JP2011038735A - Sintering machine - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a downward suction type sintering machine capable of safely manufacturing sintered ore with high strength and high quality at a high yield ratio. <P>SOLUTION: A charge layer 9 is formed by charging a sintering material including powder ore and a charcoal material on a circulated pallet 8, and the charcoal material of the charge layer 9 is ignited by an ignition furnace and sucked by a wind box 16 arranged on the lower side of the pallet 8. Gas fuel is injected by a gas fuel supply device 12a-12d on the upper side of the charge layer 9 within a hood 21 arranged on the downstream side of the ignition furnace and surrounding the upper part of the charge layer 9, mixed with air and supplied to the charge layer 9 as diluted gas fuel. An FeO ratio measured by an FeO ratio measurement device 53 for measuring an FeO ratio in a sintered ore product is used for a management index for achieving predetermined cold strength, and operation for controlling the cold strength is performed by setting a target value of the FeO ratio to be a value lower than that when the gas fuel supply devices 12a-12d are not equipped. <P>COPYRIGHT: (C)2011,JPO&INPIT

Description

  The present invention relates to a sintering machine that produces a high-strength, high-quality sintered ore using a downward suction type Dwytroid (DL) sintering machine.

  Sinter ore, which is the main raw material for the blast furnace ironmaking method, is generally manufactured through a process as shown in FIG. The raw materials are iron ore powder, iron mill recovered powder, sintered ore sieve powder (returning), CaO-containing auxiliary raw materials such as limestone and dolomite, granulation aids such as quick lime, coke powder and anthracite. These raw materials are cut out from each of the hoppers 101 on a conveyor at a predetermined ratio. The cut out raw material is added with an appropriate amount of water using a drum mixer 102 and the like, mixed and granulated to obtain a sintered raw material which is a pseudo particle having an average diameter of 3.0 to 6.0 mm. On the other hand, the sized coarse ore is cut out from the floor hopper 104 to form a floor layer on the great of the sintering machine pallet 108.

  The sintering raw material is charged on the floor layer on the endless moving type sintering machine pallet 108 through the drum feeder 106 and the cutting chute 107 from the surge hopper 105 arranged on the sintering machine, and sintered. A charging layer 109 of a sintering raw material, which is also called a binding bed, is formed. The thickness (height) of the charging layer is usually around 400 to 800 mm. Thereafter, an ignition furnace 110 installed above the charging layer 109 ignites the carbonaceous material in the surface layer of the charging layer 9 and air through a wind box 111 disposed under the pallet 108. Is sucked downward to sequentially burn the carbonaceous material in the charging layer, and the sintered raw material is burned and melted by the combustion heat generated at this time to obtain a sintered cake. The sintered cake thus obtained is then crushed and sized, and recovered as a product sintered ore comprising agglomerates of 5.0 mm or more.

  In the manufacturing process, first, the ignition layer 110 is ignited by the ignition furnace 110. The ignited charcoal in the charging layer continues to be burned by the air sucked by the wind box 111 from the upper layer portion to the lower layer portion of the charging layer, and the combustion zone gradually moves to the lower layer as the pallet 108 moves. Proceed forward (downstream). As the combustion progresses, the moisture contained in the sintering raw material particles in the charging layer is vaporized by the heat generated by the combustion of the carbonaceous material, sucked downward, and the lower layer where the temperature has not yet risen. Concentrate in the sintering raw material to form a wet zone. If the moisture concentration exceeds a certain level, moisture fills the gaps between the raw material particles, which are the flow paths of the suction gas, and the ventilation resistance is increased. Note that the melted portion necessary for the sintering reaction that occurs in the combustion zone is also a factor that increases the ventilation resistance.

The production amount (t / hr) of the sintering machine is generally determined by the sintering production rate (t / hr · m ² ) × sintering machine area (m ² ). That is, the production volume of the sintering machine includes the machine width and length of the sintering machine, the thickness of the raw material deposition layer (charge layer thickness), the bulk density of the sintering raw material, the sintering (combustion) time, the yield, etc. It depends on. In order to increase the production of sintered ore, the air permeability (pressure loss) of the charging layer is improved to shorten the sintering time, or the cold strength of the sintered cake before crushing is increased. It is considered effective to improve the retention.

