CN101999004B - Method for producing sintered ore - Google Patents
Method for producing sintered ore Download PDFInfo
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- CN101999004B CN101999004B CN2009801126413A CN200980112641A CN101999004B CN 101999004 B CN101999004 B CN 101999004B CN 2009801126413 A CN2009801126413 A CN 2009801126413A CN 200980112641 A CN200980112641 A CN 200980112641A CN 101999004 B CN101999004 B CN 101999004B
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/16—Sintering; Agglomerating
- C22B1/20—Sintering; Agglomerating in sintering machines with movable grates
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0086—Conditioning, transformation of reduced iron ores
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
- C21B13/146—Multi-step reduction without melting
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- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/14—Agglomerating; Briquetting; Binding; Granulating
- C22B1/16—Sintering; Agglomerating
- C22B1/20—Sintering; Agglomerating in sintering machines with movable grates
- C22B1/205—Sintering; Agglomerating in sintering machines with movable grates regulation of the sintering process
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B5/00—General methods of reducing to metals
- C22B5/02—Dry methods smelting of sulfides or formation of mattes
- C22B5/18—Reducing step-by-step
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
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- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
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Abstract
Disclosed is a sintered ore production process in which some or all of the iron ore powder which includes the crystallized water of Pisolite or Marra Mamba minerals etc. used as the sintering raw material is subjected to preliminary reduction in a reducing furnace, as a fluidized layer for example, using reducing gas such as blast furnace gas, and the crystallized water in the iron ore powder is removed and at the same time the hematite in the powdered iron ore is reduced to magnetite or wustite. Then a raw material wherein other iron ore powder, miscellaneous sources of iron, auxiliary raw materials, returned ore and setting material have been compounded with the pre-reduced iron ore is used in the sintered ore powder production process.
Description
Technical field
The present invention relates to the manufacture method of the agglomerate in the steel plant process, particularly the iron ore powder that contains crystal water is used for the manufacture method of the agglomerate of raw materials for sintering.
Background technology
In the manufacturing processed of agglomerate, as raw materials for sintering, use main raw material and the slag making materialses (auxiliary material) such as iron ore powder and assorted source of iron.The minus sieve that assorted source of iron is included in the sintering factory system and the sintering factory system produces outward, dust, rolled iron phosphorus etc. contain ferrous components.Slag making materials (auxiliary material) is Wingdale etc.Like this, in the manufacturing processed of agglomerate, use the different multiple raw materials for sintering of chemical composition.So the agglomerate for the chemical composition of making the operation that is suitable for blast furnace suitably cooperates raw materials for sintering usage ratio separately.And, with suitably cooperated multiple raw materials for sintering, added coke, material behind the coagulated material of coal etc. is as cooperating raw material.At general De Huaite-Selwyn Lloyd (De ワ イ ト ロ イ De) (DL) in the sintering process of formula sinter machine, making the below by the packing layer that cooperates raw material to consist of is negative pressure, air is circulated downwards from the top, make the coagulated material burning that cooperates in the raw material.And, the agglomerate that the main raw material that contains ferrous components and the auxiliary material sintering of iron ore powder etc. is manufactured blocking by the combustion heat that produces.This agglomerate is used as main raw material in blast furnace.
The higher coal of volatile component can not former state use as the coagulated material in the manufacturing processed of agglomerate, so use as coagulated material mixing afterwards with the coke of powdery or hard coal etc.The coke that uses in coagulated material is that the coke that will be not suitable for using in blast furnace because particle diameter is less is further pulverized the coke of making the particle diameter that is suitable as coagulated material.But particle diameter is less and to be not suitable for the amount of the coke that blast furnace uses less with respect to the amount of the coagulated material that needs in sintering process.Therefore, the amount of deficiency is replenished with hard coal.
Main raw material as the manufacturing processed of agglomerate is iron ore powder, can use hematite etc.But, the feed rate of hematite etc. reduces in recent years, as iron ore powder, spread out river (ロ one Block リ バ one) (Robe River) ore and Yang Di (ヤ Application デ イ Network one ジ Na) (Yandicoojina) usage quantity of Ma Lamanba (マ ラ マ Application バ) (Marra Mamba) ore etc. of peastone (the ピ ソ ラ イ ト) ore of ore etc. and western Angelis (ウ エ ス ト ア Application ジ エ ラ ス) (West Angeles) ore etc. increase.These iron ore powders contain crystal water.If will contain the iron ore powder of crystal water as the main raw material use of the manufacturing processed of agglomerate, then need a large amount of heat in the thermolysis of the crystal water in iron ore powder, so the usage quantity of the coagulated material of the supply source of conduct heat increases.That is, in the manufacturing processed of agglomerate, increase the usage quantity of the iron ore powder that contains crystal water, so improved the ratio (coagulated material ratio) of coagulated material.
But, if improve the coagulated material ratio, the heat that then passes through the burning generation of coagulated material becomes large, in the process that sintering reaction carries out in by the packing layer that cooperates raw material to consist of, the high-temperature area that combustion heating by coagulated material forms in packing layer enlarges, and fused solution excessively generates.Therefore, aeration resistance in the sintered layer rises, hindered coagulated material the needed air of burning supply and the productivity of agglomerate descends.And then, making the pore amount minimizing of agglomerate by the fused solution of excessive generation, the being reduced property decline of agglomerate causes the rising of the ratio (reducing material ratio) of the needed reducing material of ironmaking in the blast furnace, and economy descends.
