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WO1998007891A1 - Procede pour fabriquer des minerais frittes et machine a fritter les minerais - Google Patents

Procede pour fabriquer des minerais frittes et machine a fritter les minerais Download PDF

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Publication number
WO1998007891A1
WO1998007891A1 PCT/JP1997/002843 JP9702843W WO9807891A1 WO 1998007891 A1 WO1998007891 A1 WO 1998007891A1 JP 9702843 W JP9702843 W JP 9702843W WO 9807891 A1 WO9807891 A1 WO 9807891A1
Authority
WO
WIPO (PCT)
Prior art keywords
raw material
sintering
packed bed
material packed
pressure
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP1997/002843
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English (en)
Japanese (ja)
Inventor
Tsutomu Okada
Yozo Hosotani
Masanori Nakano
Kenichi Higuchi
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Nippon Steel Corp
Original Assignee
Nippon Steel Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Nippon Steel Corp filed Critical Nippon Steel Corp
Priority to DE69716231T priority Critical patent/DE69716231T2/de
Priority to JP51056998A priority patent/JP3930570B2/ja
Priority to BR9706625-7A priority patent/BR9706625A/pt
Priority to AU38653/97A priority patent/AU697445B2/en
Priority to EP97935796A priority patent/EP0861908B1/fr
Publication of WO1998007891A1 publication Critical patent/WO1998007891A1/fr
Priority to KR1019980702769A priority patent/KR100257441B1/ko
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • 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
    • C22B1/205—Sintering; Agglomerating in sintering machines with movable grates regulation of the sintering process

Definitions

  • the present invention relates to a method and a sintering machine for producing a sintered ore, which is a raw material of a blast furnace production method, and more particularly to a method for transferring a combustion molten zone from the upper side to the lower side of a sintering pallet.
  • the supply rate of the oxygen-containing gas is increased, the differential pressure is increased, the traveling speed of the combustion melting zone is extremely accelerated, the production rate is increased, and the product is increased.
  • the present invention relates to a method for producing a sinter which improves quality and yield and a sintering machine therefor.
  • Dwight toroid type sintering machines are widely used. This is done by adding a solvent such as limestone or silica stone, a fuel such as coke breeze, and water to the raw ore powder, mixing and granulating the mixture, and filling the mixture on a sintered pallet arranged in the shape of a villa.
  • the sintering pallet is sequentially moved horizontally to ignite the surface of the packed bed in the ignition furnace, and then sucked from below to burn the fuel such as coke in the blended raw material
  • the generated heat melts and solidifies the raw material ore, gradually moving the combustion zone from the surface layer to the lower layer and sintering it.
  • the sintering time is about 20 to 40 minutes.
  • the Dwight Toroids type sintering machine is a continuous type and is suitable for mass production because it is widely used. is there.
  • Current Dowai toroid type sintering machine is increased in size, width 5 m X rather force is up to things like the length 1 00 m, the production rate is 34 ⁇ 43 t Z d Z m 2 approximately.
  • the global resource situation there is a remarkable shortage of supply of lump ore, which is a raw material for the blast furnace manufacturing method, and the price of lump ore is increasing accordingly. Use is required.
  • silica stone and serpentine, limestone, and coke breeze and anthracite added as fuel are added as auxiliary materials. It is better to reduce the amount, such as coke oven gas and pulverized coal, which is the fuel for ignition.
  • the first half of the upper part of the strand is provided with the first half of the negative pressure
  • the second half of the upper part of the strand is provided with the second half of the pressure
  • By circulating the exhaust gas in the second half by the pressure in the first half and the negative pressure in the first half it is possible to reduce the amount of exhaust gas, reduce power costs and prevent a drop in productivity.
  • the part to be sintered in the second half of the atmosphere is covered with a positive pressure hood, and the second half is sintered. The purpose is to remove the blower following the wind box and reduce the amount of exhaust gas by means of exhaust gas circulation equipment that minimizes equipment costs. No attempt was made to increase it to increase productivity.
  • the sintering completion point in this method is in the early stage of the latter half of the hood, and on the strand in the remaining range of the latter half. I can only imagine that they are doing cooling in the country. Therefore, the sintering completion point is not as close as possible to the mining section, and the entire strand is not used to maximize the production rate.
  • the purpose is to prevent pressurized air from flowing out into the atmosphere, and there is no mention of actively increasing the transfer speed of the sintering zone in the raw material packed bed to improve productivity.
  • the suction flow rate at this location must be higher than the suction flow rate of the conventional method of sucking air. For this reason, the shortage of the high-temperature holding time in the baking of the upper layer of the raw material layer, which has been a problem in the past, is promoted, and the yield and quality of the upper layer of the raw material layer are deteriorated, so that the total productivity is greatly increased. It didn't make it.
  • Japanese Patent Application Laid-Open No. 61-243131 discloses that “the upper surface of a sintered ore on an endless pallet is used in order to eliminate the need for a large hermetic housing required for the pressure sintering method. A cost can be reduced by providing a hood in the hood, forcing air into the hood, and creating a negative pressure in the wind box below the endless pallet. " However, the purpose is to reduce the total power of the conventional exhaust fan power combined with the push-in and exhaust fan power, and to increase the transfer speed of the combustion zone in the packed bed to increase productivity. No attempt was made to improve the quality of the project.
  • the push-in fan and the exhaust fan are used.
  • the current sintering machine exhausts the entire volume of the high-temperature air that has expanded in volume, while the room temperature air is pushed in and blown to reduce the total power, thereby improving productivity. It does not positively increase the transition speed of the combustion zone in the required raw material bed.
  • Japanese Patent Publication No. 5-55574 discloses that “a plurality of wind boxes are divided in the longitudinal direction of the pallet, and the sintering raw material charged and laminated on the pallet is divided into a plurality of wind box groups.
  • the suction negative pressure decreases in the early stage of the sintering reaction compared to the suction negative pressure in the normal operation, and increases in the middle period up to the end of the firing reaction.