FIG. 39 shows the inside of the charging layer when the combustion (flame) front moving through the charging layer having a thickness of 600 mm is at a position of about 400 mm (200 mm from the surface of the charging layer) on the pallet of the charging layer. This shows the pressure loss and temperature distribution. The pressure loss distribution at this time is about 60% in the wet zone and about 40% in the combustion / melt zone.
FIG. 40 shows the temperature distribution in the charging layer at the time of high production and low production of sintered ore. The time during which the raw material particles begin to melt at a temperature of 1200 ° C. or higher (hereinafter referred to as “high temperature region holding time”) is t _{1 in} the case of low production, and in the case of high production with an emphasis on productivity. It is represented by t _2. In the case of high production, in order to increase the moving speed of the pallet, the high temperature region holding time t ₂ becomes shorter than t _{1 in the} case of low production. When the high temperature region holding time is shortened, firing becomes insufficient, resulting in a decrease in the cold strength of the sintered ore and a decrease in yield. Therefore, in order to increase the production amount of high-strength sintered ore, the yield strength is maintained and improved by increasing the strength of the sintered cake, that is, the cold strength of the sintered ore, even in the short-time sintering. It is necessary to take some measures that can be done. In general, SI (shutter index) and TI (tumbler index) are used as indices representing the cold strength of sintered ore.

  41 (a) shows the progress of sintering in the charging layer on the sintering machine pallet, FIG. 41 (b) shows the temperature distribution (heat pattern) in the sintering process in the charging layer, and FIG. 41 (c). ) Shows the yield distribution of the sintered cake. As can be seen from FIG. 41 (b), the temperature of the upper portion of the charging layer is less likely to rise than the lower layer portion, and the high temperature region holding time is also shortened. Therefore, in the upper part of the charging layer, the combustion melting reaction (sintering reaction) becomes insufficient, and the strength of the sintered cake becomes low. Therefore, as shown in FIG. It is a factor that causes a decline in

  In view of these problems, a method for imparting high temperature retention to the upper portion of the charging layer has been conventionally proposed. For example, Patent Document 1 discloses a technique for injecting gaseous fuel onto a charging layer after ignition of the charging layer. However, although the kind of gaseous fuel (flammable gas) is unknown in the above technique, even if it is propane gas (LPG) or natural gas (LNG), a high concentration gas is used. Moreover, since the amount of the carbon material is not reduced when the combustible gas is blown, the inside of the sintered layer becomes a high temperature exceeding 1380 ° C. For this reason, this technique has not been able to enjoy sufficient cold strength improvement and yield improvement effects. Moreover, when inflammable gas is injected immediately after the ignition furnace, there is a high risk of fire in the upper space of the sintering bed due to combustion of the combustible gas, and this is a technology that is not realistic and has not yet been put into practical use. .

  Patent Document 2 also discloses a technique of adding a combustible gas to the air sucked into the charging layer after the charging layer is ignited. It is said that about 1 to 10 minutes of supply after ignition is preferable, but the surface layer portion immediately after ignition in the ignition furnace has red-hot sintered ore remaining, and depending on the supply method, combustible gas There is a high risk of fire due to combustion, and there are few specific descriptions, but there is no effect even if combustible gas is burned in a sintered sintered zone. Since the air permeability is deteriorated due to thermal expansion, the productivity tends to be reduced, so that it has not been put into practical use.

Further, even in this technique, the amount of carbon material is not reduced when the combustible gas is blown, so that the inside of the sintered layer becomes a high temperature exceeding 1380 ° C. Therefore, it is not possible to enjoy a sufficient improvement in cold strength and a yield improvement effect. Furthermore, even if the obtained sintered ore is a sintered ore with poor reducibility.
In Patent Document 3, a hood is disposed on the charging layer in order to make the inside of the charging layer of the sintering raw material high temperature, and a mixed gas with air and coke oven gas is passed through the hood immediately after the ignition furnace. It is disclosed to blow in position. However, this technique also has a high temperature exceeding 1380 ° C. in the combustion melting zone in the sintered layer, so that the effect of coke oven gas blowing cannot be enjoyed, and the combustible mixed gas is ignited in the upper space of the sintering bed. There is a risk of fire and is not put into practical use.

