专利摘要:
Verfahren zur Schmelzreduktion von Eisenerzen, bei dem das Eisenoxid im wesentlichen im flüssigen Zustand reduziert wird und die erforderliche Energie zum Ausgleich der Wärmebilanz des Prozesses durch die Zugabe kohlenstoffenthaltender Brennstoffe an die Schmelze und durch die Nachverbrennung der entstehenden Reaktionsgase, haptsächlich CO and H2, erzeugt wird, wobei die Reaktionsgase nacheinander zweimal oder häufiger in sauerstoffenthaltenden Gasstrahlen, die in Reaktionsräume blasen, die wirkungsmäßig unabhängig voneinander sind, nachverbrannt werden.
公开号:SU1500166A3
申请号:SU874202169
申请日:1987-03-06
公开日:1989-08-07
发明作者:Эдвин Турнер Рихард;Броцманн Карл;Фасбиндер Ханс-Георг
申请人:Клекнер Кра Технологи Гмбх (Фирма);
IPC主号:
专利说明:

The invention relates to ferrous metallurgy, to methods for reducing smelting of iron ores, in which iron oxide is reduced in a liquid state.
The purpose of the invention is to reduce energy costs.
FIG. 1 given a drum melting reactor with perpendicular feed blow; in fig. 2 - the same, with a different direction to blow, a longitudinal section; in fig. 3 - the same, with the attached second reactor, a longitudinal section; in fig. 4 - the same, with a cooling chamber for flue gas and a cyclone.
Example 1. The drum, smelting reactor 1 rotates around its axis of symmetry. Hot blast is fed through conduit 2 to two tuyeres 3 and 4. The combustion gas flows from above to the surface of the melt. The first reaction zone is formed under lance 3, and the second under lance 4. Carbon-containing fuels, mainly pulverized coal, are fed into the melt through nozzles 5. Other types of coal additives are possible, for example by blowing. The crushed ore is fed through conduit 6 and is blown in with the second burned gas.
WITH
with.
flow through the lance 4. The movement of gases in the melting reactor 1 is shown by arrows. Both reaction zones (Fig. 1) function independently of one another, i.e. separately in the gas phase, since the jets are characterized by high stability. Both streams of the afterburning gas can be directed opposite to each other in the upper region (Fig. 2). At the same time, the nozzles should be located so that the gas jets do not intersect in space.
A variant of the method with a melting reactor, a first reaction zone 7 and an attached second reaction zone 8. is shown in FIG. 3. In this case, the liquid phase is also located in two separate reaction zones. Exhaust gases from the first reaction zone 7 through the opening 9 enter the second water-cooled reaction zone 8. In the reaction zone 8, the exhaust gases from the melting reactor are combusted using two streams of gas from the nozzles 10. Simultaneously, the ore that is fed to the nozzles 10 is pipeline 6j melts and is thermally reduced to FeO. Molten vustite along a water cooled chute. 11 flows into the first reaction zone 7, i.e. into the melting reactor. Consequently, liquid vustite, not in contact with fireproof material, is added to the melt in the first reaction zone 7.
The flue gases from the fusion reactor 1 pass through the rotating passage 12 and are cooled in the attached cooled chamber 13 by feeding lime through the opening 1A and crushed ore through the opening 15 (Fig. 4). At the same time, these powdered substances simultaneously capture the metal drops contained in the exhaust gas. Lime and ore dp gas cooling are added one after the other. Due to this, limestone neutralization occurs rapidly at high temperatures and then the ore is heated. After cooling, the powdery substances are separated in hot water in the cyclone 16, and if necessary, the mixture of gas and solid can be pre-cooled even more. Dp this can add0
0
five
0
five
0
five
0
five
In this case, the recirculating waste gas is pre-cyclone 10. A mixture of preheated ore (about) and lime is fed from the cyclone 16 through line 17 to the afterburning gas stream coming out of the tuyere 4. From the melting reactor, some of the exhaust gases can be flow through conduit 18 to the recovery boiler, and this part of the waste gases, for example, can be used for hot blowing. . .
In a melting reactor similar to that shown in FIG. 4, to obtain 1 ton of iron, 550 kg of gas-flame coal with 33% of volatile components and a calorific value of 7200 kcal / kg are blown through the bottom nozzles 5. Dp to further promote heat transfer from the stream of the incinerated gas in the first reaction zone between an additional about 5% of the total amount of ore is supplied through the nozzles 5. Through the lance 3 1800 m of hot blowing with a temperature of about 1200 C is supplied. In this case It is possible to achieve a burnout degree of 40%, i. The off-gas that leaves the first reaction zone has an average oxidation degree of 40%. In the second reaction zone, another 800 nm of hot lance is blown through the lance 4 at the same temperature and, therefore, a total burnout level of 80% is provided. Along with this stream of the afterburning gas, ore and lime, heated to a temperature of about 700 ° C, are fed to the second reaction zone on the bath surface. It forms 2100 m of waste gas with a heat capacity of 1.3 kcal and chemical, i.e. heat capacity of 0.4 kcal. Immediately after passing through the revolving passage 12, this waste gas is cooled by feeding the ore and the total amount of limestone to about 300 kg per ton of iron. At the same time, the average temperature is set at about 1200 ° C. Dp. Of further cooling to the temperature immediately before the cyclone, about 500 nm of recycle flue gas is added.