In patent documentation 1, as the method for operating blast furnace that it doesn't matter of the manufacturing processed with agglomerate, record the technology that the reduced iron behind the reduction of iron ore that use will contain crystal water uses as blast furnace raw material.
But, the technology of this method for operating blast furnace can not be applied in the manufacturing processed of agglomerate.In addition, in this technology, need to use the higher reducing gas of reducing power in order to make the reduction ratio 30% that contains metallic iron for the manufacturing of above reduced iron.Therefore, the cost that spends in the manufacturing of reducing gas is higher, and the price of the reduced iron of manufacturing is higher.
In addition, the rising of the coagulated material ratio increase that also brings anthracitic usage quantity.But, since anthracitic reserves than bituminous coal and sub-bituminous coal lack, market is less, so consider the stable difficulty of buying, its absolute magnitude is not enough in the future.If anthracitic feed rate is not enough, the coke that then can consider the size that will originally can use in blast furnace pulverizes to guarantee the amount of coagulated material.But, in the case, might need usage quantity or the increase coke production amount of the high raw material charcoal of the expensive cementability of newly-built coke oven or increase or buy expensive coke.That is, owing to can cause the significantly rising of expense, the coke of the size that will can use in blast furnace is used for coagulated material and uneconomical.
Patent documentation 1: Japanese kokai publication hei 9-165607 communique
Summary of the invention
The purpose of this invention is to provide a kind of manufacture method that can reduce the coagulated material ratio in the situation of using the iron ore that contains crystal water and can improve productive agglomerate.
The present invention is in order to address the above problem, take following as purport.
That is, purport of the present invention is as follows.
(1) a kind of manufacture method of agglomerate is characterized in that, the iron ore that will contain crystal water uses the reducing gas reduction, and the reduction ore that obtains is used for raw materials for sintering, makes agglomerate.
(2) such as the manufacture method of above-mentioned (1) described agglomerate, it is characterized in that, the above-mentioned iron ore that contains crystal water be peastone ore or Ma Lamanba ore at least any.
(3) such as the manufacture method of above-mentioned (1) or (2) described agglomerate, it is characterized in that, use fluidised bed to carry out above-mentioned reduction.
(4) such as the manufacture method of each described agglomerate in above-mentioned (1)～(3), it is characterized in that, as the reducing gas that in above-mentioned reduction, uses, use the gas behind the blast furnace gas partial oxidation.
(5) such as the manufacture method of above-mentioned (4) described agglomerate, it is characterized in that, the installation for blast furnace gas of above-mentioned partial oxidation is being added more than one that select in advance from coal gas of converter, coke-oven gas, Sweet natural gas, liquefied petroleum gas (LPG), other gases higher than blast furnace gas thermal value.
Description of drawings
Fig. 1 is the figure of an example of manufacture method of agglomerate of the use reduction ore of the relevant embodiments of the present invention of expression.
Fig. 2 is the figure of an example of the heating curve of the raw materials for sintering layer on the sinter machine main body of expression embodiments of the present invention.
Fig. 3 is the figure of manufacture method of agglomerate of the use reduction ore of the relevant embodiments of the invention of expression.
Embodiment
The particle diameter of the iron ore powder that uses in the manufacturing processed of agglomerate is normally about 10mm.The Ma Lamanba ore of peastone ore in the iron ore powder that uses in the manufacturing processed of agglomerate, that spread out river ore and Yang Di ore etc. and western Angelis ore etc. contains crystal water.The peastone ore contains about 8%, the Ma Lamanba ore contains about 3% crystal water, these iron ore powders are for example produced in Australia.
The 1st scheme of the manufacture method of agglomerate of the present invention is characterised in that, will contain the iron ore use reducing gas reduction of crystal water, and the reduction ore that obtains is used for raw materials for sintering, makes agglomerate.
As mentioned above, if will contain the iron ore powder former state of crystal water as the raw materials for sintering use of the manufacturing processed of agglomerate, then need heat in the thermolysis of the crystal water in iron ore powder, so the usage quantity of the coagulated material of the supply source of conduct heat increases.On the other hand, if use reducing gas to reduce to the iron ore of iron ore powder etc., then can under the temperature that is suitable for reducing, the crystal water in the iron ore be removed in reduction.Therefore, if the reduction ore that will obtain is used for raw materials for sintering, then do not need the thermolysis of crystal water, so can reduce the coagulated material ratio., compare as the situation that raw materials for sintering uses with the iron ore powder former state that will contain crystal water thereupon, can cut down expensive anthracitic usage quantity, and the ventilation resistance in the sintered layer reduces, can improve the productivity of agglomerate.And then, because the increase of the pore amount of agglomerate, so can improve the being reduced property of agglomerate.
In addition, to be used for the being reduced property of the agglomerate that raw materials for sintering makes good owing to will reducing ore, thus can reduce in the blast furnace the reducing material ratio, reduce expensive coke and the usage quantity of coal dust.
In addition, as the iron ore that contains crystal water as raw materials for sintering, preferably use at least a iron ore that comprises peastone ore or Ma Lamanba ore.