  Further, Patent Document 4 discloses a method in which a low-melting-point solvent, a carbon material, and a combustible gas are simultaneously blown at a position immediately after the ignition furnace. However, this method also has a high risk of fire in the upper space of the sintering bed because the flammable gas is blown in a state where a flame remains on the surface, and the width of the sintering zone cannot be made sufficiently thick (approximately (Less than 15 mm), the effect of inflammable gas blowing cannot be fully exhibited. In addition, since there are many low-melting solvents, excessive melting phenomenon is caused in the upper layer portion, and the pores that become air flow paths are blocked, resulting in deterioration of air permeability and reduction of productivity. This technology has not been put into practical use until now.

As described above, none of the conventional techniques proposed so far has been put into practical use, and the development of a combustible gas blowing technique that can be implemented has been eagerly desired.
As a technique for solving the above-mentioned problems, in the patent document 5, the applicant of the present invention uses various gaseous fuels diluted below the lower combustion limit concentration from above the charging layer of the sintered raw material deposited on the pallet of the sintering machine. A method is proposed in which either one or both of the maximum attained temperature and the high temperature region holding time in the charging layer are adjusted by supplying, introducing into the charging layer, and burning. Further, as a technique with further improvements, in Patent Documents 6 and 7, gaseous fuel is supplied to the atmosphere on the charging layer of the sintering raw material and diluted to below the lower combustion limit concentration on the charging layer. Has proposed a way to supply.

Japanese Patent Laid-Open No. 48-18102 Japanese Patent Publication No.46-27126 JP-A-55-18585 Japanese Patent Laid-Open No. 5-311257 WO2007-052776 JP 2008-291354 A JP 2008-292153 A

  The technique of the above-mentioned patent document 5 is a downward suction type sintering machine that supplies (introduces) gaseous fuel diluted to a predetermined concentration into the charging layer and burns it at a target position in the charging layer. By supplying it, it is possible to appropriately control the maximum temperature reached during combustion of the sintered raw material and the holding time in the high temperature range, and as a result, the cold layer strength of the sintered ore tends to be low due to insufficient heat. Operation which raises the sinter intensity | strength not only in a part but in the arbitrary parts below a charging layer middle layer part can be performed.

  However, when performing the above gas fuel supply sintering operation, there is a risk that the high temperature part such as the cracked part of the sintering bed or the sintered cake will become a fire, and the gas fuel will be backfired and the gas fuel may burn (ignition). . If the sintering operation is continued in such a flammable state (aside from the explosion problem), not only the gaseous fuel cannot be supplied into the charging layer, but also the oxygen-deficient atmosphere in which oxygen is consumed by the combustion of the gaseous fuel. Is supplied (introduced) into the charging layer. As a result, not only can the maximum temperature and high temperature range holding time during combustion not be controlled, but also a lack of combustion, resulting in a decrease in strength of the sintered ore and a decrease in yield and productivity. It will have a serious adverse effect. In the techniques of Patent Documents 6 and 7, the problem of explosion is avoided, but there is still room for improvement.

Therefore, the present invention has been made paying attention to the problems of the conventional example described above, and in a downward suction type sintering machine, a high-strength, high-quality sintered ore can be produced with high yield and safety. , and its object is to provide a sintering machine that is capable of further reducing the C0 ₂ generated in the sintering step.

  In order to achieve the above object, a sintering machine according to claim 1 of the present invention comprises a pallet that circulates and a sintered raw material that includes fine ore and carbonaceous material on the pallet to form a charging layer. A raw material supply device to be formed, an ignition furnace for igniting the carbonaceous material of the charging layer, a wind box disposed below the pallet, and the charging disposed on the downstream side of the ignition furnace A hood that surrounds the upper part of the layer, a gaseous fuel supply device that injects gaseous fuel above the charging layer in the hood, mixes with air, and supplies it as a diluted gaseous fuel to the charging layer, and product sintering An FeO measuring device for measuring the FeO ratio in the ore, and using the FeO ratio measured by the FeO measuring apparatus as a management index for achieving a predetermined cold strength, and using the target value of the FeO ratio as the gaseous fuel supply device If you do not equip It is characterized by performing operations to control between strength.

According to a second aspect of the present invention, there is provided the sintering machine according to the first aspect, wherein the gaseous fuel supply device jets the gaseous fuel at a flow velocity at which a blow-off phenomenon occurs from the ejection port.
The sintering machine according to claim 3 is characterized in that, in the invention according to claim 2, the flow velocity at which the blow-off phenomenon occurs is a velocity exceeding the combustion rate of the gaseous fuel.

