CN204803377U - Flue gas recirculation formula prereduction sintering device - Google Patents
Flue gas recirculation formula prereduction sintering device Download PDFInfo
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- CN204803377U CN204803377U CN201520390447.4U CN201520390447U CN204803377U CN 204803377 U CN204803377 U CN 204803377U CN 201520390447 U CN201520390447 U CN 201520390447U CN 204803377 U CN204803377 U CN 204803377U
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Abstract
The utility model provides a flue gas recirculation formula prereduction sintering device, the device includes: sintering machine (4), be located ignition furnace (1) of the front end of sintering machine (4), be located sealed cowling (2) of the sintering pallet top of sintering machine (4), flue gas recirculation main line (L1), the opium way pipeline (L2) that leads to exhaust stacks, oxygen boosting air piping (L3), a mixing chamber (3) for mixing circulation flue gas of carrying via flue gas recirculation main line (L1) and the oxygen -enriched air of carrying via air piping (L3), pot -type cooler (7) with, sintering deposit, and set up first dust remover (8) and draught fan (9) on flue gas recirculation main line (L1), with, set up second dust remover (10), main air exhauster (11) on pipeline (L2) is said to opium, desulfurizing tower or desulphurization unit (12) and phosphorus collector (13), wherein sintering machine (4) have a 20 -34 bellows.
Description
Technical field
The utility model relates to a kind of smoke gas circulating type prereduction agglomerating plant of iron ore.
Background technology
Current China is based on blast furnace iron-making process, and agglomerate accounts for 70% ~ 90% of feed stock for blast furnace, and sintering plant revamp accounts for 10% ~ 15% of ironmaking energy consumption, there is the problems such as energy consumption is high, pollution is large, utilization rate of waste heat is low.Conventional sintering technical process as shown in Figure 1, traditional iron ore sintering process mainly using coke powder and hard coal as fuel for sintering process provides heat, adopt the mode of down draft sintering, producing with calcium ferrite is the high basicity sinter of Binder Phase.
Chinese patent CN101343689B, CN101608256B, CN101921909B, CN102127636B, CN102676797B and the open CN103911507A of Chinese patent disclose the preparation method of agglomerate.
In addition, CN1940092A and CN100532579C discloses the preparation of pre-reduced pellet.
Domestic at present in order to increase yield with realize energy-saving and emission-reduction, have employed sinter fume internal-circulation type sintering scheme at sintering plants such as peaceful steel and Sha Gang, internal recycle technique is temperature is higher by newly-increased vacuum fan, O
2content is higher, SO
2the direct suction of bellows flue gas that content is lower is newly established pipeline and is not entered original flue, again after multi-tube dusting or supplementary fresh air or mix in a mixer with ring SAPMAC method flue gas, and enter in the hood of pallet face, again participate in sintering process by the bed of material.Corresponding is a kind of sinter fume outer circulation type sintering scheme with it, and external circulation process is on conventional sintering process basis, by O
2content is higher, SO
2the flue gas of a certain flue that content is lower is drawn by recirculation blower after main exhauster, again after gravitational dust collection or cyclone dust removal with supplement fresh oxygen-rich air or mix in a mixer with central cooler waste gas, and enter in the hood of pallet face, again participate in sintering process by the bed of material.These two kinds of sinter fume recycle modes can realize energy-saving and emission-reduction to a certain extent, but flue gas recirculation rate is low, reason is as follows: experimental study and production practice prove, in order to ensure the yield and quality index request of agglomerate, oxygen content in sintering air can not lower than 16% ~ 18%, and the oxygen content in sinter fume is only about 13%, so when carrying out flue gas recirculation, if not with addition of oxygen-rich air or pure oxygen, flue gas recirculation rate is lower than less than 35%, even if adopt oxygen enrichment or pure oxygen, also about 50% can only be circulated.) current production application display energy-saving effect not obvious, Technology need further perfect, therefore also do not obtain large-scale promotion application.
Refer to the concept of prereduction in prior art, but be only localized design or imagination.At present as a kind of new technology of not yet industrial applications, also containing metallic iron and ferric oxide in the agglomerate that prereduction sintering process is produced, for having the effect of reduced iron in blast furnace.
