CN102925666A - 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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- CN102925666A CN102925666A CN2012104083663A CN201210408366A CN102925666A CN 102925666 A CN102925666 A CN 102925666A CN 2012104083663 A CN2012104083663 A CN 2012104083663A CN 201210408366 A CN201210408366 A CN 201210408366A CN 102925666 A CN102925666 A CN 102925666A
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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 the comprehensive utilization of ferro-aluminum mineral intergrowth field, the particularly method of pre-reduced iron in a kind of 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 the association component is many, and smelting condition is poor, and the iron ore average grade only has 33%.Therefore, the external interdependency of China's iron ore increases year by year, has reached 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.At present high-quality bauxite imbalance between supply and demand is very outstanding, and dilution trend has all appearred in mine 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 surpasses 1,500,000,000 tons, owing to iron grade and aluminium grade are low for being fully used.Therefore, by the Technology innovation, take full advantage of this part ferro-aluminum mineral intergrowth, can alleviate the imbalance between supply and demand of China's iron ore imports pressure and bauxite, significant to the Sustainable development of China's Iron And Steel Industry and aluminium industry.
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 are all lower, the total content of aluminum oxide and ferric oxide has reached about 70%, has the value of comprehensive utilization.Comprehensive utilization has " first smelting after the choosing ", " iron behind the first aluminium " and " aluminium behind the first iron " three kinds of general plannings for the ferro-aluminum mineral intergrowth at present.For " first smelting after the choosing " scheme, patent 200410010400.7 and 200610017376.9 has been announced the method that the magnetic separation of Iron In Iron-rich Containing Bauxite aluminium separates, but because iron-bearing mineral and the tight symbiosis of aluminum-containing mineral in the ore, disseminated grain size are superfine, monomer is difficult to dissociate, and the ferro-aluminum separating effect is difficult to reach re-set target.And patent 201010195045.0 has been announced the method that realizes the ferro-aluminum separation by magnetizing roasting, but owing in the ore Fe occurs
3+And Al
3+Lattice mutually replace, the isomorph phenomenon is obvious, magnetizing roasting is difficult to it is dissociated.For " iron behind the first aluminium " scheme, no matter sintering process, Bayer process or integrated process all requires 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, its bulk deposition causes severe contamination to environment.Therefore, " aluminium behind the first iron " scheme obtains favor gradually, and patent 200510200493.4 has been announced by sintering and blast-furnace smelting and carried iron, and puies forward the ferro-aluminum mineral intergrowth method of comprehensive utilization of aluminium from calcium aluminate slag, because ore Al
2O
3Content is high, causes slag melting rising, viscosity to increase, so that slag iron separation difficulty, the capacity factor of a blast furnace reduces.In order to reduce the aluminium content in the ore, patent 200710034845.2 has been announced by high-temperature roasting and NaOH solution and has been leached Al in the ore
2O
3Method, its objective is as obtaining high-grade iron ore concentrate for blast-furnace smelting, and complex process that 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 that whole reduction produces in the non-blast furnace smelting process, both can break away from the alumina content height to the restriction of blast-furnace smelting, all right energy-conserving and environment-protective realize the comprehensive utilization to the ferro-aluminum mineral intergrowth.
Technical scheme of the present invention: a kind of method of ferro-aluminum mineral intergrowth fluidized pre-reduction, its characteristics are: at first the ferro-aluminum mineral intergrowth is sieved, it is that the ferro-aluminum symbiosis breeze of 0.01～8mm is as raw material that sieve is got size range; Then with feeding screw the ferro-aluminum symbiosis breeze that filters out is sent into first step fluidized-bed in the multistage fluidized bed reactor, every grade of fluidized-bed is furnished with cyclonic separator; The reductibility coal gas of high temperature passes into from last step fluidized-bed bottom simultaneously, and described reductibility coal gas of high temperature is by the reductibility coal gas of high temperature of end reducing furnace generation with through dedusting, washs and remove CO
2The tail gas Mixed adjustment that returns after the operation and get 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, fluidized-beds at different levels and cyclonic separator are crossed in reverse flow successively; Ferro-aluminum symbiosis breeze goes downstream owing to the self gravitation effect, pass through successively fluidized-beds 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 and reverse contact of described reductibility coal gas of high temperature, 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, reduction temperature is 500～950 ℃ in the fluidized-bed, and the time of Reduction on Fluidized Bed is 30 ~ 90min; At last, ferro-aluminum symbiosis breeze is discharged from the 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 the first step fluidized-bed in the described multistage fluidized bed reactor is discharged through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.