According to a fourth aspect of the present invention, there is provided the sintering machine according to the second or third aspect, wherein the gaseous fuel supply device ejects the gaseous fuel from an ejection port having an opening diameter of less than 3 mmφ.
The sintering machine according to claim 5 is the invention according to any one of 2 to 4, wherein the gaseous fuel supply device ejects gaseous fuel from an ejection port having an opening diameter of 0.8 to 1.5 mmφ. It is characterized by letting.

The sintering machine according to a sixth aspect is the invention according to any one of the first to fifth aspects, wherein the gaseous fuel supply device controls at least one of a high temperature region holding time and a maximum attained temperature in the charging layer. It is characterized by being configured.
A sintering machine according to a seventh aspect is the invention according to any one of the first to sixth aspects, wherein the gaseous fuel supply device is configured to adjust at least one of a supply amount and a concentration of a diluted gaseous fuel. It is a process for controlling the high temperature region holding time in the layer.

According to an eighth aspect of the present invention, there is provided the sintering machine according to any one of the first to seventh aspects, wherein the gaseous fuel supply device is configured by adjusting at least one of a supply amount and a concentration of the diluted gaseous fuel. It is characterized by being configured to control the maximum reached temperature in the in-layer to a range of 1200 to 1380 ° C.
A sintering machine according to a ninth aspect is the invention according to any one of the first to eighth aspects, wherein the gaseous fuel supply device receives at least a part of the diluted gaseous fuel introduced from above the charging layer. Control is performed so as to reach the combustion / melting zone in the charging layer without being burned.

A sintering machine according to a tenth aspect is the invention according to any one of the first to ninth aspects, wherein the gaseous fuel supply device supplies the diluted gaseous fuel introduced from above the charging layer to the charging layer. It is characterized by controlling the form of the combustion / melting zone in the charging layer.
A sintering machine according to an eleventh aspect is the invention according to any one of the first to tenth aspects, wherein the gaseous fuel supply device introduces the diluted gaseous fuel into the charging layer. It is characterized in that it is carried out after the sintered cake is formed on the surface layer portion until the sintering is completed.

A sintering machine according to a twelfth aspect is the invention according to any one of the first to eleventh aspects, wherein the gaseous fuel supply device is configured to combust and melt the introduction of the diluted gaseous fuel into the charging layer. It is characterized in that it is performed in a region where the thickness of the band is 15 mm or more.
A sintering machine according to claim 13 is the invention according to any one of claims 1 to 12, wherein the gaseous fuel is blast furnace gas, coke oven gas, blast furnace / coke oven mixed gas, city gas, natural gas, It is any one combustible gas selected from gas, methane gas, ethane gas, propane gas, and mixed gas thereof.

According to the present invention, in the operation of the downward suction type sintering machine, the charging layer is formed by the gaseous fuel supply device in the hood surrounding the upper portion of the charging layer formed on the pallet that is circulated by the gaseous fuel supply device. By injecting gaseous fuel from the upper side of the gas and supplying it to the charging layer as diluted gaseous fuel mixed with air, the Feo ratio in the sintered product ore is reduced compared to the case where no gaseous fuel supply device is provided. The cold strength is controlled with the low Feo ratio as a target value. For this reason, since the measurement of Feo can be performed more quickly and easily than the measurement of the cold strength, the control accuracy of the cold strength can be improved, and the basic unit of the coagulation material such as powder coke can be reduced. The effect that the amount of CO ₂ emission in the sintering process can be reduced is obtained.