The defects such as at present, energy-saving and emission-reduction and environment protection are had higher requirement to SINTERING PRODUCTION, and it is high that existing SINTERING PRODUCTION technology has energy consumption, and smoke discharge amount is large, and desulphurization cost is high.In order to adapt to the needs of SINTERING PRODUCTION, adopting flue gas recirculation sintering technology, from watershed management, on the one hand, the sensible heat in flue gas and latent heat can be utilized; On the other hand, the quantity discharged of flue gas can be reduced, reduce desulphurization cost.
The contradiction of the shortage of coke and blast fumance STRENGTH ON COKE demand (skeleton of coke as the bed of material and the reductive agent of direct reduction reactor) constrains the development of long flow process iron-smelting process, and large blast furnace production is had higher requirement to raw material ventilation property.In order to strengthen the vitality of long flow process iron-smelting process, adopt prereduction sintering technology, part reduction deoxidation process is completed in sintering, not only can reduce the consumption of coke, and prereduced sinter porosity is high, improve the ventilation property of the bed of material, contribute to the raising of large blast furnace productivity.
In addition, phosphorus is as one of main harmful element in steel smelting procedure, must remove, but at present process for producing steel and iron can only in ore dressing and steelmaking process dephosphorization, this is the major cause of the high-phosphorus iron ore utilization of resources difficulty of rich reserves, if can in sintering process direct dephosphorization, reduce the impact of phosphorus on subsequent handling equipment and quality product, will the exploitation of high-phosphorus iron ore resource be contributed to.
For above defect, this patent, based on prior art, sinters two kinds of technology by fusion flue gas recirculation sintering and prereduction, have developed a kind of smoke gas circulating type prereduction sintering process and device, can solve the above-mentioned technical barrier faced to a certain extent.
Utility model content
Pre existing reduction sintering technology is still in concept and phase of basic research, and do not have a set of specific embodiment, the flue gas after prereduction contains higher CO, and brings difficulty to follow-up fume treatment; And the cycling rate of existing flue gas recirculation sintering technology not only flue gas is low, effects of energy saving and emission reduction is also very limited, and economic benefit is not remarkable; In addition, existing traditional sintering techniques completes sintering process under a kind of oxidizing atmosphere, can not realize the direct dephosphorization of high-phosphorus iron ore.
For the shortcoming that above-mentioned existing sintering technology exists, the utility model proposes a kind of smoke gas circulating type prereduction sintering process, join carbon in can also utilizing while being intended to produce prereduced sinter and restore phosphorus in high-phosphorus iron ore.In the Direct Reduction of prior art, kakoxene is reduced into gas P
2, after touching metallic iron, generate Fe again
2p, therefore do not have in the prior art described in the utility model in join the effect of carbon dephosphorization.And in technology of the present utility model, inside joining carbon bead can be high-phosphorus iron ore carbon-burdened pellet, the phosphorus in bead is reduced into gas P
2after, be diffused into pelletizing outside in time, what contact with it is agglomerate (not having metallic iron) and weak oxide atmosphere (oxygen content is lower, generally below 10%), because this ensure that removing of phosphorus.In addition, the utility model adopts the mode of flue gas recirculation sintering, realizes enrichment and the recycling of phosphor resource, and sensible heat in efficiency utilization flue gas and latent heat, reaches the object of resources effective utilization and energy-saving and emission-reduction.
Designer of the present utility model shows through Theoretical Calculation and results of laboratory, and prereduced sinter is when reduction degree reaches 40% ~ 60%, and blast furnace fuel ratio can be down to below 450kg/t, and ironmaking cost will significantly reduce, simultaneously CO
2reducing discharging will more than 10%.
Because the flue gas after prereduction contains higher CO, its way of solution of the present utility model is exactly flue gas recirculation sintering, can also utilize the CO latent heat in flue gas, reduces energy consumption, avoids the impact on follow-up fume treatment.In addition, the utility model can adopt most flue gas to carry out recycle, because this technique is in order to ensure reducing atmosphere inside the outside weak oxide of material and pelletizing, require lower to the oxygen content of sintering gas, what adopt is little air quantity and lower negative pressure sintering processing, and also reduces the requirement of strength of prereduced sinter, because the consolidation mechanism of prereduced sinter, the liquid bonding phase of the mainly liquid phase of ferric metasilicate and Calucium Silicate powder, and part calcium ferrite; And the liquid bonding phase of conventional sintering mainly calcium ferrite, in essence also can not the prereduced sinter of production high strength.And blast fumance is also lower to the requirement of strength of prereduced sinter, when adopting prereduced sinter as blast furnace burden, solve the problem of upper blast furnace low temperature reduction degradation, loss of strength greatly reduces, prereduced sinter has flourishing porosity simultaneously, thus ensure that the ventilation property of the bed of material, this is also the basic reason that when adopting prereduced sinter, BF Productivity improves.