  • the yield, drop strength (SI) and RDI of the upper part of the sintering bed can be improved, and in addition, the exhaust power can be reduced.
  • the sensible heat of the sinter can be recovered efficiently.
  • the sinter in the upper part of the sintering bed has already improved the RDI and SI compared to the sinter in the lower part, and in order to further improve the quality of the entire sinter, 'It is more important to improve the sinter in the lower layer. Even if the yield in the upper part of the sintering bed can be improved, the quality of the sinter ore can be reduced, and the power consumption can be reduced somewhat, the balance of the air intake volume at the beginning, middle and late stages of sintering can be improved to save energy. Also There were also adverse effects such as lower yield in the middle part and lower SI in the lower part.
  • the production rate of the sintering machine largely depends on the transition speed when the combustion zone in the raw material packed bed gradually transitions from the surface layer to the lower layer.
  • the problem in improving the sintering production rate is that the sintering machine is in the process of firing from the upper layer to the lower layer of the raw material bed in the strand from the ignition section to the mining section. That is, the transition speed of the combustion melting zone is slow. Therefore, if the transition speed of the combustion melting zone is the same as before, increasing the layer thickness of the packed bed and the moving speed of the sintering pallet will increase the length of the sintering machine required to complete sintering. As the sintering time increases, the production rate does not increase.
  • the transition speed of the combustion zone is too high, the amount of heat required for sintering cannot be secured due to insufficient coke combustion, which may lead to deterioration in yield and quality. Therefore, it is important to secure the heat required for the sintering reaction and to increase the transition speed of the combustion melting zone in order to greatly increase the production rate of the sintering machine. Furthermore, in the raw material bed, since the ventilation resistance of the combustion zone is large, if the thickness of the combustion zone in the height direction of the raw material bed is minimized, the air permeability is improved and coke combustion is performed. By increasing the speed, the transition speed of the combustion melting zone can be increased. Thus, controlling the cooling rate of the cooling zone above the combustion zone and the transition speed of the combustion zone in a well-balanced manner is also important for greatly improving the production rate of the sintering machine.
  • the present invention is to reduce the thickness of the raw material packed layer and the moving speed of the sintered pallet. It is an object of the present invention to provide a method for producing a sintered ore, a method for producing a low SiO 2 sintered ore, and a sintering machine used for these methods, which can greatly increase the productivity of the sintering machine by increasing it.
  • the gist of the present invention that achieves the above objects is as follows.
  • a blended raw material containing raw material ore, a solvent and a fuel is charged on a sintering machine pallet to form a raw material packed bed, which is then ignited on the surface of the raw packed bed and lit from above.
  • the mass flow rate of the oxygen-containing gas to be supplied to the raw material packed bed is determined when the upper layer of the raw material packed bed is sufficiently fired.
  • the sintering is performed by changing the mass flow rate of the oxygen-containing gas supplied in the range of sintering the upper layer to 1.0 to 2.6 times, and sintering. Concentration production method.
  • a pressurized hood for pressurizing an oxygen-containing gas is provided on the raw material packed bed on the sintered pallet, and the pressure in the pressurized hood is increased to 100 to 3000 mmAci with respect to the atmospheric pressure.
  • a pressurized hood for supplying oxygen-containing gas under pressure within the range of 5 to 95% of the pressure is provided, and the inside of the pressurized hood is pressurized to 100 to 3000 dragon Aq against atmospheric pressure.
  • the sinter production method according to any one of (1) to (3).
  • a pressurized hood for pressurizing and supplying an oxygen-containing gas within a range of 5 to 95% of the width of the pallet is provided on the raw material packed layer on the sintered pallet.
  • the sintering exhaust gas is circulated through a pressurized hood provided on the raw material packed layer and pressurized to supply an oxygen-containing gas, wherein (12) to (14).
  • the sintering machine according to 1.
  • FIG. 1 is a view showing an embodiment of a sintering machine according to Examples la and 3a of the present invention.
  • FIG. 2 is a view showing an embodiment of a sintering machine according to Embodiment 1b of the present invention.
  • FIG. 3 is a diagram showing an embodiment of a sintering machine according to Examples lc to le and 3b of the present invention.
  • FIG. 4 is a diagram showing an embodiment of a sintering machine according to Examples 2a to 2d and 3c of the present invention.
  • FIG. 5 is a view showing another embodiment of the sintering machine of the present invention.
  • FIG. 6 is a view showing a sealing mechanism of a pressurized hood of the sintering machine according to the present invention.
  • FIG. 7 is a view showing a plate-shaped thin cake supporting stand of the sintering machine according to the present invention. is there.
  • FIG. 8 (a) is an explanatory diagram showing the transition of the combustion melting zone in the pallet according to the present invention.
  • FIG. 8 (b) is a sectional view taken along the line AA ′ of the combustion melting zone in the pallet according to the present invention.
  • FIG. 8 (c) is an explanatory diagram showing the transition of the combustion melting zone at the time of cooling on the strand according to the present invention.
  • FIG. 8 (a) is an explanatory view showing one example of a raw material packed bed sintering process of the present invention.
  • I is the initial raw material zone
  • ⁇ is the wet (condensed water) zone
  • m is the dry zone
  • w is the combustion zone
  • V is the melting zone
  • VI is the sintering zone.
  • FIG. 8 (b) is a sectional view taken along the line AA ′ in the center of FIG. 8 (a).
  • point B indicates a position closest to the ignition furnace where an initial combustion melting zone is formed in the present invention and the supply amount of the oxygen-containing gas in the raw material packed bed is changed and increased
  • point C is the combustion completion point. Is shown. In normal operation, operation is performed so that the sintering completion point is constant in order to use the entire strand efficiently and stably produce. When the production volume is important, the sintering completion point should be as close as possible to the mining side, and when yield and quality are to be emphasized, allowance for one or two wind boxes should be provided.