It is a schematic structure figure showing one embodiment of the present invention. It is a block diagram of a sintering machine, (a) is a top view, (b) is a side view. It is a perspective view which shows schematic structure of a gaseous fuel supply apparatus. It is a typical cross section of the width direction of the sintering machine pallet of a gaseous fuel supply apparatus. It is sectional drawing similar to concrete FIG. 4 of a gaseous fuel supply apparatus. It is sectional drawing of the conveyance direction of the sintering machine pallet of FIG. It is an expanded sectional view showing a gaseous fuel injection nozzle. It is explanatory drawing which shows the gaseous fuel injection state of a gaseous fuel supply apparatus. It is a figure explaining the experiment which investigates the influence of the gaseous fuel supply position to a sintering cake. It is a photograph of an experimental device for examining the ejection speed at which the blow-out phenomenon occurs. It is a photograph which shows the blow-off phenomenon investigation result when the opening diameter of a jet nozzle is 1 mmφ. It is a graph which shows the relationship between nozzle thickness and nozzle flow velocity. It is a photograph of the experimental apparatus which investigates the influence of the pressure loss in long piping. It is a figure explaining the conditions which simulate the dilution situation of gaseous fuel when gaseous fuel is ejected in a horizontal direction. It is a figure which shows the result of having simulated the dilution condition when LNG is jetted in the horizontal direction at 200 m / s from the jet nozzle with an opening diameter of 1 mmφ. It is a figure which shows the result of having simulated the dilution condition when LNG is jetted in a horizontal direction at 200 m / s from the jet nozzle whose opening diameter is 1 mmφ. It is a figure explaining the method of calculating | requiring the combustion limit of blast furnace gas. It is a graph which shows the temperature dependence of the combustion minimum density | concentration of methane gas. It is a figure explaining the relationship between the combustion component (combustion gas) density | concentration and temperature of gaseous fuel in the normal temperature in air | atmosphere. It is a figure explaining a sintering reaction. It is explanatory drawing which shows the property of the calcium ferrite in a sintering reaction. It is explanatory drawing which shows the sintered ore quality requested | required from a blast furnace. It is explanatory drawing which shows the sinter quality suitable for the operation of the low reducing material ratio of a blast furnace. It is explanatory drawing which shows specifically the sintered ore quality requested | required from a blast furnace. Skeletal secondary hematite. It is a state diagram explaining the process to produce | generate. It is explanatory drawing which shows the change of the mineral structure in a sintering process. Is a diagram for explaining a reducing CO ₂ emissions in ironmaking process. It is a characteristic diagram which shows the relationship between Feo in sintered ore when not using a gaseous fuel supply apparatus, shutter intensity | strength, reducibility (JIS-RI), and reduction | restoration powdering index | exponent (JIS-RDI). It is explanatory drawing which shows the temperature change in a sintered layer by gaseous fuel blowing. It is the figure (photograph) which observed the form of the combustion zone with the case where there is no dilution city gas blowing and with it. It is the figure (photograph) which observed the form of the combustion zone when there is no gaseous fuel blowing and when propane gas, C gas, and city gas were blown. It is a characteristic diagram which shows the relationship between Feo in the sintered ore by this invention, shutter intensity | strength, reducibility (JIS-RI), and a reduction | restoration powdering index (JIS-RDI). It is a schematic diagram which shows the gaseous fuel supply control system to a gaseous fuel supply apparatus. It is a flowchart which shows an example of the gaseous fuel supply control processing procedure performed with a control apparatus. It is a graph which shows the change of the production amount of the state which was not blown in LNG, and the blown state, sintered ore intensity | strength, an aggregate unit, and a reducibility. It is a graph which shows the change of the powder rate at the time of the production amount of a state in which LNG is not blown, and the blown state, a powder coke basic unit, and sintering-blast furnace transportation. It is a graph which shows the change of the sintered ore cold intensity | strength of the state which is not blown in LNG, and the blown state, reducibility (JIS-RI), and reduction | restoration powdering property (JIS-RDI). It is a figure explaining the conventional sintering process. It is a figure explaining the pressure loss and temperature distribution in a sintered layer. It is explanatory drawing which compared the temperature distribution at the time of high production and low production. It is a graph of the temperature distribution and yield distribution in a sintering machine.

Hereinafter, an embodiment of the present invention will be described with reference to the drawings.
FIG. 1 is a schematic configuration diagram showing a sintering machine according to the present invention, in which a hopper 1a for storing iron ore powder, a hopper 1b for storing CaO-based auxiliary raw materials such as limestone and dolomite, recovered powder in an ironworks, return ore ( A raw material supply unit 1 having a hopper 1c for storing sinter ore powder and a hopper 1d for storing powdered coke or anthracite. Each raw material cut out from each hopper 1a to 1d of the raw material supply unit 1 is a pseudo particle having an average diameter of 3.0 to 6.0 mm, which is granulated by mixing an appropriate amount of water with the drum mixer 2. The sintered raw material is stored in the surge hopper 5 of the sintering machine 3, and the fine-grained sintered ore is stored in the floor hopper 4.