According to embodiment of the present utility model, provide a kind of iron ore prereduction sintering method, the method comprises:
1) by iron ore powder (such as fine iron breeze, as common iron ore or high-phosphorus iron ore) and coal fuel (such as coke powder or coal dust) mixing after pelletizing (such as disk pelletizing or pressure ball) and join the pelletizing of carbon in obtaining, wherein: the weight ratio in coal and ore deposit is the scope at 0.08 ~ 0.35:1 (wt), preferably 0.1 ~ 0.3:1 (wt), more preferably 0.15 ~ 0.2:1 (wt), pelletizing mean diameter is at 3 ~ 15mm, preferably 4 ~ 11mm, more preferably 5 ~ 8mm;
2) prepare burden with iron ore powder, flux and coal fuel powder, wherein the amount ratio of iron ore powder, flux and coal fuel is 75-85:10-15:3-6; Then, in primary mixer, add water (such as based on the 5-9wt% of solid materials gross weight, as 7wt%) carry out mixing to obtain sinter mixture,
3) by step 1) in obtain in join pelletizing, the step 2 of carbon) in the sinter mixture that obtains and additional coal fuel fine powder mix in second drum mixer, obtain prereduction sinter mixture, wherein: the amount ratio (by wt) of sinter mixture, carbon-burdened pellet and additional coal fuel fine powder is 50-70:28-48:1-5, preferred 53-65:34-46:1.2-3; More preferably 55-62:36-43:1.5-2.5; With
4) pallet prereduction sinter mixture being arranged into sinter machine carries out prereduction sintering (preferably, carry out smoke gas circulating type prereduction sintering, more preferably sinter under lower negative pressure, little air quantity).Here lower negative pressure refer to be equivalent to normal sintering negative pressure (such as-14 to-17.2KPa) 70% ~ 90% negative pressure (such as-11KPa is to-15KPa, as-11.2 to-14.4KPa).Little air quantity described here refer to be equivalent to conventional air quantity 80% ~ 90% air quantity (such as 72m
3/ (m
2.min) to 81m
3/ (m
2.min)).
Preferably, the bottom of sinter machine has such as 20-34, preferably 22-32, more preferably 24-28 bellows.
Preferably, aforesaid method also comprises:
5) agglomerate after prereduction sintering (namely under the condition of hypoxemia (as 0.1-3vol%) or anaerobic) under the condition of anoxybiotic cools.Preferably, in pot type water cooler, rare gas element (as nitrogen) is adopted to cool.
In step 1) in, in general, in the process preparing pelletizing, adopt the water (such as based on the 5-9wt% of solid materials gross weight, as 7wt%) of wetting amount.
In step 2) in, in general, coal fuel is the mixing of both coke powder or coke powder and coal dust, and the weight ratio of coal fuel and iron ore powder is 3 ~ 10: 75 ~ 85, preferably 4 ~ 6: 75 ~ 85.
Generally, step 4) in smoke gas circulating type prereduction sintering refer to: from several bellows (the such as the 3rd to the 12nd bellows of sinter machine head or front end, as 3-10 bellows) and from the flue gas of several bellows (the such as the reciprocal 1st to the 8th bellows reciprocal) of sinter machine afterbody (or rear end) as circulating flue gas, circulating flue gas after simple gravitational dust collection or utilize the first fly-ash separator (8) carry out dedusting after (such as utilize cyclone dust collector (8) carry out cyclone dust removal after) mix with oxygen-rich air (5) and form mixing air, return sinter machine afterwards for sintering.
Generally, in step 2) in primary mixer with addition of coal fuel quantity (wt) account for step 2) in coal fuel powder and step 3) in the 75-90wt% of consumption (wt) sum of additional coal fuel fine powder, preferred 78-85wt%.This additional coal fuel fine powder is for improving the incendivity of fuel.In addition, those skilled in the art are based on heat balance principle and best water distribution with join carbon and test and can determine that this joins carbon ratio.
In addition, in step 2) and step 3) in join carbon ratio, the coal fuel later stage adds ratio and determines by further commerical test, such as, consider the factors such as granulating process, bed permeability, bed depth.Such as, sinter mixture granularity is thicker, and bed permeability is better, and bed depth is thicker, and it is then higher that the coal fuel later stage adds ratio, otherwise lower.