In addition, preferably use the fluidised bed reduction furnace to carry out above-mentioned reduction.
Be about 10mm or in the reduction of the iron ore of the bulk of the size more than it at particle diameter, use shaft furnace or converter etc.But, the Ma Lamanba ore (for example Australia product) of the above-mentioned peastone ore of spreading out river ore and Yang Di ore etc. and western Angelis ore etc. is powdery following about particle diameter 10mm, so at the reduced ore cubic meter of stone face of the reduction of these iron ore former states being made the powdery that can use as raw materials for sintering, the fluidised bed reduction furnace is fit to.
Here, with reference to Fig. 1, embodiments of the present invention are described.Here, the method for using the fluidised bed reduction furnace is described.
In Fig. 1, the iron ore powder 11 of raw material is supplied in the fluidised bed reduction furnace 1, reduce by reducing gas 15.The reduction ore 19 that will obtain in fluidised bed reduction furnace 1 and other raw materials (iron ore, assorted source of iron, auxiliary material, return mine and coagulated material 20) mix and make and cooperate raw material 21, be encased in the sinter machine main body 5.Agglomerate 23 fragmentations that to discharge from sinter machine main body 5 with sieve 7 sieves, are separated into tiny under the finished product agglomerate 24 of the particle diameter that is suitable as blast furnace raw material on the sieve and the sieve and return mine 25.
In addition, as the reducing gas that in reduction, uses, preferably use the gas behind the installation for blast furnace gas partial oxidation.As the reducing gas that in reduction, uses, also can use the gas behind coal gas of converter, coke-oven gas, Sweet natural gas, the liquefied petroleum gas (LPG) partial oxidation, will be than the gas behind the cheap blast furnace gas partial oxidation of coal gas of converter, coke-oven gas, Sweet natural gas, liquefied petroleum gas (LPG) but particularly preferably use.If with the blast furnace gas partial combustion, then can access the reducing gas of high temperature, so easily the fluidised bed temperature of reaction is warmed up to the needed temperature of reduction of iron ore.Also the blast furnace gas former state can be used as reducing gas, but in the case, for the fluidised bed temperature of reaction being warmed up to the needed temperature of reduction of iron ore, produced the needs that the preheating temperature of blast furnace gas improved or iron ore is preheating to high temperature etc., it is large that machine utilization becomes.Therefore, with use the situation of the gas after the blast furnace gas partial combustion (partial oxidation) is compared, equipment cost rises, and uneconomical.In addition, be not limited to blast furnace gas, state in the use in the situation of coal gas of converter, coke-oven gas etc., preferably the reducing gas as high temperature uses with similarly partial combustion of blast furnace gas.
In example shown in Figure 1, utilize the sensible heat of fluidised bed reduction furnace Exhaust Gas 16 to use heat exchanger 2 with blast furnace gas 12 preheatings.Make the preheating blast furnace gas 13 after the preheating further in partial combustion burner 3, obtain reducing gas 15 by air 14 partial combustions.Reducing gas 15 is with CO gas, CO
2Gas and N
2Gas is principal constituent.The reducing gas 15 that obtains is like this supplied in the fluidised bed reduction furnace 1, and the iron ore powder that contains crystal water 11 with peastone ore or Ma Lamanba ore etc. in fluidised bed reduction furnace 1 reduces.
The fluidised bed reduction furnace Exhaust Gas 16 that to discharge from the top of fluidised bed reduction furnace 1 is used for the preheating of blast furnace gas 12 as described above heat exchanger 2, then, the sensible heat of residual again heat exchanger Exhaust Gas 17 is used for vapor recovery in waste heat recovery unit 4, waste heat recovery unit gas 18 is processed outside system.
In addition, in the temperature of wanting to improve reducing gas 15 or improve in the situation of reducing power, preferably to add at least one of blast furnace gas 12 or preheating blast furnace gas 13 from coal gas of converter, coke-oven gas, Sweet natural gas, liquefied petroleum gas (LPG), other than select the high gas of blast furnace gas thermal value more than one.
Because reduction rate is slower under the low temperature about than 700 ℃, so be made as more than 700 ℃ reduction temperature better for obtaining higher reduction ratio.Because the crystal water of peastone ore or Ma Lamanba ore etc. is since about 350 ℃ decomposition, so by reduce processing under the temperature more than 700 ℃, crystal water is also removed simultaneously.If more than being heated to ore about 1200 ℃ in the reducing gas environment, then partial melting and each other welding of particle is so preferably reduce processing about than 1200 ℃ under the low temperature.Become preheating blast furnace gas 13 owing to will in heat exchanger 2, heating up as the blast furnace gas 12 of raw material, again partial combustion in partial combustion burner 3, temperature is risen and become the reducing gas 15 of high temperature, so can will guarantee that the heat on the basis of above-mentioned reduction temperature supplies with as the sensible heat of reducing gas 15.