  • the sintering completion point should be kept close to the ignition furnace side to keep the sintering constant.
  • the operation where the sintering completion point C 'is changed to the middle part of the strand Is performed when cooling on a strand, for example, as shown in Fig. 8 (c), the operation where the sintering completion point C 'is changed to the middle part of the strand Is performed.
  • the supply amount of the oxygen-containing gas may be changed based on the layer thickness or the position in the strand length direction based on the present invention disclosed below.
  • an example is shown in which the sintering completion point is located at a position where the strand length is 95% from the ignition portion.
  • the blowing or suction pressure is shown as the pressure with respect to the atmospheric pressure.
  • the range of 30% or less of the strand length from the ignited part is almost equivalent to the firing area of the upper 20% of the raw material packed bed, and the yield and quality of the upper layer of the raw material packed bed are generally lower and middle. Inferior to. This is because the coke combustion rate, which gives the calorific value necessary for the calcination reaction, is not sufficient because it is just after ignition. In addition, it is due to the heat dissipated from the surface. Therefore, it is necessary to secure the amount of heat required for the sintering reaction.
  • the range of 30% or less of the strand length from the ignition portion, which is the firing area in the upper layer of the raw material packed layer is less than the conventional range.
  • the high temperature holding time of the upper part of the raw material packed bed can be secured, so that the yield and quality of the upper part of the raw material packed bed can be secured.
  • the calorific value of the part may be increased.
  • the suction negative pressure at the site it is preferable to lower the suction negative pressure at the site, to enhance the coke segregation at the upper part of the raw material packed layer, or to add a please to the surface layer.
  • heat can be applied from the outside of the raw material packed layer. For example, hot air can be sucked into the portion, or induction heating by microwave or the like can be performed.
  • the range of 30 to 95% of the strand length from the ignition part corresponds to the firing area in the lower part of the raw material packed bed.
  • the sintered zone in the upper part of the raw material packed bed has low air resistance.
  • the thickness of the combustion-melting zone having a high airflow resistance increases, so that the airflow resistance increases.
  • the air permeability deteriorates and the calorific value becomes excessive.
  • the mass flow rate of the oxygen-containing gas is forcibly supplied from above to the combustion zone with a large pressure loss in the range from the middle to the lower part (within the range of 30 to 95% of the strand length from the ignition part).
  • the coke combustion rate in the middle to lower layers is increased, and the combustion melting zone is increased.
  • the cooling speed of the cooling zone above the combustion melting zone is increased by increasing the cooling speed, and the calorie required for sintering is secured, and the thickness of the combustion melting zone is reduced and the air permeability is improved. in this way It is important to control the calorific value and air permeability depending on the temperature of the combustion melting zone and the thickness in the height direction of the raw material packed bed in order to improve the sintering production rate.
  • the mass flow rate represents the mass of gas flowing per unit time, and the unit is expressed in kgZ s or the like.
  • the generally used flow rate is a volume flow rate, which indicates the volume of gas flowing per unit time, and the unit is expressed in m 3 Z s or the like.
  • the volume flow varies with temperature and pressure according to the equation of state of the gas.
  • the oxygen-containing gas in the present invention includes not only the atmosphere but also the exhaust gas discharged from the sintering machine and the exhaust gas from other processes, etc., as well as the mixed gas of the atmosphere and the exhaust gas and the oxygen-enriched gas. It also contains gas, and gas with an oxygen concentration of 12 to 40 vol% is preferred.
  • the mass flow rate of the oxygen-containing gas supplied to the raw material storage layer within the range of 30 to 95% of the length of the strand from the ignition part is set to the range of the raw material charge in the range of the strand excluding the above range.
  • the reason why the mass flow rate of the oxygen-containing gas supplied to the ⁇ layer is adjusted to 1.01 to 2.6 times is that when the mass flow rate is less than 1.01 times, the transition speed of the combustion melting zone hardly changes. If it is more than 6 times, the gas flow velocity will increase too much and the combustion melting zone will be supercooled, or the raw material packed bed will be compacted due to the increase in the differential pressure above and below the raw material packed bed, and the gas permeability will be impaired.
  • the mass flow rate of the oxygen-containing gas sucked into the raw material packed bed within the range of 50 to 85% of the length of the strand from the ignition part is adjusted to the range of the raw material filled in the range of the strand excluding the above range. It is particularly preferable to adjust the mass flow rate of the oxygen-containing gas supplied to the bed to 1.1 to 1.8 times from the viewpoint of improving the productivity of sinter.
  • the length of the strand from the ignition part must be 30 to 95%.
  • Thickness direction of raw material packed bed within the range Is preferably 1.1 to 5.0 times the pressure difference in the thickness direction of the raw material packed bed in the range of the strand excluding the above range.
  • the ventilation resistance is about 1.5 to 5 times larger than that of the other range.
  • the differential pressure is less than 1.1 times, the effect of promoting the transition speed of the combustion and melting zone by increasing the air flow rate is small, and if the differential pressure exceeds 5.0 times, the gas flow velocity becomes too large, and Since the speed is greatly increased, it becomes impossible to secure a high-temperature holding time, and the raw material packed layer is undesirably densified and the air permeability is deteriorated. Further, it is particularly preferable to increase the pressure difference to 1.2 to 2.0 times from the viewpoint of improving productivity. It is preferable that the gas supply is gradually increased from the ignition section to the ore removal section to make the transition speed of the combustion melting zone and the cooling speed close.
  • the cooling rate will be faster than the coke burning rate for a short period of time, and some parts will not be able to maintain a sufficient amount of calcining heat. This is because the quality of the sinter is deteriorated.
  • the mass flow rate is increased by increasing the differential pressure of the raw material bed within the range of 30 to 95% of the strand length from the ignition part, the production rate of sinter As well as improving the yield, it is possible to obtain products with excellent yield and quality. If the pressure difference is increased and the gas supply is increased, the amount of exhaust gas discharged from this part also increases in tandem with this. However, since the firing reaction is active and the oxygen consumption efficiency is high, the oxygen consumption efficiency may be reduced.