Step 2) in the consumption of iron ore powder be then requirement based on prereduction pellet intensity, because main intensity relies on the outer liquid bonding phase wrapped up in sinter mixture and produce, with the requirement of prereduced sinter reduction degree, general requirement reduction degree is advisable 40% ~ 60%, and this mainly comes from the reduction of carbon-burdened pellet.
Generally, in step 3) in the coal fuel fine powder that uses require that the grade of particle of more than 90% is less than 1mm, be preferably less than 0.6mm, be more preferably less than 0.4mm.
Generally, for the preparation of step 1) in the iron ore material of iron ore powder be the raw material of various ironmaking conventional in prior art, such as, it is selected from: iron ore concentrate, such as common magnetite concentrate or high phosphorus iron ore concentrate.
In this application, flux is one or more (such as two or three) of being selected from Wingdale, rhombspar, unslaked lime, serpentine.Generally, control CaO and SiO in agglomerate preparation process
2weight ratio be 1.0 ~ 2.5:1.
In step 4) sintering step in, after the ignition furnace (1) of sinter machine (4) to sinter machine hood, adopt seal closure (2) all to cover, and keep being tiny structure (such as-50-5Pa) in seal closure.Sinter machine has such as 20-32 (preferred 24-28) bellows (being positioned at the bottom of sinter machine) usually, wherein from several bellows (the such as the 3rd to the 12nd bellows, as the 3rd to the 10th bellows) of sinter machine head (or front end) and from the flue gas of several bellows (the such as the reciprocal 1st to the 8th bellows reciprocal) of sinter machine afterbody (or rear end) as circulating flue gas.Circulating flue gas mixes with oxygen-rich air (5) and forms mixing air after dedusting, is transfused to afterwards in seal closure (2) for sintering.That is, circulating flue gas mixes with oxygen-rich air (5) and forms mixing air after dedusting, is transfused in seal closure (2).The flue gas of bellows and igniting section bellows (the such as the 1st and the 2nd bellows) in the middle part of sinter machine enters in the second fly-ash separator (10) and thionizer (12) and processes under main exhauster (11) effect, and the flue gas after process is discharged.Preferably, especially when the raw material adopted is high-phosphorus iron ore, need to increase a phosphorus collector (13) after carrying out flue gas desulfurization.This phosphorus collector (13) is airtight water cycle cooling tank, and wherein water coolant flows through the pipeline of its inside.When flue gas flows through collector (13) and water coolant carry out indirect heat exchange, make phosphorus steam meet cold one-tenth solid-state phosphorus, and stockpile bottom cooling tank, to realize the recycling to high-phosphorus iron ore phosphor resource.Phosphorus collector (13) is for recycling the phosphorus simple substance be embedded in flue gas.Preferably, the second fly-ash separator (10) is electric precipitator or electricity+cloth bag complex dust collector.
In step 5) in, preferably, rare gas element such as nitrogen is adopted to cool in agglomerate pot type water cooler (7) after prereduction, in order that prevent the secondary oxidation of prereduced sinter, cooled high-temp waste gas is used for cogeneration use, and the exhaust gas recirculation after cogeneration is used for the cooling of agglomerate.In order to avoid cooled prereduced sinter reoxidizes problem in transportation, preferably, in the exit of pot type water cooler (7) to prereduced sinter spraying or spray the calcium chloride solution of a certain amount of (such as based on the 0.5-6wt% of agglomerate dry weight) or aqua calcis (such as with the aqueous solution form of 0.5-5wt% concentration, preferably 1-4wt% concentration, more preferably 2-3wt% concentration).Spray the object of calcium chloride: thin film can be formed on the surface of prereduced sinter, prevent prereduced sinter to be again oxidized in transportation, the low temperature reduction degradation index of agglomerate at upper blast furnace can also be reduced.Spray the object of calcium hydroxide: at surface coverage one deck white lime of prereduced sinter, can compare calcium chloride film, protective layer is more stable, fine and close, prevents prereduced sinter to be again oxidized in transportation.
After cloth, bed thickness is 500 ~ 1000mm, preferred 750-900mm.