  The sintering machine 3 has an endless moving type sintering machine pallet 8 disposed below the floor hopper 4 and the surge hopper 5, and the flooring hopper 4 is moved along with the movement of the sintering machine pallet 8. A fine-grained sintered ore is cut out from the sinter to form a floor layer on the great of the sintering machine pallet 8, and a sintering raw material is loaded on the floor layer using a drum feeder and a cutting chute from the surge hopper 5. Then, a charging layer 9 having a thickness (height) of about 400 to 800 mm, which is also called a sintered bed, is formed.

An ignition furnace 11 is disposed on the downstream side of the surge hopper 5 above the charging layer 9, and the carbon material in the surface layer of the charging layer 9 is ignited by the ignition furnace 11. The ignition furnace 11 is supplied with a coke oven gas called a so-called C gas generated in a coke oven in an ironworks. By burning this coke oven gas, charcoal in the surface layer of the charging layer 9 is supplied. Ignite the material.
On the downstream side of the ignition furnace 11, for example, four gaseous fuel supply devices 12 a to 12 c are arranged adjacent to each other in series in the conveying direction of the sintering machine pallet 8.

  Then, the sintered cake formed by the sintering machine 3 is pulverized by the pulverizer 61 and then cooled by the sinter cooler 62, and then the product sintered ore composed of agglomerates of 5.0 mm or more by the sieve 63. Is supplied to the blast furnace 64, and a return ore made of agglomerates of less than 5.0 mm is supplied to the return hopper 1c.

  As shown in FIG. 2, each of the gaseous fuel supply devices 12 a to 12 d is arranged at a position on the downstream side of the ignition furnace 11 and in the pallet traveling direction in the process in which the combustion / melting zone proceeds in the charging layer 9. It is preferable that two or more gas fuels are supplied to the charging layer 9 at a position after ignition of the carbon material in the charging layer 9. The gaseous fuel supply devices 12a to 12c are arranged on the downstream side of the ignition furnace 11 at one or a plurality of arbitrary positions after the combustion front advances below the surface layer. From the viewpoint of adjusting the cold strength and reducibility of the ore, the size, position, and number of arrangement are determined as described later.

  Specifically, as shown in FIGS. 2 (a) and 2 (b), the sintering machine 3 is located at the left end position where the sintering machine pallet 8 is folded back from the lower stage side to the upper stage side to the floor hopper 4 and the downstream side thereof. A feeding section 14 as a sintering raw material supply device having a surge hopper 5 arranged is formed, and in this feeding section 14, fine-grained sintered ore cut out from the floor hopper 4 is sinter pallet. A floor layer is formed by laying down on the Great of No. 8, and a sintering raw material quantitatively cut out from the surge hopper 4 is charged on the floor layer to form a charging layer (sintering bed) 9 having a predetermined thickness. It is formed.

  An ignition furnace 11 is disposed opposite to the upper surface of the charging layer 9 on the downstream side of the supply section 14, and the gaseous fuel supply devices 12 a to 12 d are similarly installed adjacent to the downstream side of the ignition furnace 11. An ore discharge portion 15 for discharging the sintered cake generated on the sintering machine pallet 8 is formed on the most downstream side of the sintering machine pallet 8 and continuously disposed opposite to the upper surface of the bed 9. ing. The sintering machine pallet 8 is turned back at the discharge unit 15 and heads toward the supply unit 14.

  Here, between the feed section 14 and the discharge section 15 between the upper and lower sintering machine pallets 8, an ignition furnace is applied to the carbon material of the surface layer portion of the charging layer 9 formed on the upper sintering machine pallet 8. Above the sintering machine pallet 8 for sequentially moving the combustion / melting zone of the charging layer 9 formed by igniting at 11 to the lower layer side of the charging layer 9 as the sintering machine pallet 8 moves. A wind box 16 for sucking air through the charging layer 9 is disposed. The wind box 16 is connected to a dry electrostatic precipitator 18 via a main exhaust duct 17, and a main wind exhaust device 19 is connected to the exit side of the electric precipitator 18. The exhaust air output from the main exhaust device 19 is dissipated from the chimney 20 to the atmosphere.