  • the unit of airflow can be reduced by minimizing the supply of excess gas in the upper part and in the vicinity of the mining part.
  • the present inventors avoid the deterioration of air permeability caused by the consolidation of the raw material packed bed by increasing the mass flow rate of the oxygen-containing gas by combining the downward suction of the raw material packed bed and the pressurization from above. Then, the mass flow rate of the oxygen-containing gas to be supplied to the raw material packed bed within the range of 30 to 95% of the length of the strand from the ignition section is reduced to the range of the raw material in the range of the strand excluding the above range.
  • a pressurized hood is provided to cover the raw material packed bed loaded on the sintering pallet, the inside of the hood is pressurized, and oxygen-containing gas is blown from above to the raw material packed bed.
  • the air is sucked and exhausted from the wind box just below the pallet, and the pressure difference between the upper part of the raw material packed bed and the lower part of the raw material packed bed is controlled. Let the gas flow.
  • the static pressure in the raw material packed bed is higher than the static pressure in the raw material packed bed formed by suctioning the raw material packed bed from below at atmospheric pressure. Can be increased.
  • the present invention can increase the mass flow rate to be supplied into the raw material packed bed compared to the conventional method.
  • Gas density can be made higher than before.
  • the supply amount of the oxygen-containing gas into the raw material packed bed increases, the coke burning rate in the raw material packed bed increases, the calorific value of the combustion zone increases, and the transition speed increases.
  • the cooling zone transition speed increases. If the static pressure in the raw material packed bed increases, the heat transfer rate between the gas and the solid also increases, which can promote the transition of the combustion melting zone and the cooling of the cooling zone.
  • gas can be supplied to the combustion melting zone where a reaction has occurred by forming a uniform gas flow through the sintered zone having low airflow resistance.
  • gas when gas is supplied by suction from below, gas is subjected to relatively high ventilation resistance in the wet zone with relatively high ventilation resistance and the combustion and melting zone in which the calcination reaction is occurring. Flow, forming an uneven gas flow This is a state in which the reaction efficiency between the body and the solid tends to deteriorate. Therefore, the gas flow pushed in from above forms a more uniform gas flow than the gas flow sucked from below, so that the oxygen consumption efficiency is improved and the unit air volume required for sinter production can be reduced. .
  • the pressure hood provided above the raw material packed bed must be 100 to 3000 mm.
  • the suction negative pressure of the wind box just below the pallet is set in the range of 12000 to 1 mmAq, due to the setting of the differential pressure pattern above and below the raw material packed bed. If the pressure is less than 2000 mmAq, the static pressure level in the raw material bed will not be much higher than in the conventional method even if the upper part of the raw material bed is pressurized. The increase in heat transfer rate due to an increase in gas density is small. If it exceeds 1 nunAq, the exhaust gas cannot be sucked.
  • the upper and lower sides of the raw material packed bed within the range of 30 to 95% of the strand length from the ignition part It is preferable that the pressure difference be between 1,000 and 3000 mmAq, which depends on the layer thickness and the pallet speed.
  • the pressure difference between the upper and lower parts of the raw material bed is less than 1 000 Aq
  • the pressure difference in the raw material bed is smaller than in the conventional method, and the gas flow rate is lower than the effect of increasing the static pressure. This is because the adverse effects increase.
  • the strand length is within the range of 30 to 95% from the ignition section.
  • the mass flow rate of the oxygen-containing gas sucked into the raw material bed in the above-mentioned range is 1.01 to 1.01 with respect to the mass flow rate of the oxygen-containing gas supplied to the raw material bed in the range of the strand excluding the above range. 2.
  • the pressure difference in the layer thickness direction of the raw material packed bed is increased by a factor of 6 with respect to the pressure difference in the layer thickness direction of the raw material packed bed in the strand range excluding the above range. It can be easily adjusted by a factor of 0.
  • the transition speed of the combustion zone cannot be increased from the current level.
  • the area with a strand length of 30% or less from the ignition part is blown from the upper part of the raw material packed bed with 100 to 100 mmAq under pressure and directly below the pallet.
  • the negative suction pressure for suction and exhaust from the wind box force is set to 11,000 to 11 mmAq, and the differential pressure between the upper and lower parts of the raw material bed is adjusted to 300 to 2,000 nnnAq to obtain the differential pressure of the conventional downward suction. If the pressure difference is the same or a small pressure difference, the high-temperature holding time can be secured or increased, and the calorific value required for firing can be obtained. At this time, the oxygen supply rate of the upper layer of the raw material packed bed is increased, so that the same effect of improving coke combustibility as oxygen enrichment can be obtained, and the yield and quality of the upper layer of the raw material packed bed can be improved. You can do more.
  • the pressurized feed is moved from the ignition section to the It is preferable to set the length within a range of 30 to 95% in terms of simplification of equipment. Furthermore, if the pressurized hood is divided into a plurality of pieces in the length direction of the strand, the mass flow rate can be changed stepwise from the igniting section to the mining section.
  • the transition speed of the combustion melting zone is high because the vicinity of the side wall within 5% in the pallet width direction from the pallet side wall of the raw material packed layer has less airflow resistance than the center part. For this reason, if a pressure hood is provided within the range of 5 to 95% of the width of the raw material packed bed and gas is supplied so that the transition speed of the combustion melting zone becomes uniform in the width direction, the combustion melting zone The effect of increasing the transition speed is even greater.