Conventional sintering process is 2.5 ~ 4.5m/min at sintering pallet machine speed, and vertical sintering speed is 20 ~ 40mm/min, and mixture temperature is 35 ~ 80 DEG C, and sintering negative pressure is-14KPa ~-17.2KPa, and sintering air quantity is 90 ± 5m
3/ (m
2.min), spent air temperture is carry out sintering under 100 ~ 150 DEG C of conditions.
According to another embodiment of the present utility model, be provided for the device in aforesaid method or a kind of iron ore prereduction agglomerating plant, this device comprises: sinter machine (4); Be positioned at the ignition furnace (1) of the front end of sinter machine (4); Seal closure (2) above the pallet being positioned at sinter machine (4); Flue gas recirculation main line (L1); Towards the large flue pipeline (L2) of blowdown stack; Oxygen-rich air pipeline (L3); The circulating flue gas carried via flue gas recirculation main line (L1) for mixing and the mixing chamber (3) of oxygen-rich air carried via airline (L3); With, the pot type water cooler (7) of agglomerate.
Preferably, said apparatus comprises further: be arranged at the first fly-ash separator (8) on flue gas recirculation main line (L1) and induced draft fan (9); With, be arranged at the second fly-ash separator (10) on large flue pipeline (L2), main exhauster (11), thionizer or desulfurizer (12) and phosphorus collector (13).Preferably, the first fly-ash separator (8) is tornado dust collector and the second fly-ash separator (10) is electric precipitator or electricity+cloth bag complex dust collector.
In this application, preferably, sinter machine (4) has 20-32, preferably 22-30, more preferably 24-28 bellows (being positioned at the bottom of sinter machine).Several bellows (the such as the 3rd to the 12nd bellows, as the 3rd to the 10th bellows) of sinter machine head or front end and several bellows (the such as the reciprocal 1st to the 8th bellows reciprocal) the respective flue gas of sinter machine afterbody or rear end export arm and are connected to flue gas recirculation main line (L1).
Preferably, the middle part bellows (such as the 11st or the 13rd bellows) of sinter machine (4) and igniting section bellows (the such as the 1st and the 2nd bellows) respective flue gas export branch road and are connected to large flue pipeline (L2).
In this application, the technical process of not explaining and operating duty traditionally sintering method are carried out.
In this application, " optionally " expression is carried out or is not carried out." optional " expression is with or without.
The sinter machine used in the application is sinter machine conventional in prior art.
Compared to prior art, Advantageous Effects of the present utility model:
1, Integrated Development a kind of smoke gas circulating type prereduction sintering process (technique basic procedure as shown in Figure 2), this technique realizes the recycle of sinter fume while obtaining prereduced sinter, reach the object of energy-saving and emission-reduction, can also high-phosphorus iron ore be processed, complete the direct dephosphorization of high-phosphorus iron ore.
2, by conventional sintering compound, carbon-burdened pellet and need the later stage to add levigate after fuel add in second drum mixer, to ensure that prereduction sinter mixture has good ventilation property, improving the incendivity of carbon-burdened pellet outer fuel, is the important leverage obtaining high strength, high reduction degree prereduced sinter.
3, on the basis of conventional sintering, carry out the little air quantity sintering of lower negative pressure, sintering wind, mainly from circulating flue gas and oxygen-rich air, controls the utilization coefficient of agglomerate at 0.8 ~ 1.0t/ (m
2.h) left and right.Bed thickness can be improved further on the height of the conventional sintering bed of material, realize super deep-bed sintering, need the basicity reducing agglomerate, improve the ratio of silicon-dioxide, such as increase a certain proportion of serpentine, to increase the liquid phase of agglomerate and to improve intensity and the metallurgical performance of prereduced sinter.
(conventional sintering, consolidation style mainly: Fe
2o
3+ CaO=CaOFe
2o
3(calcium ferrite)
4, in technology of the present utility model, consolidation style is: inside join the crystallization formation metallic iron crystal stock body that carbon bead is metallic iron, and generating portion low melting point peridotites phase; Then there is following reaction in outside agglomerate: SiO
2+ CaO=CaOSiO
2(Calucium Silicate powder); Fe
2o
3+ CaO=CaOFe
2o
3(calcium ferrite), a certain amount of liquid phase (compound of formation is all low melting component) is produced mainly through above-mentioned reaction, in cool down, utilize this part liquid phase to realize the bonding of agglomerate and pellet, to obtain the prereduced sinter of higher-strength.