The reducing gas 15 that makes blast furnace gas 12 partial combustions and make is because CO
2The gaseous constituent ratio is high and H with respect to the ratio of its CO gaseous constituent ratio
2O gaseous constituent ratio is with respect to its H
2The ratio of gaseous constituent ratio is high, so although not with the reducing power of reduction of iron ore to metallic iron, can revert to wustite.But when reduction temperature was low, reduction rate was slower, so although can promptly revert to magnetite from rhombohedral iron ore, spended time in the reduction from the magnetite to the wustite.Thereby, if by reducing gas 15 that blast furnace gas 12 partial combustions make is reduced the iron ore powder that contains crystal water 11 of peastone ore or Ma Lamanba ore etc. in fluidised bed reduction furnace 1, can access then that crystal water is removed, the reduction ore 19 (situation that also has iron in a part is arranged) between mainly being restored to from the magnetite to the wustite.
As mentioned above, in order to be that the Ma Lamanba ore former state reduction of the peastone ore of spreading out river ore and Yang Di ore etc. of powdery following about 10mm and western Angelis ore etc. makes can be as the reduction ore of the powdery of raw materials for sintering use with particle diameter, the fluidised bed reduction furnace is fit to.But, for example in the peastone ore and Ma Lamanba ore that produce in Australia, although be a small amount of, have to mix that particle diameter is arranged is the situation of the piece about below the above 20mm of 10mm.As the fluidised bed reduction furnace of the iron ore powder reduction that such size-grade distribution amplitude is larger, to compare with bubbly flow layer reduction furnace, the circular flow reduction furnace is more suitable.In bubbly flow layer reduction furnace, have more than the mobile commencing speed that gas flow rate need to be controlled to be particle and below the end speed, keep well the flow state of the particle in the fluidised bed and suppress particle from the situation of dispersing of fluidised bed.Therefore, if the size-grade distribution amplitude of iron ore powder is large situation about can not tackle is arranged.On the other hand, in the circular flow reduction furnace, because the particle that will disperse captures with swirler and make particle at the fluidised bed internal recycle, so can be with larger gas flow rate running.The reason that the circular flow reduction furnace is fit to be because, owing to can process micropartical from the capture limit of swirler to the oversize particle corresponding to larger gas flow rate, so can use the larger particle of size-grade distribution amplitude (iron ore powder).
The peastone ore of the powdery below using about 10mm or Ma Lamanba ore are in the situation that reduce in the circular flow reduction furnace; if the superficial velocity of reducing gas crosses low then coarse grain meeting bias is deposited in the bottom of fluidised bed; become the larger state of pressure variation (slagging scorification state), the situation that has reduction efficiency to descend.On the other hand, if the superficial velocity of reducing gas is too high, then become the less thin state of particle hold-up of iron ore in the fluidised bed, the situation that has reduction efficiency to descend.Thereby, in order to obtain stable flow state, the superficial velocity of reducing gas preferably about 4m/s to about the 15m/s.
In embodiments of the present invention, as shown in Figure 1, the iron ore 11 that will contain crystal water uses reducing gas 15 reduction, and the reduction ore 19 that obtains is used for raw materials for sintering, carries out the sintering of this reduction ore 19, makes agglomerate 23.If the ore 19 of will reducing is used for raw materials for sintering, then raw materials for sintering is exposed in the environment of high temperature gas that contains aerobic in sintering process, the heat release so reduction ore 19 is oxidized.Thereby the heat that the burning by coagulated material can be produced reduces the amount corresponding to the heat that is supplied to as the heat of oxidation based on the reduction ore oxidation.That is, by reducing ore for raw materials for sintering, can reduce the usage quantity of the coagulated material in the sintering.The reduction ratio of reduction ore is higher, the per unit mass of reduction ore carry out oxidation the time heat that produces larger, so when the usage quantity of reduction ore be that one regularly the effect of the higher usage quantity that then reduces coagulated material of reduction ratio is larger.In addition, when the reduction ratio of reduction ore when identical, the more at most oxidation thermal value of usage quantity of reduction ore is larger, so it is larger to reduce the effect of usage quantity of coagulated material.And then, owing to being removed at the Crystallization water of making the reduction ore, so by using the reduction ore, no longer need to use to supply with the use of coagulated material of the needed heat of decomposition of crystal water.Thereby, also can reduce the usage quantity of this part coagulated material.
In the oxidation of the reduction ore in sintering process, because iron ore self heat release, so oxidation reaction heat is to the temperature rising direct effect of iron ore, with respect to this, in the burning of coagulated material, by the heat transfer from the coagulated material particle of the combustion gases of high temperature and the high temperature in the combustion processes, iron ore heats up.Thermal value and the heating-up time of the more coagulated material of thermal value that therefore, need to bring than the oxidation of reduction ore.
Thereby, compare with the situation of using the reduction ore, in the situation that do not use the reduction ore, the high-temp combustion that forms in sintered layer by the burning of agglomerated material zone becomes large.That is, about the heating mode in the raw materials for sintering layer, as shown in Figure 2, compare with the heating mode 32 in the situation of not using the reduction ore, the heat-up rate of the heating mode 31 in the situation of use reduction ore is larger and speed of cooling is larger.As a result, can suppress the obstruction of the pore that the generation of excessive fused solution, the fused solution that suppresses to generate cause, so if use the reduction ore, then can make the higher agglomerate of being reduced property.