Each of the gaseous fuel supply devices 12a to 12d is schematically shown in FIGS. 3 and 4, and the fuel supply unit surrounding hood 21 having an open upper end surrounding the upper portion of the sintering machine pallet 8 is provided. It is surrounded by.
The fuel supply unit surrounding hood 21 includes front and rear walls 21a in the conveying direction of the sintering machine pallet 8, and left and right walls 21b along the conveying direction of the sintering machine pallet 8 that connect the left and right ends of the front and rear walls 21a. The surrounding part 21c formed in the shape of a rectangular frame with the upper and lower ends open, and the transmittance disposed at the upper ends of the front and rear walls 21a and the left and right walls 21b constituting the surrounding part 21c are 25% or more and 55% or less. For example, it is comprised with the scattering prevention fence 21d comprised with the punch metal set to 45%.

In the surrounding portion 21 c, a straight plate-shaped rectifying plate 22 extending along the conveying direction of the sintering machine pallet 8 and having the top portion upward is provided with a predetermined pitch in the width direction orthogonal to the conveying direction of the sintering machine pallet 8. For example, three rows of rectifying plate rows 22a to 22c are arranged in the vertical direction having a configuration in which a predetermined number of them are arranged in parallel.
These rectifying plate rows 22a to 22c are arranged between the rectifying plate rows 22a and 22b adjacent in the vertical direction and between 22b and 22c, and the rectifying plate 22 of the other rectifying plate row is positioned between the rectifying plates 22 of one rectifying plate row. It is arranged in a staggered manner.

Therefore, by the rectifying plate rows 22a to 22c, the air passing between the sucked rectifying plate rows 22a to 22c and the gaseous fuel supplied from the gaseous fuel supply devices 12a to 12d can be mixed to dilute the gaseous fuel. At the same time, it has a function of preventing the diluted diluted gas fuel from leaking to the outside.
As shown in FIGS. 5 and 6, the specific configuration of the fuel supply unit surrounding hood 21 is such that the outer hood portion 25 is attached to the support beam 24 disposed between the columns 23 suspended outside the sintering machine pallet 8. The inner hood portion 26 is supported inside the outer hood portion 25 so as to be relatively movable up and down by a relative movement mechanism 27.

  As described above, the fuel supply unit surrounding hood 21 includes a surrounding portion 21c formed in a rectangular frame shape by the front and rear walls 21a and the left and right walls 21b, and a rectangular frame-shaped scattering prevention fence formed at the upper end of the surrounding portion 21c. The outer hood portion 25 is fixedly arranged on the support beam 23 as described above.

  On the other hand, the rectifying plate 22 disposed in the fuel supply unit surrounding hood 21, that is, the rectifying plate rows 122 a to 22 c are supported by the inner hood portion 26. The inner hood portion 26 extends downward along the inside of the front and rear walls 21a of the outer hood portion 25 that is fixed to the front and rear frame portions 26b of the support frame 26a. A predetermined number of, for example, four vertical support plate portions 26c extending to a position above the charging layer (sinter bed) on the sintering machine pallet 8, and a plurality of stages at the lower end position of these vertical support plate portions 26c, For example, it is composed of three horizontal support plate portions 26d. Between the horizontal support plate portions 26d, the above-mentioned equilateral mountain-shaped rectifying plates 22 are arranged in parallel in a width direction orthogonal to the conveying direction of the sintering machine pallet 8 at a predetermined pitch P (for example, 400 mm). Three rectifying plate rows 22a to 22c are arranged in the direction. That is, the rectifying plate rows 22 a to 22 c are supported by the horizontal support plate portion 26 d and are suspended from the inner hood portion 26.

  Here, it is preferable that the width W of the rectifying plates 22 in the rectifying plate rows 22a to 22c is set to be twice or more the horizontal interval Lh as seen in FIG. Specifically, the width W of the mountain-shaped rectifying plate 17 is 100 mm or more, and the horizontal and vertical intervals Lh and Lv of the rectifying plate 22 are 50 mm or more, desirably 100 mm or more. Thus, by setting the size of the rectifying plate 22, it is possible to reduce the ventilation resistance due to the formation of the boundary layer on the surface of the rectifying plate 22.