Example 2. Approximately 50 tons of liquid iron in 1 is formed into an extensive drum melting reactor having a length of 10 m and a diameter of 6 m, with a refractory lining 60 cm thick, preferably about 600 kg are fed into the first reaction zone into the molten iron gas flame per ton of iron. The total amount of carbon required for the combustion of oxygen is blown through six nozzles with a free jet about 5 m long with a uniform distribution over the bath surface of the reaction zone. At the same time, in order to improve the degree of afterburning, approximately 5% of the total ore is introduced below the bath surface in the region of the first reaction zone.
On its way to the exit from the melting reactor, the exhaust gas passes through the second reaction zone, in which hot blast is fed to the bath using the same technology as in the first reaction zone. The hot blast is mixed with fine ore, which is heated as a result. Due to the addition of ore and hot air in the area of the bath surface in the second reaction zone, the increased content of iron oxide in the slag is established in comparison with the first reaction zone. The degree of afterburning achieved in the second reaction zone is about 80% and 90% of this heat, as in the first reaction zone, is transferred to the bath. In order to improve the circulation of the bath and the associated improvement in heat transfer from the stream of afterburning gas, it is advisable to introduce an inert gas with or without coal dust under the bath surface in the area of the second reaction zone. The method significantly reduces energy costs.
F Ormula of the invention 1, Method of smelting reduction of iron ores, including recovery
five
0
five
0
five
iron oxide n; ,, i; obi state, the flow of carbon into the melt. holding the fuel, the afterburning of the resulting reaction gases, mainly CO and Hj, to conserve energy, equalizing the heat balance, characterized in that 5, in order to reduce energy costs, the reaction gases are subsequently burned at least twice in independent reaction zones.
2. The method according to claim 1, wherein the mixture is molded in a zone of high reduction potential.
3. Method by software. 1 to 2, characterized in that multi-stage afterburning is carried out in one or two series-connected containers.
4. Method according to paragraphs. 1-3, which is such that the crushed ore is introduced into the second or one of the subsequent afterburning reaction zones.
5. Method according to paragraphs. 1–4, which means that carbon dioxide-containing fuel is introduced into the first afterburning zone with the maximum reduction potential.
6. Method according to paragraphs. i-5, about tl and .- that the oxygen-containing blast is fed obliquely to the surface of the melt.
40
7. Method according to paragraphs. 1-6, about tl and - by the fact that the degree of afterburning in the first zone is 30- - 50%, and with repeated afterburning 60-100%.
8. Method according to paragraphs. 1-7, about the tol. With the fact that preheated air is not used for afterburning 4g.
;. :
Phi2.1
fig.Z
权利要求:
Claims (8)
[1]
Claim
1, A method for the reduction smelting of iron ores, including the reduction of iron oxide in the;.; H - .com state, the supply of carbon-. containing fuels, afterburning of the resulting reaction gases, mainly СО and Н а , in order to save energy equalizing the heat balance, characterized in that, in order to reduce energy costs, re ~ 1θ the reaction gases sequentially burn at least twice in independent from one another reaction • zones.
[2]
2. The method of pop. 1, due to the fact that in the zone of high reduction potential, the melt is circulated.
[3]
3. The method according to PP. 1 and 2, characterized in that the multistage
20 afterburning is carried out in one or two series-connected containers.
[4]
4. The method according to PP. 1-3, about t l and chaya that is crushed -
25 n ore is introduced into the second or one of the subsequent afterburning reaction zones.
[5]
5. The method according to PP. 1-4, about t l and -
30, in that, carbon-containing fuel is introduced into the first afterburning zone with maximum reduction potential.
[6]
6. The method according to PP. 1-5, Otl and „-Characterizing in that the oxygen-containing blast is fed obliquely to the surface of the melt.
[7]
7. The method according to PP. 1-6, about t l and -
40, which is due to the fact that the degree of afterburning in the first zone is 3050%, and after repeated afterburning is 60-100%.
[8]
8. The method according to PP. 1-7, t l.
45 nii use preheated air.
Fig. H
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同族专利:
公开号 | 公开日
BR8701047A|1988-01-05|
CA1286113C|1991-07-16|
JPS62263908A|1987-11-16|
CS147287A2|1988-09-16|
KR920000520B1|1992-01-14|
CN87102252A|1987-09-16|
JPH0219167B2|1990-04-27|
DE3763487D1|1990-08-09|
US4798624A|1989-01-17|
KR870009033A|1987-10-22|
EP0236802B2|1997-11-19|
CS265234B2|1989-10-13|
EP0236802B1|1990-07-04|
EP0236802A2|1987-09-16|
ZA871469B|1987-08-17|
DE3607775C2|1988-08-25|
IN166837B|1990-07-21|
AU572043B2|1988-04-28|
AU6919987A|1987-09-10|
ES2000076B3|1990-09-01|
EP0236802A3|1988-06-01|
ES2000076T5|1998-01-01|
AT54333T|1990-07-15|
CN1005274B|1989-09-27|
DE3607775A1|1987-09-17|
ES2000076A4|1987-11-16|
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法律状态:
优先权:
申请号 | 申请日 | 专利标题
DE3607775A|DE3607775C2|1986-03-08|1986-03-08|
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