  • the pressure hood is installed above the moving sintering pallet. It is preferable to provide a seal mechanism at the lower end of the pressure hood to avoid air leakage. As shown in FIG. 6, the sealing mechanism is such that the sheet 24 provided at the lower end of the hood is pressed against the upper surface of the raw material-filled layer 7 by the internal pressure of the pressurizing hood 19 to seal, A structure in which the pallet is slid on the raw material packed layer 7 as it moves is preferable. In addition, a structure having several stages of sealing mechanisms 23, a structure in which air is blown from the outside of the pressure hood 19 between the pressure hood 19 and the raw material packed layer 7, a side wall of the pallet 6, and the like are provided. It is also possible to provide a sealing mechanism by utilizing it, and it is not limited to these examples.
  • the oxygen concentration should be between 12 and 21 in the pressurized hood in the range of 30-95% of the strand length from the igniter, and particularly preferably in the range of 60-80% of the strand length.
  • Supplying a gas adjusted to less than vol% promotes the generation of magnetite that improves RD1 and suppresses the oxidation of nitrogen in coke to NOx, improving RDI and reducing NOx. It is effective in controlling the occurrence You.
  • part of the exhaust gas from the sintering machine can be recycled.
  • the capacity of the blower for exhaust gas circulation is designed by taking into account the suction negative pressure, the air flow, and the size of the equipment so that the air flow from the upper part of the raw material packed bed can be sent to the exhaust gas treatment equipment.
  • the oxygen concentration is preferably 12 vol% or more and less than 21 vol%. In particular, when the oxygen concentration is less than 18 vol%, the effects of improving RDI and suppressing NOx generation become more remarkable.
  • the optimal number of plate-shaped sinter cake support stands 21 depends on the size of the pallet 6, for example, a 4 m wide and 2 m long pallet. At the conclusion, it is 2 to 10 sheets and the height is preferably 200 to 400. The more the number of sinter cake support stands, the more the sinter cake support effect can be exhibited. However, if the number of sheets exceeds 10, the volume occupied by the sinter cake support stand will increase, and conversely, the adverse effect on the production rate will begin to appear, and the production rate will begin to decline. If the sinter cake is supported by the sinter cake support stand, breathability is improved.
  • the amount of CO generated increases due to the increased coke combustion rate, and the reaction to reduce the generated NO with CO gas becomes more active, thereby suppressing the generation of NOx. .
  • the present invention is of particularly useful for the production of low Si0 2 sinter containing Si0 2 3.9 ⁇ 4.9mass% is, Si0 2 is a call want underlying limestone blending ratio becomes below 4.9Mass% and a CaO Si0 2 of the influence of the reduction of slag main component begin to remarkable deterioration of the production rate and RD1, because can not improve the production rate and RD! exacerbated also by the present invention and is less than 3.9mass%.
  • the mass flow rate of the oxygen-containing gas sucked into the raw material packed bed within the range of 30 to 95% of the length of the strand from the ignition section in the strand from the ignition section to the mining section can be increased up to 2.6 times the mass flow rate of the oxygen-containing gas sucked into the raw material packed bed in the range of the strand excluding the above range, so that the conventional layer thickness of 400 to 600 mm can be obtained.
  • the moving speed of the sintering pallet can be increased 2.0 times or more compared to the conventional method.
  • the thickness of the material-filled bed can be as large as 600 to 1500 mm, which is more than twice the conventional thickness, thereby increasing the production rate of the sintering machine up to 2.0 times the conventional sintering production rate. It has the tremendous effect of improving the production rate as well as improving the product yield and quality, and reducing the basic unit of exhaust gas flow rate.
  • the production rate can be kept constant, and the product yield and sinter quality can be improved, and the exhaust gas flow rate can be reduced.
  • a sintering machine used in the method for producing a sintered ore of the present invention a plurality of wind boxes at the lower part of a sintering strand are connected in parallel to a suction duct, and In addition to the conventional structure with a blower, a blower is added, and suction is performed from any point within the range of 30 to 95% of the suction duct length from the ignition section to the mining section, and the suction duct is used.
  • the mass flow rate of the oxygen-containing gas supplied to the raw material packed bed within the range of 30 to 95% of the length of the strand from the ignition part is reduced by the range of the strand excluding the above range.
  • 1.0 to 2.6 times the mass flow rate of the oxygen-containing gas to be sucked into the raw material bed, and the pressure difference in the thickness direction of the raw material bed except for the above range It can be adjusted to 1.1 to 5.0 times the pressure difference in the thickness direction of the raw material packed bed in the range of the command.
  • the suction duct is divided into a range of 30 to 95% of the length of the strand from the ignition part and the remaining range, and the structure in which the blowers are installed independently is the mass flow rate and the differential pressure. It is preferable in terms of adjusting the position.
  • three blowers may be provided for the front, middle and rear stages of the strand, the front and rear stages do not need to change the differential pressure, so the front and rear stages are connected to each other, and the strand length is 30 It is preferable to use two aircraft for the middle stage within the range of ⁇ 95% and for the other range.
  • a hood is provided on the raw material bed to be pressurized, and the inside of the hood is pressurized and the pressure in the hood and the pressure in the window box below It is preferable to measure Further, it is desirable to provide a seal structure between the hood and the raw material packed bed and between the hood or the hood and the pallet.
  • FIGS. 1 to 3 are views showing an embodiment of the sintering machine of the present invention.
  • the sintering blended raw material 1 is continuously supplied from the surge hopper 2 to the pallet 6 via the drum feeder 3 and the raw material charging device 5, and is layered on the pallet 6 as a raw material filling layer 7. It is laminated.
  • the sprocket 4 on the raw material supply side is rotated to move the pallet 6 at a predetermined speed, and at the same time, a plurality of wind boxes 8 and a main box provided below the pallet 6 are provided. 9, Intake by the blower 11 through the exhaust gas dust collector 10 and exhaust from the chimney 12.
  • a sub duct 13 is connected to a part of the main duct 9, and the sub duct 13 is taken in by a blower 15 through an exhaust gas dust collector 14, and the exhaust gas is returned to the main duct 9. Exhaust gas taken in by the probe 15 can also be discharged from the chimney 12. Further, it is desirable that the main body 9 be provided with a damper 16 for adjusting the negative pressure in the duct.