Described multistage fluidized bed reactor is 2 ~ 4 grades.
Contain mass percent in the described ferro-aluminum mineral intergrowth and be 5 ~ 30% Al
2O
3, 30 ~ 70% TFe, 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 preferred 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.
Reduction temperature is 650～950 ℃ in the described fluidized-bed.
The time of described Reduction on Fluidized Bed is 50 ~ 90min.
The present invention's advantage compared with prior art is:
(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 that whole reduction produces in the non-blast furnace smelting process, both can break away from the alumina content height to the restriction of blast-furnace smelting, all right energy-conserving and environment-protective realize the comprehensive utilization to the ferro-aluminum mineral intergrowth.
(2) fluidization can directly be utilized breeze among the present invention, and mass transfer, heat transfer efficiency are high.Simultaneously, the generation of defluidization of can avoiding boning of the aluminum oxide of high-content can realize in enormous quantities, serialization production in the ferro-aluminum mineral intergrowth.
(3) the reduction tail gas that first step cyclonic separator is discharged among the present invention through dedusting, wash and remove CO
2Return after the operation to be blended in the 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 the recycle coal gas of high temperature, in the comprehensive utilization of ferro-aluminum mineral intergrowth, realize energy-saving and emission-reduction.
Description of drawings
Fig. 1 is process flow diagram of the present invention.
Embodiment
Introduce in detail the present invention below in conjunction with drawings and the specific embodiments.But following embodiment only limits to explain the present invention, and protection scope of the present invention should comprise the full content of claim, is not limited only to present embodiment.
At first filtering out granularity is raw material less than the ferro-aluminum symbiosis breeze of 8.00mm, then with feeding screw ferro-aluminum symbiosis breeze is sent into first step fluidized-bed in the multistage fluidized bed reactor, the reductibility coal gas of high temperature passes into from last step fluidized-bed bottom simultaneously, with the breeze countercurrent flow, fluidized-beds at different levels and cyclonic separator are crossed in reverse flow successively, and breeze passes through fluidized-beds at different levels successively because the self gravitation effect goes downstream, contact with the reductibility coal gas of high temperature is reverse, carry out fluidized reduction; At last, breeze is discharged from the 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 the end reducing furnace outlet coal gas and carries out Gas adjustment, realizes recycle.
Embodiment 1
Referring to Fig. 1, at first with TFe content 31.13%, Al
2O
3The ferro-aluminum mineral intergrowth of content 26.51% sieves, and chooses granularity and be the breeze of 0.074 ~ 0.150mm 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, passes into the reductibility coal gas of high temperature by fourth stage fluidized-bed R4 bottom simultaneously.The tail gas that the reductibility coal gas of high temperature that the 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 the operation and getting, its reducing component CO% is 90%.Gas passes into third stage fluidized-bed R3 after the gas solid separation of the coal gas of high temperature process fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges, gas passes into second stage fluidized-bed R2 after the gas solid separation of the coal gas of high temperature process third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges, the coal gas of high temperature that second stage fluidized-bed R2 discharges through the gas solid separation of second stage cyclonic separator S2 after gas pass into first step fluidized-bed R1, the coal gas of high temperature that first step fluidized-bed R1 discharges through the gas solid separation of first step cyclonic separator S1 after gas through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze that enters first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe behind the 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 that enters second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze that enters third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze that enters fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads behind the 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 the fluidized-bed internal pressure is 0.5MPa, and reduction temperature is 900 ℃ in the fluidized-bed, and the recovery time is 50min.Bonding defluidization phenomenon does not occur in whole reduction process, breeze reduction degree 52.64% after the reduction, degree of metalization 28.96%.