And then, if the peastone ore or the Ma Lamanba ore former state that replace containing crystal water are used and use reduction ore 19 as raw materials for sintering, then origin reduces in the steam output of the steam of crystal water in sintering, and along with the usage quantity of the needed coagulated material of thermolysis of crystal water descends, reduce in the high-temp combustion zone that the oxidation of the burning by coagulated material and reduction ore forms, and has suppressed the generation of excessive fused solution.Therefore, the pressure-losses of sintered layer 22 shown in Figure 1 descends.Therefore, attracting the attraction negative pressure of gas blower 6 at sintering master Exhaust Gas is that the air capacity that time per unit attracted in the sintered layer 22 increases under certain condition, and the amount of sintering master emission gases 26 increases.In addition, by the use of reduction ore 19, the heating mode in the sintered layer 22 as shown in Figure 2, heat-up rate becomes large and speed of cooling becomes large, so the sintering deadline shortens.As a result, the machine speed of sinter machine main body 5 is risen.Thereby, can improve the productivity of agglomerate.
If the reduction ratio of reduction ore surpasses 30%, the ore that then usually reduces more contains metallic iron.Reduction under with temperature high about than 800 ℃, made in the situation that the reduction ratio that contains more metallic iron surpasses 30% reducing iron ore, the metallic iron that generates in the reduction ore becomes the lower tight tissue of void content, the reduction ore to reoxidize speed slack-off, the heating curve in the sintered layer 22 broadens.
On the other hand, with temperature reduction low about than 800 ℃, made in the situation that the reduction ratio that contains more metallic iron surpasses 30% reducing iron ore, the metallic iron that generates in the reduction ore becomes the more tissue of pore, easily reoxidize, might will reduce ore be encased in the sinter machine main body 5 before reduction ore burning.
Namely, surpass 30% reduction ore if make reduction ratio with the temperature of reduction temperature than about 800 ℃ high, the situation that heating curve in the sintered layer 22 broadens in the manufacturing processed of agglomerate is then arranged, surpass 30% reduction ore if make reduction ratio with the temperature than about 800 ℃ low, then in the manufacturing processed of agglomerate, be encased in reduction ore burning before the sinter machine main body 5.Thereby the reduction ratio of reduction ore is preferably below 30%.In addition, as in record in the patent documentation 1 like that, in blast furnace, use above the reduction ore of 30% metallic iron by containing reduction ratio, can be reduced in the amount of coke of using in the blast furnace.Thereby, containing reduction ore that reduction ratio surpasses 30% metallic iron and compare with in the manufacturing processed of agglomerate, using, its usage economy is better in blast furnace.
The oxidisability of reducing gas 15 (OD:%) can be used the H in the reducing gas
2Concentration (H
2%:vol%), H
2O concentration (H
2O%:vol%), CO concentration (CO%:vol%) and CO
2Concentration (CO
2%:vol%) as follows definition.
OD＝(H
2O％+CO
2％)/(H
2％+H
2O％+CO％+CO
2％)×100
When the oxidisability OD of reducing gas 15 hangs down, the H in the reducing gas 15
2Concentration and CO concentration and larger, the reducing power of reducing gas 15 is larger.If the oxidisability OD of reducing gas 15 is lower than about 20%, then in reduction ore 19, more contain metallic iron.Thereby, to generate in large quantities metallic iron in order being suppressed in the reduction ore 19, to avoid the heating curve in the sintered layer 22 to broaden, avoid reduction ore 19 burnings before being encased in sinter machine main body 5, the oxidisability OD that preferably makes reducing gas 15 is more than about 20%, makes the quantitative change of the metallic iron that contains in reduction ore 19 few.
Because the oxidisability OD average out to 40～50% of blast furnace gas 12, so when reducing gas 15 is made in blast furnace gas 12 partial combustions, become higher than the oxidisability OD of blast furnace gas 12, the OD of reducing gas 15 can be not little than 20% left and right sides.In addition, make reducing gass 15, oxidisability OD is little and reducing power is good reducing gas by the ironmaking by-product gas higher than blast furnace gas 12 thermal values being mixed in the blast furnace gas 12, can making only to compare by blast furnace gas 12.As a result, the productivity of the reduction ore 19 in the fluidised bed reduction furnace 1 is risen.But, being no more than 30%, can not generating more metallic iron in order to make reduction ratio, the oxidisability OD that preferably makes reducing gas 15 is more than about 20%.On the other hand, if the oxidisability OD of reducing gas 15 is higher than about 70%, carrying out of then reducing is slack-off, and the productivity of the reduction ratio step-down of reduction ore or reduction ore descends.Thereby the oxidisability OD that preferably makes reducing gas 15 is below 70%.
Then, the manufacturing of the actual agglomerate that carries out of present inventor described.Here, to not within the scope of the invention comparative example and the embodiment that follows above-mentioned embodiment describe.In an embodiment, details is narrated in the back, and the part that will contain the iron ore powder of crystal water is carried out prereduction, and the crystal water in the iron ore powder is removed, and the rhombohedral iron ore in the iron ore powder is mainly reverted to magnetite or wustite, use this pre-reduction of ore powder to produce agglomerate.In any one of comparative example and embodiment, all use by the iron ore powder that contains crystal water, assorted source of iron, auxiliary material, return mine and material that coagulated material consists of as cooperating raw material.In addition, as the iron ore powder that contains crystal water, in any one of comparative example and embodiment, all use a kind of river iron ore powder of spreading out as the peastone ore.Spread out the river iron ore powder and account for the 16mass% that cooperates raw material.In addition, as the index of the being reduced property that represents agglomerate, measured reduction ratio by JISM8713.