5, in addition, super deep-bed sintering can be adopted, on the one hand, in order to give full play to the auto accumulation heat effect of the bed of material, fuel saving consumption; On the other hand, prereduction sinter mixture has good ventilation property, and this is the prerequisite realizing super deep-bed sintering).
Accompanying drawing explanation
Fig. 1 is the sintering process schema of prior art.
Fig. 2 is the utility model structure drawing of device.
Reference numeral: 1-ignition furnace, 2-seal closure, 3-mixing chamber, 4-sinter machine, 5-oxygen-rich air, the delivery conduit (waste heat recovery utilization) of 6-cooling draught, 7-pot type water cooler, 8-first fly-ash separator, 9-induced draft fan, 10-second fly-ash separator, 11-main exhauster, 12-desulfurizer, 13-phosphorus collector, 14-chimney; L1-flue gas recirculation main line, L2-large flue pipeline, L3-oxygen-rich air pipeline.
Fig. 3 is the schematic diagram of phosphorus collector 13.
1301-gas approach end, 1302-smoke outlet, 1303-entrance of cooling water end, 1304-cooling water outlet end, the outlet that 1305-is elemental phosphorous.
Embodiment
Adopt a kind of iron ore prereduction agglomerating plant in a specific embodiment, as shown in Figure 2, this device comprises: sinter machine 4; Be positioned at the ignition furnace 1 of the front end of sinter machine 4; Seal closure 2 above the pallet being positioned at sinter machine 4; Flue gas recirculation main line L1; Towards the large flue pipeline L2 of blowdown stack; Oxygen-rich air pipeline L3; For the mixing chamber 3 of the oxygen-rich air that mixes the circulating flue gas carried via flue gas recirculation main line L1 and carry via airline L3; With, the pot type water cooler 7 of agglomerate.
Preferably, said apparatus comprises further: be arranged at the fly-ash separator 8 on flue gas recirculation main line L1 and induced draft fan 9; With, be arranged at the fly-ash separator 10 on large flue pipeline L2, main exhauster 11, thionizer or desulfurizer 12 and phosphorus collector 13.As shown in Figure 3, phosphorus collector 13 comprises gas approach end 1301, smoke outlet 1302, entrance of cooling water end 1303, cooling water outlet end 1304, elemental phosphorous outlet 1305.
Preferably, sinter machine 4 has such as 20-34, preferably 22-32, more preferably 24-28 bellows (being positioned at the bottom of sinter machine).The flue gas of several bellows (the such as the 3rd to the 12nd bellows, as the 3rd to the 10th bellows) of sinter machine head or front end and several bellows (the such as the reciprocal 1st to the 8th bellows reciprocal) of sinter machine afterbody or rear end exports arm and is connected to flue gas recirculation main line L1.
Preferably, the middle part bellows (such as the 11st or the 13rd bellows) of sinter machine 4 and the flue gas of igniting section bellows (the such as the 1st and the 2nd bellows) export branch road and are connected to large flue pipeline L2.
Embodiment 1
A kind of iron ore smoke gas circulating type prereduction sintering method comprises the following steps:
1) carry out pelletizing by after iron ore powder (i.e. v-ti magnetite concentrate) and coke powder or coal blending by pressure ball or disk pelletizing mode, join the pelletizing of carbon in acquisition, wherein colliery is than being 0.18:1 (wt), and pelletizing mean diameter is 6mm;
2) use iron ore powder (i.e. common powdered iron ore can be fine ore, also can be the mixture of fine ore and concentrate), (it comprises the mixture of raw lime stone, Wingdale and serpentine three kinds of raw materials to flux; The amount ratio of these three kinds of raw materials makes control CaO and SiO in agglomerate preparation process
2weight ratio be about 1.2:1) and coke powder carry out preparing burden (obtaining butt material), wherein the amount ratio of iron ore powder, flux and char fuel is 83:12:5; Then, the water added in primary mixer based on the 7wt% of butt material gross weight carries out mixing to obtain sinter mixture,
3) by step 1) in obtain in join pelletizing, the step 2 of carbon) in the sinter mixture that obtains and additional coal fuel fine powder (grade of the particle of more than 90% is less than 0.4mm) mix in second drum mixer, obtain prereduction sinter mixture, wherein: the amount ratio (by wt) of sinter mixture, carbon-burdened pellet and additional coal fuel fine powder is 58:40:2;
4) as shown in Figure 2, pallet prereduction sinter mixture being arranged into sinter machine 4 (bottom of this sinter machine 4 has 24 bellows) carries out smoke gas circulating type prereduction sintering, and sinters under lower negative pressure, little air quantity.Here lower negative pressure refer to be equivalent to normal sintering negative pressure 80% negative pressure (such as-12.8KPa).Little air quantity described here refer to be equivalent to conventional air quantity 85% air quantity (76.5m
3/ (m
2.min)); With
5) agglomerate after prereduction sintering (namely under the condition of hypoxemia (as 0.1-3vol%) or anaerobic) under the condition of anoxybiotic, adopts nitrogen to cool in pot type water cooler 7.Spray a certain amount of calcium chloride or calcium hydroxide (such as with the solution form of 1-4wt% concentration) in the exit of water cooler to prereduced sinter, reduce reoxidizing of transportation prereduced sinter.