  • the ignition furnace 27 ignites the upper surface of the raw material packed bed 7 and controls the speed so that the raw material packed bed 7 on the pallet 6 completes the sintering reaction over the whole bed while reaching the mining section. Continuous operation is performed. Exhaust gas can be circulated to the pressurized hood 19 by the blower 18 from the front of the chimney 12, and air can be mixed at the same time. When pressurizing the inside of the pressurized hood 19, a seal mechanism 23 as shown in FIG. 6 is provided between the surface layer portion of the raw material packed bed and the lower end of the hood. Maintain internal pressure.
  • the length in the pallet traveling direction and the length in the pallet width direction can be set freely. Further, in this apparatus, the thickness of the raw material-filled layer 7 can be 600 to 1500 mm, which makes it possible to make the raw material-filled layer 7 thicker than before.
  • Blending raw materials, without particular for the manufacture of a low Si0 2 sinter one conventional As a general formulation, various iron ore and limestone, quicklime, serpentinite, miscellaneous raw materials such as scale, return ores, Si0 2 is 5.8Mass% in sinter coke breeze, A 1 2 0 3 was adjusted to 1.8 mass%, and the basicity was adjusted to 1.7. The return ratio was set at 15% based on the total of 100 new materials, and the coke ratio was set at 4.2% based on the total of 100 new materials. The same formulation was used for both the comparative example and the example.
  • Example 1a the layer thickness was 550 hidden, the length of the strand from the ignition section was 30%, and the length from the strand length of 95% to the mining section was 1500 mmAq.
  • the air was sucked downward at a pressure of 2500 mmAq between 30 and 95%, and the upper part of the raw material packed bed was opened to the atmosphere.
  • the mass flow ratio was 1.26 and the differential pressure in the layer thickness direction was 2500 Aq in the other range within the range of the strand length of 30 to 95%.
  • Example 1b the layer thickness was 550 mm, the area from the ignition section to the mining section was suctioned downward at -1000 mmAq, and the pressurized hood on the upper portion of the raw material packed bed having a strand length of 30 to 95% was drawn. The inside was pressurized to 1500 mmAq. In this case, the mass flow ratio was 1.27 and the differential pressure in the layer thickness direction was 2500 mmAq in the range of the strand length of 50 to 95% with respect to the other range.
  • Example 1c the layer thickness was 550 mm, the length from the ignition section was 30% of the strand length, and the section from the 95% strand length to the mining section was suctioned downward at -500 mmAq.
  • the pressure hood is further continued and the pressure in the pressure hood is increased to 500 Aq.
  • the pressure in the pressure hood was increased to 2000 mniAq.
  • the mass flow ratio is 1.77 and the pressure difference in the layer thickness direction is 3000 when the strand length is within the range of 30 to 95%. Aq.
  • Example 1d the layer thickness was 550 nim, the area from the ignition section to the mining section was suctioned downward at a rate of 1000 mniAq, and a pallet width direction of 50 to 90% strand length 1 () to 90% Exhaust gas before the chimney was circulated in the pressure hood provided in the range, and the oxygen concentration was adjusted to 18 vol% and pressurized to 1500 mmAq.
  • the mass flow rate ratio was 1.27 and the differential pressure in the thickness direction was 2500 dragon Aq in the range of 50 to 90% of the strand length.
  • Example 1e four layers of plate-shaped skeleton supporters were installed evenly in the pallet width direction in parallel on the pallet with a layer thickness of 550 mm, and the distance from the ignition part to the mining part was -1000. Suction was performed using Aq, and the inside of a pressure hood provided in the range of 10 to 90% in the pallet width direction with a strand length of 5 () to 90% was pressurized to 1500 mmAq. In this case, the mass flow ratio was 1.27 and the differential pressure in the thickness direction was 2500 face Aq in the range of 50 to 90% of the strand length.
  • Example 1f the layer thickness was 800 ⁇ , and other settings were the same as in Example 1e.
  • the mass flow ratio was 1.27 and the differential pressure in the layer thickness direction was 2500 mmAq in the range of the strand length of 50 to 90% with respect to the other range.
  • the same compounding material as in the example was sintered by the conventional method in which the atmosphere was sucked from the ignition section to the mining section at a constant layer thickness of 550 and a negative pressure of 1500 minAq. did.
  • Table 1 shows the production rates, product yields, RD1, and NOx emissions per unit of the sintered ore obtained in Comparative Example 1 and Examples 1a to 1f.
  • the basic unit of NOx emission is represented by the product of the exhaust gas flow rate and the NOx concentration in the exhaust gas.
  • the production rate was significantly improved as compared with the comparative example.
  • the product yield tends to decrease, but in the present invention, the product yield is improved.
  • the RD1, J1S-RKJIS standard (final reduction rate) and the basic unit of NOx emission were also improved, and excellent operational and environmental effects were achieved.
  • FIGS. 4 and 5 show another embodiment of the sintering machine of the present invention.
  • the difference from the embodiment shown in FIGS. 1 and 3 is that the main duct 9 is completely removed. It is divided into independent blowers 11 and 15.
  • a blower 29 can be provided. When setting a plurality of pressure patterns in the direction of the strand length, a plurality of blowers may be provided in this manner.
  • the blending raw materials were the same as in Example 1, and the operation was adjusted for the pallet speed so that the sintering completion point was in the mining part.
  • Example 2a the layer thickness was 550 ⁇ , the length from the ignition part to the strand length of 50% was 1 lOOmmAq, and the distance from the ignition part to the strand length of 80% to the tailing part was 1500mmAq, and was lower at 1500mmAq. Suction is performed to open the upper part of the raw material packed bed to the atmosphere, and the lower part of the strand length of 50 to 80% is suctioned at -500 mmAq, and the pressure in the pressurized hood is set to 2000 mmAq. Pressed. In this case, if the strand length is within the range of 50 to 80%, the mass flow rate is The ratio was 1.52, and the differential pressure in the thickness direction was 2500 mmAq.