(comparative example)
In comparative example, iron ore powder is not carried out the such reduction of the present invention, the iron ore powder former state is used in sintering process as raw materials for sintering.The cooperation raw material that uses in order to make 1 ton of finished product agglomerate is 1477kg.The per 1 ton of finished product agglomerate of coagulated material uses 60.2kg.Wherein, anthracitic usage quantity is per 1 ton of finished product agglomerate 18.4kg.
Reduction ratio is 65%, and the productivity of agglomerate is time per unit and per unit sintering area 1.50t/h/m
2
When producing molten iron with blast furnace, the main raw material that per 1 ton of molten iron uses 1620kg to be made of agglomerate, iron ore stone and nodulizing, agglomerate is 1245kg wherein.At this moment, per 1 ton of molten iron is produced 1402kg finished product agglomerate in advance, its residual quantity be before the packing into of blast furnace by the sintering breeze under the sieve that screens out, it is re-used as raw materials for sintering.
In order to produce 4,000,000 tons of molten iron in blast furnace middle age, year produce 5,610,000 tons of finished product agglomerate, year use 10.3 ten thousand tons of hard coals, year use 107.8 ten thousand tons to spread out the river iron ore powder.At this moment, the total of in blast furnace, using the usage quantity of reducing material of coke and coal dust be per 1 ton of molten iron 490kg.
(embodiment)
The summary of expression embodiment in Fig. 3.In an embodiment, use the circular flow that is consisted of by the 1st fluidised bed reduction furnace 42 and the 2nd fluidised bed reduction furnace 41 as the fluidised bed reduction furnace.If superficial velocity is 7m/s.
To spread out river iron ore powder 51 in the 1st fluidised bed reduction furnace 42 becomes reduced ore stone 1 (52) 900 ℃ of lower reduction, and the ore 1 (52) that will reduce in the 2nd fluidised bed reduction furnace 41 becomes reduced ore stone 2 (53) 900 ℃ of lower reduction.
The blast furnace gas 54 that boosts is become the blast furnace gas 55 that boosts after the preheating by heat exchanger 44 preheatings, in partial combustion burner 45, use the air 56 that boosts to make its partial combustion and produce reducing gas 57, supply in the 2nd fluidised bed reduction furnace 41.In above-mentioned heat exchanger 44, blast furnace gas 54 preheatings of will boosting of the burning Exhaust Gas 62 after using Exhaust Gas 60 usefulness burners 43 with the 1st fluidised bed reduction furnace 42 to burn by the air 61 that boosts.
The crystal water of spreading out river iron ore powder 51 that supplies in the 1st fluidised bed reduction furnace 42 is 8mass% under dried state.This value is the state that is not present in the moisture (being called attached water) in the interparticle space of surface, iron ore of iron ore particle, the pore in the iron ore particle etc. by precipitation, aproll etc., and actual attached water is 4mass%.In an embodiment, when the quality 1042kg that spreads out river iron ore powder 51 that will contain attached water 4% reduces, use 1244Nm in circular flow
3Temperature is that 975 ℃, oxidisability OD are 56% reducing gas 57.This 1244Nm
3Reducing gas 57 be with the blast furnace gas (1140Nm that boosts
3) 54 by heat exchanger 44 be preheating to 711 ℃, then partial combustion is made in partial combustion burner.
In the 2nd fluidised bed reduction furnace 41, making the 864kg reduction ratio by this reducing gas 57 reduction reduction ores 1 (52) is 22% reduction ore 2 (53).
In the 1st fluidised bed reduction furnace 42, import the Exhaust Gas 58 of the 2nd fluidised bed reduction furnace 41 and use as reducing gas, will spread out river iron ore powder 51 and produce reduction ore 1 (52) 900 ℃ of lower reduction.For the reduction temperature in the 1st fluidised bed reduction furnace 42 is remained 900 ℃, the air 59 that will boost imports 344Nm
3In the 1st fluidised bed reduction furnace 42, make its partial combustion.
The Exhaust Gas 60 of the 1st fluidised bed reduction furnace 42 comprises crystal water and the attached water of spreading out river iron ore powder 51, is 1667Nm
3The Exhaust Gas 60 of the 1st fluidised bed reduction furnace 42 comprises the unburned gas composition, so pass through 6184Nm as described above in burner 43
3The air that boosts make its perfect combustion, be warmed up to after 989 ℃, blast furnace gas 54 preheatings of will boosting in heat exchanger 44 are discharged as heat exchanger Exhaust Gas 63 from heat exchanger 44.About heat exchanger Exhaust Gas 63, carry out vapor recovery and become waste heat recovery unit Exhaust Gas 64 with waste heat recovery unit 46, follow processing in cooling and dedusting device 47 and become cooling and dedusting device Exhaust Gas 65, and then carry out power recovery by in pressure recovery device 48, pressure being transformed to electric power, become Exhaust Gas 66 after the pressure recovery, Exhaust Gas after the pressure recovery 66 is processed outside system.