In addition, in step 1) in, in the process preparing pelletizing, adopt the water (namely based on the 7wt% of the butt material gross weight of step 1) of wetting amount.
Wherein, in step 4) in smoke gas circulating type prereduction sintering carry out as follows: the 3rd to the 10th bellows from sinter machine head or front end and the inverse the 1st from sinter machine afterbody or rear end to the flue gas of the 8th bellows reciprocal as circulating flue gas, the circulating flue gas carried via flue gas recirculation main line L1, forming mixing air by mixing with the oxygen-rich air 5 carried from oxygen-rich air pipeline L3 after the first fly-ash separator 8 (i.e. tornado dust collector) dedusting, returns sinter machine 4 afterwards for sintering.
After cloth on pallet, bed thickness is about 850mm.
In step 4) sintering step in, after the ignition furnace (1) of sinter machine (4) to sinter machine hood, adopt seal closure (2) all to cover, and keep being tiny structure (such as-50 to-5Pa) in seal closure.
Sintering process is 3.5 ~ 4.0m/min at sintering pallet machine speed, and vertical sintering speed is 30mm/min, and mixture temperature is 40 ~ 50 DEG C, and sintering negative pressure is-13KPa, and sintering air quantity is 72m
3/ (m
2.min), spent air temperture is carry out sintering under 120 DEG C of conditions.
In the middle part of sinter machine, the flue gas of bellows (namely the 11st to 9th reciprocal) and igniting section bellows (the such as the 1st and the 2nd bellows) enters in the second fly-ash separator 10 (i.e. electric precipitator) and thionizer 12 via large flue pipeline L2 and processes under main exhauster 11 acts on, and the flue gas after process is discharged.
In step 5) in, agglomerate after prereduction adopts nitrogen to cool in pot type water cooler 7, to prevent the secondary oxidation of prereduced sinter, cooled high-temp waste gas is transported to for cogeneration in afterheat generating system, and the exhaust gas recirculation after cogeneration to pot type water cooler 7 for the cooling of agglomerate.Spray a certain amount of calcium chloride (such as with the solution form of 2-5wt% concentration) in the exit of water cooler to prereduced sinter, reduce reoxidizing of transportation prereduced sinter.
The reduction degree of the prereduced sinter obtained is in 40% ~ 45% scope, and this mainly comes from the reduction of carbon-burdened pellet.
Owing to using common fine iron breeze in the present embodiment 1, without the need to increasing a phosphorus collector 13 on large flue pipeline L2.
Embodiment 2
Repeat embodiment 1, just adopt high-phosphorus iron ore powder to replace fine iron breeze to make Carbon-containing Pellets.Large flue pipeline L2 increases a phosphorus collector 13.By analyzing the phosphorus content of pellet in the phosphorus content of high-phosphorus iron ore powder and prereduced sinter, the dephosphorization rate recording pellet is 75wt%.
Comparative example 1 (prior art)
Repeat embodiment 1.According to the technique described in CN102127636B.
Effect data
Claims (15)
1. a smoke gas circulating type prereduction agglomerating plant, is characterized in that this device comprises: sinter machine (4); Be positioned at the ignition furnace (1) of the front end of sinter machine (4); Seal closure (2) above the pallet being positioned at sinter machine (4); Flue gas recirculation main line (L1); Towards the large flue pipeline (L2) of blowdown stack; Oxygen-rich air pipeline (L3); A kind of mixing chamber (3) of the circulating flue gas carried via flue gas recirculation main line (L1) for mixing and the oxygen-rich air carried via oxygen-rich air pipeline (L3) or central cooler waste gas; With, the pot type water cooler (7) of agglomerate; Wherein sinter machine (4) has 20-34 bellows.