  • Example 2b the layer thickness was 550 mm, the length from the ignition section to 50% of the strand length was suctioned downward at 1 500 mmAq, and a pressure hood was further provided in this range.
  • the pressure in the pressurized hood was set to 500 mmAq, the pressure from the strand length of 80% to the mining part was reduced by 1000 Aq, and the pressure in the hood was set to 500 mmAq.
  • Downward suction was performed at 1500 mmAq between strand lengths of 50-80%, and the pressure in the pressure hood was increased to 100 mmAq.
  • the mass flow ratio was 1.56 and the pressure difference in the thickness direction was 2500 mm Aq in the range of 50 to 80% of the strand length.
  • Example 2c the layer thickness was 800 mm, and other settings were the same as in Example 2a. In this case, the mass flow ratio was 1.52 and the differential pressure in the layer thickness direction was 2500 mmAq in the range of 50 to 80% of the strand length c.
  • Example 2d the layer thickness was set to 800, and four plate-like sinter cake support stands were installed on the pallet evenly in the width direction of the pallet. Same as a. In this case, the mass flow ratio was 1.52 and the differential pressure in the layer thickness direction was 2500 mmAq in the range of the strand length of 50 to 80%, compared to the other range.
  • Comparative Example 1 the same blended raw material as in Examples 2a to 2d was suctioned from the ignition section to the mining section at a layer thickness of 550 ⁇ and a negative pressure of 1500 Aq, and the inside of the blended raw material layer was baked at a negative pressure. Sintered by conventional methods.
  • Table 2 shows the production rate, product yield, RDI, and NOx emission rate of the sintered ore obtained in Comparative Example 1 and Examples 2a to 2d.
  • the production rates of Examples 2a to 2d were remarkably improved as compared with the comparative examples.
  • the product yield tends to decrease, but in the present invention, the product yield is also improved.
  • RD and JI The unit emissions of S-RI and NOx have also been improved, and excellent operational and environmental benefits have been achieved.
  • Example 2d of the present invention has extremely excellent characteristics as the characteristics of the sintered ore that surpasses the values of the known technology.
  • Example 3a a layer thickness of 550 mni, a stroke length of 60% from the ignition part, and a stroke length of 80% from the strand length to the mining part were suctioned downward at ⁇ 1500 mmAq.
  • the air was suctioned by suctioning downward at 1,500 mm (1) between the strand lengths of 60-80%.
  • the mass flow ratio was 1.26 and the pressure difference in the thickness direction was 2500 Aq.
  • Example 3b the thickness of the layer was 550 mm, the initial firing period from the ignition portion to the strand length of 60%, and the final firing period from the strand length of 80% to the mining portion was-1500 mmAq.
  • the mass flow ratio was 1.38 within the range of the strand length of 60 to 80% and the pressure difference in the thickness direction was 2500 mmAq.
  • Example 3c the layer thickness was 550 mm, the strand length from the ignition section was 60%, and the strand length from 80% to the mining section was suctioned downward at -500 mmAq.
  • a pressure hood is further provided in the pressure hood, the pressure in the pressure hood is set to 500 mmAq, and a pressure of 1500 mmAq is drawn downward between a strand length of 60 to 80% and pressurized.
  • the pressure inside the hood at 100 mmAq, a part of the exhaust gas before the chimney was blown under pressure with the oxygen concentration adjusted to 16%.
  • the mass flow ratio was 1.56 and the differential pressure in the thickness direction was 2500 mmAq in the range of the strand length of 60 to 80% with respect to the other range.
  • Comparative Example 2 the same compounding raw material as in Examples 3a to 3c was used with a layer thickness of 550 ⁇ and a negative The atmosphere was sucked from the ignition section to the mining section at a constant pressure of 1500 imnAq, and the inside of the mixed material layer was sintered by a conventional method of sintering at a negative pressure.
  • Table 3 shows the production rates, product yields, RD1 and NOx emission basic units of the sintered ore obtained in Comparative Example and Examples 3a to 3c.
  • the production rate was significantly improved as compared with the comparative example.
  • the product yield tends to decrease, but in the present invention, the product yield is also improved.
  • Et al is, RDI, JIS-RI and NOx emissions per unit is also improved, as well as an excellent effect in operation plane and environmental, it could manufacture a low Si0 2 sinter.
  • the setting of the negative pressure during sintering, the oxygen concentration of the suction gas, and the suction time are not limited to those in the above-described embodiment.
  • Productivity orientation, RDI, J1S-RI improvement orientation, NOx emission reduction orientation, exhaust gas volume reduction Can be changed by pointing o
  • the layer thickness of the compounding material packed bed which had been difficult conventionally can be increased greatly, and the pallet moving speed can be increased, and the production rate of the sintering machine can be greatly improved.
  • the product yield and RD for JIS-RI are improved, and the amount of exhaust gas is reduced.
  • the present invention simultaneously provides an incompatible improvement effect, and the effect is extremely large.

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Abstract

Selon un procédé permettant de fabriquer des minerais frittés, on charge un matériau brut fondu, contenant un minerai brut en poudre, un solvant et un combustible, sur une palette d'une machine à fritter de façon à former un lit rempli de matériau brut, puis on fait brûler une surface dudit lit de façon à effectuer la réaction de frittage du haut vers le bas. Selon le procédé permettant de fabriquer des minerais frittés, quand, dans la machine à fritter, la couche supérieure du lit rempli de matériau brut est correctement cuite, on modifie le débit massique d'un gaz contenant de l'oxygène amené audit lit de façon qu'il soit égal à 1,01 à 2,6 fois le débit massique de gaz contenant de l'oxygène amené, dans les limites de cuisson de la couche supérieure du lit, ce qui permet un frittage ayant un rendement élevé et donnant un produit d'excellente qualité. Idéalement, quand l'extrémité d'une zone où se forme une bande en fusion provenant de la combustion atteint une position inférieure de 20 % de la hauteur du lit par rapport à la couche supérieure de celui-ci, on modifie de la manière décrite ci-dessus le débit massique du gaz contenant de l'oxygène amené au lit afin d'effectuer le frittage.