Reduction ore 2 (53) and iron ore, mix source of iron, auxiliary material, return mine and coagulated material 81 mixes as cooperating raw material 82 will cooperate raw material 82 to be encased in and forms sintered layer 83 in the sinter machine main body 71.The agglomerate 84 that to discharge from sinter machine main body 71 is broken and with sieves 73 screenings, is respectively tiny under the finished product agglomerate 85 of the particle diameter that is suitable as blast furnace raw material on the sieve and the sieve and returns mine 86.Attract gas blower 72 to attract sintering master Exhaust Gas 87 usefulness sintering master Exhaust Gas, then carry out dedusting, desulfurization, out of stock etc. Exhaust Gas is processed.
In an embodiment, same with comparative example, spread out the river iron ore powder and account for the 16mass% that cooperates raw material.But, in an embodiment, this is spreaded out the river iron ore powder reduce as described above, the reduced ore masonry that obtains is like this cooperated for a part that cooperates raw material.As a result, can not use hard coal, only use the coagulated material of 41.8kg to make agglomerate.That is, the usage quantity of the coagulated material of per 1 ton of finished product agglomerate is 41.8kg.The usage quantity of this coagulated material is corresponding to the amount after the coagulated material usage quantity of comparative example has been removed anthracitic usage quantity.
At this moment, the reduction ratio that the JISM8713 of being reduced property by the expression agglomerate measures is 68%, compares with this reduction ratio 65% of comparative example and has risen 3 percentage points.That is, can improve the being reduced property of agglomerate.In addition, the productivity of agglomerate is time per unit and per unit sintering area 1.58t/h/m
2, with this productivity 1.50t/h/m of comparative example
2Compare the 0.08t/h/m that risen
2That is, can improve productivity.
With 113.2 ten thousand tons spread out the as described above prereduction of river iron ore powder, by the reduced ore masonry after the prereduction is made agglomerate for a part that cooperates raw material, can year produce 5,890,000 tons of being reduced property and improve 3 percentage points finished product agglomerate.
The result, in order to produce 4,000,000 tons of molten iron with blast furnace year, per 1 ton of molten iron can use the 1307kg agglomerate, compares the usage quantity that can increase agglomerate and reduces the relatively poor iron ore stone of being reduced property with the usage quantity 1245kg of the agglomerate of per 1 ton of molten iron of comparative example.
The improvement of the being reduced property by agglomerate and the rising of agglomerate usage ratio, the total of in blast furnace, using the usage quantity of reducing material of coke and micro mist carbon be per 1 ton of molten iron 482kg, compare with per 1 ton of molten iron 490kg of the reducing material usage quantity of comparative example, the reducing material usage quantity can be reduced per 1 ton of molten iron 8kg.
In comparative example, per 1 ton of finished product agglomerate uses coagulated material 60.2kg, year 5610000 tons of finished product agglomerate of production, year 33.8 ten thousand tons of coagulated materials of use.On the other hand, in an embodiment, per 1 ton of finished product agglomerate uses coagulated material 41.8kg, year 5890000 tons of finished product agglomerate of production, year 24.6 ten thousand tons of coagulated materials of use.Thereby, with respect to comparative example, in an embodiment, the usage quantity year of coagulated material has been cut down 9.2 ten thousand tons.
In comparative example, per 1 ton of molten iron uses the 490kg reducing material, and year 4000000 tons of molten iron of production are so used 1,960,000 tons of reducing materials in year.On the other hand, in an embodiment, per 1 ton of molten iron uses the 482kg reducing material, and year 4000000 tons of molten iron of production are so used 192.8 ten thousand tons of reducing materials in year.Thereby, with respect to comparative example, in an embodiment, the usage quantity year of reducing material has been cut down 3.2 ten thousand tons.
In an embodiment, with respect to comparative example, will be as CO
2The total year of the coagulated material in generation source and the usage quantity of reducing material has been cut down 12.4 ten thousand tons, correspondingly can cut down CO
2Generation.
Industrial applicibility
According to the present invention, can reduce the coagulated material ratio and productivity and the being reduced property of raising agglomerate.In the manufacturing processed of agglomerate, by cutting down the coagulated material ratio, can cut down costliness and the unsettled anthracitic usage quantity of supply is arranged.And then, can increase the turnout of the good agglomerate of being reduced property, so in blast furnace process, can reduce reducing material ratio, the coke that reduces costliness and the usage quantity of coal dust.In addition, by the reduction of the ratio of the coagulated material in the sintering process and the reduction of the ratio of the reducing material in the blast furnace process, can suppress the CO of whole iron manufacturing process
2Generation is conducive to prevent global warming.
Claims (10)
1. the manufacture method of an agglomerate is characterized in that, the iron ore that will contain crystal water uses the reducing gas reduction behind the blast furnace gas partial oxidation, and the reduction ore that obtains is used for raw materials for sintering, makes agglomerate.
2. the manufacture method of agglomerate as claimed in claim 1 is characterized in that, the above-mentioned iron ore that contains crystal water be peastone ore or Ma Lamanba ore at least any.
3. the manufacture method of agglomerate as claimed in claim 1 or 2 is characterized in that, uses fluidised bed to carry out above-mentioned reduction.
4. the manufacture method of agglomerate as claimed in claim 1 or 2, it is characterized in that, the blast furnace gas of above-mentioned partial oxidation is being added more than one that select in advance from coal gas of converter, coke-oven gas, Sweet natural gas, liquefied petroleum gas (LPG), other gases higher than blast furnace gas thermal value.