2. device according to claim 1, is characterized in that it comprises further: be arranged at the first fly-ash separator (8) on flue gas recirculation main line (L1) and induced draft fan (9); With, be arranged at the second fly-ash separator (10) on large flue pipeline (L2), main exhauster (11), thionizer or desulfurizer (12) and phosphorus collector (13).
3. device according to claim 1 and 2, is characterized in that sinter machine (4) has 20-32 bellows.
4. device according to claim 1 and 2, is characterized in that sinter machine (4) has 24-28 bellows.
5. device according to claim 3, is characterized in that several bellows of sinter machine head or front end and several bellows flue gas separately of sinter machine afterbody or rear end export arm and be connected to flue gas recirculation main line (L1).
6. device according to claim 4, is characterized in that several bellows of sinter machine head or front end and several bellows flue gas separately of sinter machine afterbody or rear end export arm and be connected to flue gas recirculation main line (L1).
7. device according to claim 3, is characterized in that, the middle part bellows of sinter machine (4) and igniting section bellows flue gas separately export branch road and be connected to large flue pipeline (L2).
8. device according to claim 4, is characterized in that, the middle part bellows of sinter machine (4) and igniting section bellows flue gas separately export branch road and be connected to large flue pipeline (L2).
9. according to the device in claim 2,5,6,7 or 8 described in any one, it is characterized in that, the first fly-ash separator (8) is tornado dust collector.
10. device according to claim 3, is characterized in that, the first fly-ash separator (8) is tornado dust collector.
11. devices according to claim 4, is characterized in that, the first fly-ash separator (8) is tornado dust collector.
12., according to the device in claim 2,5,6,7,8,10 or 11 described in any one, is characterized in that, the second fly-ash separator (10) is electric precipitator or electricity+cloth bag complex dust collector.
13. devices according to claim 3, is characterized in that, the second fly-ash separator (10) is electric precipitator or electricity+cloth bag complex dust collector.
14. devices according to claim 4, is characterized in that, the second fly-ash separator (10) is electric precipitator or electricity+cloth bag complex dust collector.
15. devices according to claim 9, is characterized in that, the second fly-ash separator (10) is electric precipitator or electricity+cloth bag complex dust collector.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520390447.4U CN204803377U (en) | 2015-06-05 | 2015-06-05 | Flue gas recirculation formula prereduction sintering device |
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| CN201520390447.4U CN204803377U (en) | 2015-06-05 | 2015-06-05 | Flue gas recirculation formula prereduction sintering device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106282546A (en) * | 2015-06-05 | 2017-01-04 | 中冶长天国际工程有限责任公司 | A kind of smoke gas circulating type prereduction sintering process and device |
| CN107304460A (en) * | 2016-04-19 | 2017-10-31 | 中冶长天国际工程有限责任公司 | A kind of iron ore prereduction sintering method and its device |
| WO2021072814A1 (en) * | 2019-10-14 | 2021-04-22 | 中国科学院过程工程研究所 | Oxygen-enriched sintering flue gas circulation system and application thereof |
| CN113528809A (en) * | 2021-07-02 | 2021-10-22 | 北京科技大学 | Hydrogen-rich sintering gasification dephosphorization recovery system and method |
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2015
- 2015-06-05 CN CN201520390447.4U patent/CN204803377U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106282546A (en) * | 2015-06-05 | 2017-01-04 | 中冶长天国际工程有限责任公司 | A kind of smoke gas circulating type prereduction sintering process and device |
| CN106282546B (en) * | 2015-06-05 | 2018-11-06 | 中冶长天国际工程有限责任公司 | A kind of smoke gas circulating type prereduction sintering process |
| CN107304460A (en) * | 2016-04-19 | 2017-10-31 | 中冶长天国际工程有限责任公司 | A kind of iron ore prereduction sintering method and its device |
| CN107304460B (en) * | 2016-04-19 | 2019-10-01 | 中冶长天国际工程有限责任公司 | A kind of iron ore prereduction sintering method and its device |
| WO2021072814A1 (en) * | 2019-10-14 | 2021-04-22 | 中国科学院过程工程研究所 | Oxygen-enriched sintering flue gas circulation system and application thereof |
| CN113528809A (en) * | 2021-07-02 | 2021-10-22 | 北京科技大学 | Hydrogen-rich sintering gasification dephosphorization recovery system and method |
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