Embodiment 2
Referring to Fig. 1, at first with TFe content 31.13%, Al
2O
3The ferro-aluminum mineral intergrowth of content 26.51% sieves, and chooses granularity and be the breeze of 0.074 ~ 0.150mm 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, passes into high-temperature reductibility coal gas by fourth stage fluidized-bed R4 bottom simultaneously.The tail gas that the reductibility coal gas of high temperature that the 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 the operation and getting, its reducing component CO% is 90%.Gas passes into third stage fluidized-bed R3 after the gas solid separation of the coal gas of high temperature process fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges, gas passes into second stage fluidized-bed R2 after the gas solid separation of the coal gas of high temperature process third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges, the coal gas of high temperature that second stage fluidized-bed R2 discharges through the gas solid separation of second stage cyclonic separator S2 after gas pass into first step fluidized-bed R1, the coal gas of high temperature that first step fluidized-bed R1 discharges through the gas solid separation of first step cyclonic separator S1 after gas through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze that enters first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe behind the 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 that enters second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze that enters third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze that enters fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads behind the 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 the fluidized-bed internal pressure is 0.58MPa, and reduction temperature is 800 ℃ in the fluidized-bed, and the recovery time is 60min.Bonding defluidization phenomenon does not occur in whole reduction process, breeze reduction degree 53.85% after the reduction, degree of metalization 30.78%.
Embodiment 3
Referring to Fig. 1, at first with TFe content 31.13%, Al
2O
3The ferro-aluminum mineral intergrowth of content 26.51% sieves, and chooses granularity and be the breeze of 0.150 ~ 0.224mm 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, passes into high-temperature reductibility coal gas by fourth stage fluidized-bed R4 bottom simultaneously.The tail gas that the reductibility coal gas of high temperature that the 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 the operation and getting, its reducing component CO% is 98%.Gas passes into third stage fluidized-bed R3 after the gas solid separation of the coal gas of high temperature process fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges, gas passes into second stage fluidized-bed R2 after the gas solid separation of the coal gas of high temperature process third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges, the coal gas of high temperature that second stage fluidized-bed R2 discharges through the gas solid separation of second stage cyclonic separator S2 after gas pass into first step fluidized-bed R1, the coal gas of high temperature that first step fluidized-bed R1 discharges through the gas solid separation of first step cyclonic separator S1 after gas through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze that enters first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe behind the 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 that enters second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze that enters third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze that enters fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads behind the 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 the fluidized-bed internal pressure is 0.5MPa, and reduction temperature is 900 ℃ in the fluidized-bed, and the recovery time is 60min.Bonding defluidization phenomenon does not occur in whole reduction process, breeze reduction degree 54.68% after the reduction, degree of metalization 32.02%.
Embodiment 4
Referring to Fig. 1, at first with TFe content 31.13%, Al
2O
3The ferro-aluminum mineral intergrowth of content 26.51% sieves, and chooses granularity and be the breeze of 0.150 ~ 0.224mm 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, passes into high-temperature reductibility coal gas by fourth stage fluidized-bed R4 bottom simultaneously.The tail gas that the reductibility coal gas of high temperature that the 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 the operation and getting, its reducing component CO% is 98%.Gas passes into third stage fluidized-bed R3 after the gas solid separation of the coal gas of high temperature process fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges, gas passes into second stage fluidized-bed R2 after the gas solid separation of the coal gas of high temperature process third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges, the coal gas of high temperature that second stage fluidized-bed R2 discharges through the gas solid separation of second stage cyclonic separator S2 after gas pass into first step fluidized-bed R1, the coal gas of high temperature that first step fluidized-bed R1 discharges through the gas solid separation of first step cyclonic separator S1 after gas through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze that enters first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe behind the 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 that enters second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze that enters third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze that enters fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads behind the 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 the fluidized-bed internal pressure is 0.5MPa, and reduction temperature is 900 ℃ in the fluidized-bed, and the recovery time is 90min.Bonding defluidization phenomenon does not occur in whole reduction process, breeze reduction degree 62.87% after the reduction, degree of metalization 44.30%.