5. the manufacture method of agglomerate as claimed in claim 3, it is characterized in that, the blast furnace gas of above-mentioned partial oxidation is being added more than one that select in advance from coal gas of converter, coke-oven gas, Sweet natural gas, liquefied petroleum gas (LPG), other gases higher than blast furnace gas thermal value.
6. the manufacture method of an agglomerate is characterized in that, has:
The operation that reducing gas behind the use blast furnace gas partial oxidation reduces to the iron ore that contains crystal water;
The operation of the reduction ore sintering that will obtain by above-mentioned reduction.
7. the manufacture method of agglomerate as claimed in claim 6 is characterized in that, the above-mentioned iron ore that contains crystal water is at least a of peastone ore or Ma Lamanba ore.
8. such as the manufacture method of claim 6 or 7 described agglomerate, it is characterized in that, use fluidised bed to carry out above-mentioned reduction.
9. such as the manufacture method of claim 6 or 7 described agglomerate, it is characterized in that, the blast furnace gas of above-mentioned partial oxidation is being added more than one that select in advance from coal gas of converter, coke-oven gas, Sweet natural gas, liquefied petroleum gas (LPG), other gases higher than blast furnace gas thermal value.
10. the manufacture method of agglomerate as claimed in claim 8, it is characterized in that, the blast furnace gas of above-mentioned partial oxidation is being added more than one that select in advance from coal gas of converter, coke-oven gas, Sweet natural gas, liquefied petroleum gas (LPG), other gases higher than blast furnace gas thermal value.
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| JP2008102550A JP4384698B2 (en) | 2008-04-10 | 2008-04-10 | Method for producing sintered ore |
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| PCT/JP2009/056620 WO2009125693A1 (en) | 2008-04-10 | 2009-03-31 | Production of sintered ore |
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| KR (1) | KR101284532B1 (en) |
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| CN102213659A (en) * | 2011-04-12 | 2011-10-12 | 河北钢铁股份有限公司邯郸分公司 | Method for researching sintering performance of iron ore by utilizing mini-sintering test |
| JP5892317B2 (en) * | 2011-12-27 | 2016-03-23 | Ｊｆｅスチール株式会社 | Production method of raw materials for blast furnace |
| JP5892318B2 (en) * | 2011-12-27 | 2016-03-23 | Ｊｆｅスチール株式会社 | Agglomerate production method |
| KR101590994B1 (en) * | 2014-09-12 | 2016-02-19 | 주식회사 포스코 | Method for manufacturing sintered ore and apparatus for the same |
| CN104726692A (en) * | 2015-04-03 | 2015-06-24 | 甘肃酒钢集团宏兴钢铁股份有限公司 | Method for improving reduction temperature of iron ore in shaft furnace magnetizing roasting |
| CN104988305B (en) * | 2015-07-14 | 2017-03-01 | 江苏永钢集团有限公司 | The production technology of acid sinter ore |
| CN106048212B (en) * | 2016-06-07 | 2017-11-28 | 东南大学 | One kind classification reduction burning produces sintering deposit and separates CO2Device and method |
| CN106048214B (en) * | 2016-06-07 | 2017-11-28 | 东南大学 | A kind of synthesis gas reduction burning produces sintering deposit and separates CO2Devices and methods therefor |
| CN106011460B (en) * | 2016-07-15 | 2018-03-06 | 攀钢集团攀枝花钢铁研究院有限公司 | A kind of method that sintering deposit is prepared using iron concentrate containing high sulphur |
| CN106636508B (en) * | 2016-10-30 | 2018-06-19 | 华北理工大学 | A kind of efficient circulation utilizes the iron-smelting process of top gas |
| KR101977358B1 (en) * | 2017-08-28 | 2019-05-10 | 주식회사 포스코 | Method and apparatus for manufacturing sintered ore |
| CN113025771B (en) * | 2021-03-05 | 2022-05-17 | 山东大学 | Grate type direct reduced iron production system and method for sintering machine |
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| US6402808B1 (en) * | 1998-07-24 | 2002-06-11 | Technological Resources Pty. Ltd. | Direct smelting process |
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| JPS589126B2 (en) * | 1981-02-28 | 1983-02-19 | 住友金属工業株式会社 | Method for reducing nitrogen oxides in sintering machine exhaust gas |
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| JP2001271121A (en) | 2000-03-28 | 2001-10-02 | Nkk Corp | Method for producing sintered ore for blast furnace |
| JP5020501B2 (en) * | 2005-11-17 | 2012-09-05 | 新日本製鐵株式会社 | Pretreatment method of sintered raw material and method of manufacturing sintered ore |
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| GB1247417A (en) * | 1969-05-22 | 1971-09-22 | Armco Steel Corp | Method of blast furnace reduction of iron ores |
| US6402808B1 (en) * | 1998-07-24 | 2002-06-11 | Technological Resources Pty. Ltd. | Direct smelting process |
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| BRPI0911318A2 (en) | 2015-09-29 |
| KR101284532B1 (en) | 2013-07-16 |
| BRPI0911318B1 (en) | 2018-03-06 |
| JP2009249725A (en) | 2009-10-29 |
| KR20100129793A (en) | 2010-12-09 |
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