PCT/JP1997/002843 1996-08-16 1997-08-15 Procede pour fabriquer des minerais frittes et machine a fritter les minerais Ceased WO1998007891A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
DE69716231T DE69716231T2 (de) 1996-08-16 1997-08-15 Verfahren und vorrichtung zum sintern von mineralien
JP51056998A JP3930570B2 (ja) 1996-08-16 1997-08-15 焼結鉱の製造方法およびその焼結機
BR9706625-7A BR9706625A (pt) 1996-08-16 1997-08-15 Método de produção de minério sinterizado e máquina de sinterização para o mesmo
AU38653/97A AU697445B2 (en) 1996-08-16 1997-08-15 Method of producing sintered ore and sintering machine therefor
EP97935796A EP0861908B1 (fr) 1996-08-16 1997-08-15 Procede pour fabriquer des minerais frittes et machine a fritter les minerais
KR1019980702769A KR100257441B1 (en) 1996-08-16 1998-04-16 Method of manufacturing sintered ore and sintering machine therefor

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JP8/233696 1996-08-16
JP23369696 1996-08-16
JP27858696 1996-10-01
JP8/278586 1996-10-01
JP18026597 1997-06-23
JP9/180265 1997-06-23

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BR (1) BR9706625A (fr)
DE (1) DE69716231T2 (fr)
WO (1) WO1998007891A1 (fr)

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JP2009523912A (ja) * 2006-01-19 2009-06-25 シーメンス・ファオアーイー・メタルズ・テクノロジーズ・ゲーエムベーハー・ウント・コ 焼結装置における焼結のためのプロセス
JP2011252203A (ja) * 2010-06-02 2011-12-15 Nippon Steel Corp 焼結鉱の製造方法、シンターケーキ支持スタンドの設計方法及び原料充填層の層厚決定方法
WO2014080450A1 (fr) 2012-11-20 2014-05-30 Ｊｆｅスチール株式会社 Dispositif d'alimentation en combustible de gaz d'oxygène pour appareil de frittage
CN113215390A (zh) * 2020-12-24 2021-08-06 北京高能时代环境技术股份有限公司 一种含铜污泥烧结方法
US11104643B2 (en) 2017-06-19 2021-08-31 Unitika Ltd. Bismaleimide modified product and method for producing the same
JPWO2021172254A1 (fr) * 2020-02-27 2021-09-02

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AU2006309650B8 (en) * 2005-10-31 2010-12-16 Jfe Steel Corporation Method for producing sintered ore and sintering machine
JP4590001B2 (ja) * 2008-02-27 2010-12-01 新日本製鐵株式会社 焼結鉱の製造方法および焼結機
CN101881559B (zh) * 2010-07-22 2011-11-16 张健 新型节能烧结机
CN103033064B (zh) * 2012-12-28 2015-03-11 北京世纪源博科技股份有限公司 烧结烟气余热回收装置
CN103033063B (zh) * 2012-12-28 2016-05-18 北京世纪源博科技股份有限公司 烧结烟气余热回收方法
CN115143792B (zh) * 2022-07-22 2025-06-24 山东钢铁股份有限公司 一种烧结机和提高烧结成品率的方法
JPWO2024117144A1 (fr) * 2022-11-29 2024-06-06

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JPH0543951A (ja) * 1991-08-13 1993-02-23 Nippon Steel Corp 焼結機の操業方法
JPH05247546A (ja) * 1991-10-03 1993-09-24 Metallges Ag 焼結機による酸化鉄含有物の焼結方法
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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2009523912A (ja) * 2006-01-19 2009-06-25 シーメンス・ファオアーイー・メタルズ・テクノロジーズ・ゲーエムベーハー・ウント・コ 焼結装置における焼結のためのプロセス
JP2011252203A (ja) * 2010-06-02 2011-12-15 Nippon Steel Corp 焼結鉱の製造方法、シンターケーキ支持スタンドの設計方法及び原料充填層の層厚決定方法
WO2014080450A1 (fr) 2012-11-20 2014-05-30 Ｊｆｅスチール株式会社 Dispositif d'alimentation en combustible de gaz d'oxygène pour appareil de frittage
US11104643B2 (en) 2017-06-19 2021-08-31 Unitika Ltd. Bismaleimide modified product and method for producing the same
JPWO2021172254A1 (fr) * 2020-02-27 2021-09-02
WO2021172254A1 (fr) * 2020-02-27 2021-09-02 Ｊｆｅスチール株式会社 Procédé de production de minerai fritté
EP4112756A4 (fr) * 2020-02-27 2023-01-11 JFE Steel Corporation Procédé de production de minerai fritté
US12404566B2 (en) 2020-02-27 2025-09-02 Jfe Steel Corporation Method for producing sintered ore
CN113215390A (zh) * 2020-12-24 2021-08-06 北京高能时代环境技术股份有限公司 一种含铜污泥烧结方法
CN113215390B (zh) * 2020-12-24 2022-07-22 北京高能时代环境技术股份有限公司 一种含铜污泥烧结方法

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DE69716231T2 (de) 2003-08-14
KR100257441B1 (en) 2000-05-15
BR9706625A (pt) 1999-11-23
EP0861908A1 (fr) 1998-09-02
CN1062913C (zh) 2001-03-07
AU3865397A (en) 1998-03-06
JP3930570B2 (ja) 2007-06-13
CN1198779A (zh) 1998-11-11
DE69716231D1 (de) 2002-11-14
EP0861908A4 (fr) 1998-10-07
EP0861908B1 (fr) 2002-10-09

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