Embodiment 5
Referring to Fig. 1, at first with TFe content 30.71%, Al
2O
3The ferro-aluminum mineral intergrowth of content 21.30% sieves, and chooses granularity and be the breeze of 0.150 ~ 0.224mm 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, passes into high-temperature reductibility coal gas by fourth stage fluidized-bed R4 bottom simultaneously.The tail gas that the reductibility coal gas of high temperature that the 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 the operation and getting, its reducing component CO% is 98%.Gas passes into third stage fluidized-bed R3 after the gas solid separation of the coal gas of high temperature process fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges, gas passes into second stage fluidized-bed R2 after the gas solid separation of the coal gas of high temperature process third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges, the coal gas of high temperature that second stage fluidized-bed R2 discharges through the gas solid separation of second stage cyclonic separator S2 after gas pass into first step fluidized-bed R1, the coal gas of high temperature that first step fluidized-bed R1 discharges through the gas solid separation of first step cyclonic separator S1 after gas through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze that enters first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe behind the 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 that enters second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze that enters third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze that enters fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads behind the 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 the fluidized-bed internal pressure is 0.67MPa, and reduction temperature is 900 ℃ in the fluidized-bed, and the recovery time is 60min.Bonding defluidization phenomenon does not occur in whole reduction process, breeze reduction degree 54.98% after the reduction, degree of metalization 32.47%.
Embodiment 6
Referring to Fig. 1, at first with TFe content 54.75%, Al
2O
3The ferro-aluminum mineral intergrowth of content 5.1% sieves, and chooses granularity and be the breeze of 0.150 ~ 0.224mm 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, passes into high-temperature reductibility coal gas by fourth stage fluidized-bed R4 bottom simultaneously.The tail gas that the reductibility coal gas of high temperature that the 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 the operation and getting, its reducing component CO% is 80%.Gas passes into third stage fluidized-bed R3 after the gas solid separation of the coal gas of high temperature process fourth stage cyclonic separator S4 that fourth stage fluidized-bed R4 discharges, gas passes into second stage fluidized-bed R2 after the gas solid separation of the coal gas of high temperature process third-stage cyclone separator S3 that third stage fluidized-bed R3 discharges, the coal gas of high temperature that second stage fluidized-bed R2 discharges through the gas solid separation of second stage cyclonic separator S2 after gas pass into first step fluidized-bed R1, the coal gas of high temperature that first step fluidized-bed R1 discharges through the gas solid separation of first step cyclonic separator S1 after gas through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.In addition, the breeze that enters first step fluidized-bed R1 enters second stage fluidized-bed R2 by Gravitative Loads by tremie pipe behind the 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 that enters second stage fluidized-bed R2 enters third stage fluidized-bed R3 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of second stage cyclonic separator S2 gas solid separation also enters third stage fluidized-bed R3 by tremie pipe simultaneously; The breeze that enters third stage fluidized-bed R3 enters fourth stage fluidized-bed R4 by Gravitative Loads by tremie pipe behind the coal gas of high temperature fluidized reduction, the breeze of third-stage cyclone separator S3 gas solid separation also enters fourth stage fluidized-bed R4 by tremie pipe simultaneously; The breeze that enters fourth stage fluidized-bed R4 is discharged by tremie pipe by Gravitative Loads behind the 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 the fluidized-bed internal pressure is 0.5MPa, and reduction temperature is 700 ℃ in the fluidized-bed, and the recovery time is 70min.Bonding defluidization phenomenon does not occur in whole reduction process, breeze reduction degree 73.68% after the reduction, degree of metalization 40.35%.
Reach a conclusion thus: by the inventive method prereduction ferro-aluminum mineral intergrowth, production efficiency is high, has avoided simultaneously the generation of bonding defluidization, thereby can serialization mass disposal ferro-aluminum mineral intergrowth, and the recycle coal gas of high temperature in the comprehensive utilization of ferro-aluminum mineral intergrowth, is realized energy-saving and emission-reduction.
Need to prove 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 fully, implementation procedure and method same the various embodiments described above; And the non-elaborated part of the present invention belongs to techniques well known.
The above; only be part embodiment of the present invention, but protection scope of the present invention is not limited to this, any those skilled in the art are in the technical scope that the present invention discloses; the variation that can expect easily or replacement all should be encompassed within protection scope of the present invention.
