, wash and remove CO
2mixed adjustment after operation and obtaining, its reducing component CO% is 98%.Coal gas of high temperature gas after the gas solid separation of fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges passes into third stage fluidized-bed R3, coal gas of high temperature gas after the gas solid separation of third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges passes into second stage fluidized-bed R2, second stage fluidized-bed R2 discharge coal gas of high temperature gas after the gas solid separation of second stage cyclonic separator S2 pass into first step fluidized-bed R1, first step fluidized-bed R1 discharge coal gas of high temperature after the gas solid separation of the first step cyclonic separator S1 gas through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze entering first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of first step cyclonic separator S1 gas solid separation also enters second stage fluidized-bed R2 by tremie pipe simultaneously; The breeze entering second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze entering third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze entering fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads after coal gas of high temperature fluidized reduction, and the breeze of fourth stage cyclonic separator S4 gas solid separation is also discharged by tremie pipe simultaneously, obtains the breeze of high reduction degree, for end reducing furnace.Fluidizing gas velocity is 0.31m/s, and fluidized-bed internal pressure is 0.67MPa, and in fluidized-bed, reduction temperature is 900 DEG C, and the recovery time is 60min.Bonding defluidization phenomenon is there is not, breeze reduction degree 54.98% after reduction, degree of metalization 32.47% in whole reduction process.
Embodiment 6
See Fig. 1, first by TFe content 54.75%, Al
2o
3the ferro-aluminum mineral intergrowth of content 5.1% sieves, and choosing granularity is that the breeze of 0.150 ~ 0.224mm is as raw material.The ferro-aluminum symbiosis breeze of screening enters the first step fluidized-bed R1 of 4 grades of fluidized-bed reactors by feeding screw, pass into high-temperature reductibility coal gas by bottom fourth stage fluidized-bed R4 simultaneously.The tail gas that the reductibility coal gas of high temperature that reductibility coal gas of high temperature is produced by end reducing furnace and first step cyclonic separator S1 discharge through dedusting, wash and remove CO
2mixed adjustment after operation and obtaining, its reducing component CO% is 80%.Coal gas of high temperature gas after the gas solid separation of fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges passes into third stage fluidized-bed R3, coal gas of high temperature gas after the gas solid separation of third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges passes into second stage fluidized-bed R2, second stage fluidized-bed R2 discharge coal gas of high temperature gas after the gas solid separation of second stage cyclonic separator S2 pass into first step fluidized-bed R1, first step fluidized-bed R1 discharge coal gas of high temperature after the gas solid separation of the first step cyclonic separator S1 gas through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze entering first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of first step cyclonic separator S1 gas solid separation also enters second stage fluidized-bed R2 by tremie pipe simultaneously; The breeze entering second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze entering third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe after coal gas of high temperature fluidized reduction, and the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze entering fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads after coal gas of high temperature fluidized reduction, and the breeze of fourth stage cyclonic separator S4 gas solid separation is also discharged by tremie pipe simultaneously, obtains the breeze of high reduction degree, for end reducing furnace.Fluidizing gas velocity is 0.23m/s, and fluidized-bed internal pressure is 0.5MPa, and in fluidized-bed, reduction temperature is 700 DEG C, and the recovery time is 70min.Bonding defluidization phenomenon is there is not, breeze reduction degree 73.68% after reduction, degree of metalization 40.35% in whole reduction process.
Reach a conclusion thus: by the inventive method prereduction ferro-aluminum mineral intergrowth, production efficiency is high, avoid the generation of bonding defluidization simultaneously, thus can serialization mass disposal ferro-aluminum mineral intergrowth, and recycle coal gas of high temperature, while the comprehensive utilization of ferro-aluminum mineral intergrowth, realizes energy-saving and emission-reduction.
It should be noted that, according to the various embodiments described above of the present invention, those skilled in the art are the four corners that can realize independent claim of the present invention and appurtenance completely, implementation procedure and the same the various embodiments described above of method; And non-elaborated part of the present invention belongs to techniques well known.
The above; be only part embodiment of the present invention, but protection scope of the present invention is not limited thereto, any those skilled in the art are in the technical scope that the present invention discloses; the change that can expect easily or replacement, all should be encompassed within protection scope of the present invention.
Claims (5)
1. a method for ferro-aluminum mineral intergrowth fluidized pre-reduction, is characterized in that: first sieved by ferro-aluminum mineral intergrowth, and it is that the ferro-aluminum symbiosis breeze of 0.224 ~ 8mm is as raw material that sieve gets size range; Then with feeding screw the ferro-aluminum symbiosis breeze that filters out sent into the first step fluidized-bed in multistage fluidized bed reactor, every grade of fluidized-bed is furnished with cyclonic separator; Simultaneously reductibility coal gas of high temperature passes into from last step fluidized-bed bottom, described reductibility coal gas of high temperature be the reductibility coal gas of high temperature that produced by end reducing furnace and through dedusting, wash and remove CO
2the tail gas Mixed adjustment returned after operation and obtaining, described reductibility coal gas of high temperature reducing component CO%+H
2the volume content of % is 50 ~ 98%; Described reductibility coal gas of high temperature and the countercurrent flow of ferro-aluminum symbiosis breeze, reversely successively flow through fluidized-bed at different levels and cyclonic separator; Ferro-aluminum symbiosis breeze goes downstream due to self gravitation effect, successively through fluidized-bed at different levels, and after every grade of cyclonic separator gas solid separation, entered next stage fluidized-bed by tremie pipe by the tiny breeze that gas is taken away, ferro-aluminum symbiosis breeze contacts with described reductibility coal gas of high temperature is reverse, carry out Reduction on Fluidized Bed, wherein fluidizing gas velocity is 0.2 ~ 0.4m/s, described multistage fluidized bed internal pressure hold-in range is 0.4 ~ 0.8MPa, in fluidized-bed, reduction temperature is 500 ~ 950 DEG C, and the time of Reduction on Fluidized Bed is 30 ~ 90min; Finally, ferro-aluminum symbiosis breeze is discharged from last step fluidized-bed, and reduction degree reaches more than 50%, smelts for end reducing furnace;
The reduction tail gas that cyclonic separator in first step fluidized-bed in described multistage fluidized bed reactor is discharged through dedusting, wash and remove CO
2return after operation to be blended in end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle;
In described ferro-aluminum mineral intergrowth containing mass percent be: TFe content 31.13%-55%, Al
2o
3content 26.51%-30%;
Described multistage fluidized bed reactor is 2 ~ 4 grades.
2. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1, is characterized in that: the size range of described ferro-aluminum symbiosis breeze is 0.224 ~ 1mm.
3. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1, is characterized in that: described reductibility coal gas of high temperature reducing component CO%+H
2the volume content of % is preferably 70 ~ 98%.
4. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1, is characterized in that: in described fluidized-bed, reduction temperature is 650 ~ 900 DEG C.
5. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1, is characterized in that: the time of described Reduction on Fluidized Bed is 50 ~ 90min.
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