Claims (11)
1. the method for a ferro-aluminum mineral intergrowth fluidized pre-reduction is characterized in that: at first the ferro-aluminum mineral intergrowth is sieved, it is that the ferro-aluminum symbiosis breeze of 0.01～8mm is as raw material that sieve is got size range; Then with feeding screw the ferro-aluminum symbiosis breeze that filters out is sent into first step fluidized-bed in the multistage fluidized bed reactor, every grade of fluidized-bed is furnished with cyclonic separator; The reductibility coal gas of high temperature passes into from last step fluidized-bed bottom simultaneously, and described reductibility coal gas of high temperature is by the reductibility coal gas of high temperature of end reducing furnace generation with through dedusting, washs and remove CO
2The tail gas Mixed adjustment that returns after the operation and get 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, fluidized-beds at different levels and cyclonic separator are crossed in reverse flow successively; Ferro-aluminum symbiosis breeze goes downstream owing to the self gravitation effect, pass through successively fluidized-beds 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 and reverse contact of described reductibility coal gas of high temperature, 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, reduction temperature is 500～950 ℃ in the fluidized-bed, and the time of Reduction on Fluidized Bed is 30 ~ 90min; At last, ferro-aluminum symbiosis breeze is discharged from the last step fluidized-bed, and reduction degree reaches more than 50%, smelts for end reducing furnace.
2. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 is characterized in that: the reduction tail gas that the cyclonic separator in the first step fluidized-bed in the described multistage fluidized bed reactor is discharged through dedusting, wash and remove CO
2Return after the operation to be blended in the end reducing furnace outlet coal gas and carry out Gas adjustment, realize recycle.
3. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 and 2 is characterized in that: contain mass percent in the described ferro-aluminum mineral intergrowth and be 5 ~ 30% Al
2O
3, 30 ~ 70% TFe.
4. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 and 2, it is characterized in that: described multistage fluidized bed reactor is 2 ~ 4 grades.
5. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 3 is characterized in that: the Al of described ferro-aluminum symbiosis breeze
2O
3Content is that 15～30%, TFe content is 30 ~ 55%.
6. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1, it is characterized in that: the size range of described ferro-aluminum symbiosis breeze is 0.05～1mm.
7. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 and 2 is characterized in that: described reductibility coal gas of high temperature reducing component CO%+H
2The volume content of % is preferred 70 ~ 98%.
8. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 and 2, it is characterized in that: described fluidizing gas velocity is 0.2～0.4m/s.
9. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 and 2, it is characterized in that: described multistage fluidized bed internal pressure hold-in range is 0.4～0.8MPa.
10. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 and 2 is characterized in that: reduction temperature is 650～900 ℃ in the described fluidized-bed.
11. the method for ferro-aluminum mineral intergrowth fluidized pre-reduction according to claim 1 and 2 is characterized in that: the time of described Reduction on Fluidized Bed is 50～90min.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103725819A (en) * | 2013-12-31 | 2014-04-16 | 中国科学院过程工程研究所 | Iron ore powder fluidized reduction system and method |
| CN106929665A (en) * | 2017-03-14 | 2017-07-07 | 江苏省冶金设计院有限公司 | A kind of system and method for processing high-iron bauxite |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102528068A (en) * | 2012-01-16 | 2012-07-04 | 中国科学院过程工程研究所 | Device and method for preparing superfine nickel powder |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102528068A (en) * | 2012-01-16 | 2012-07-04 | 中国科学院过程工程研究所 | Device and method for preparing superfine nickel powder |
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| 张奔等: "流态化气基还原高铝铁矿的研究", 《中国稀土学报》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103725819A (en) * | 2013-12-31 | 2014-04-16 | 中国科学院过程工程研究所 | Iron ore powder fluidized reduction system and method |
| CN103725819B (en) * | 2013-12-31 | 2015-06-03 | 中国科学院过程工程研究所 | Iron ore powder fluidized reduction system and method |
| CN106929665A (en) * | 2017-03-14 | 2017-07-07 | 江苏省冶金设计院有限公司 | A kind of system and method for processing high-iron bauxite |
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