Further, the vertical arrangement of the current plate 22 is preferably arranged in a tournament shape (staggered shape) or a labyrinth shape in multiple stages. With such an arrangement structure, the flow velocity of the sucked air is averaged, and the formation of vortex flow due to the entrainment of air can be suppressed. However, if the number of steps in the vertical direction of the rectifying plate 22 is increased too much, the pressure loss at the opening increases, and the load on the wind box 16 that sucks air under the sintering machine pallet 8 increases, and the suction air Since the amount is reduced, it may interfere with the sintering operation. Therefore, it is preferable to control the pressure loss due to the installation of the rectifying plate rows 22a to 22c in the opening to 10 mmH ₂ O or less. For this reason, in this example, the rectifying plates 22 installed inside the openings are arranged such that the rectifying plates 22 having a width W = 300 mm are arranged with a horizontal interval Lh = 100 mm, and further with a vertical interval Lv = 70 mm. It is arranged in three stages and in a tournament form. Further, below the charging layer 9, air is sucked by the wind box 16 at a suction speed of about 0.9 m / s.

  Incidentally, when the rectifying plate rows 22a to 22c are not installed, a vortex is formed in the gas supply unit surrounding hood 21, and as a result, the gas fuel injection nozzle 31 is provided below the rectifying plate row 22c as will be described later. Gas fuel is dissipated when placed and injected in the horizontal direction. On the other hand, when the rectifying plate rows 22a to 22c are installed as described above, although the pressure loss at the opening of the gas supply unit surrounding hood 21 is slightly increased, the formation of eddy currents in the hood 21 is also suppressed, and the lowermost stage A slight amount of gaseous fuel is recognized between the rectifying plate row 22c and the upper end thereof, but it is possible to create a state in which no gaseous fuel is present above the rectifying plate row 22c. As a result, the dissipation factor (0.1% or less) of gaseous fuel can also be reduced.

  Furthermore, in the present invention, the outer hood portion 25 and the inner hood 26 are relatively movable, and in this example, a relative movement mechanism 27 that allows the inner hood 26 to move is provided. As shown in FIG. 5, the relative movement mechanism 27 that moves the inner hood 26 is fixed to the left and right walls 21 b of the outer hood portion 27, and the cylinder tube 27 a is fixed and the piston rod 27 b protrudes upward, for example, two on the left and right. Each is composed of four hydraulic cylinders 27 c, and the tip of the piston rod 27 b is connected to the support frame 26 a of the inner hood portion 26. FIG. 6 shows an example in which a bracket 27d on which the cylinder tube 27a can be disposed is provided on the front and rear walls 21a side of the outer hood portion 25, and the relative movement mechanism 27 is disposed on the bracket 27d. The relative movement mechanism 27 may be on either the front / rear wall 21a side or the left / right wall 21b side. Furthermore, as long as the anti-scattering fence 21d is strong enough to support the inner hood 26, the relative movement mechanism 27 may be mounted on the anti-scattering fence 21d. A jack may be used instead of the hydraulic cylinder, and as the relative movement mechanism 27, a lifting device having a lifting function is sufficient.

  And the gaseous fuel supply mechanism 12i (i = ad) is arrange | positioned between the front-and-back walls 21a which comprise the base 21c of the outer side hood part 25. As shown in FIG. As shown in FIG. 5, the gaseous fuel supply mechanism 12i includes, for example, seven gaseous fuel injection nozzles 31 arranged in parallel with a predetermined pitch in the width direction along the conveying direction of the sintering machine pallet 8. The gaseous fuel supply nozzle 32 is configured to supply gaseous fuel to the gaseous fuel injection nozzles 31.

  As shown in FIG. 3 described above, the gaseous fuel injection nozzle 31 is a gaseous fuel that injects the gaseous fuel inward in the horizontal direction with respect to the gaseous fuel injection nozzles 31 at both ends in the width direction. For the remaining gaseous fuel injection nozzles 31, a predetermined number of gaseous fuels are horizontally disposed at a predetermined pitch in the conveying direction of the sintering machine pallet 8 at the symmetrical positions facing the adjacent gaseous fuel injection nozzles 31. A gas fuel injection port 31a for injecting the gas is provided. The gaseous fuel injected in the horizontal direction from the gaseous fuel outlet 31a diffuses into the atmosphere introduced through the outer hood portion 25 and becomes diluted gaseous fuel diluted to a predetermined concentration, and the charging layer (sintered) Bed) 9 is sucked. In addition to the horizontal direction, the injection direction may be downward or obliquely upward. The injected gaseous fuel quickly becomes a diluted gaseous fuel that is diffused and diluted in the atmosphere.

  Further, as shown in FIGS. 6 and 7, each gaseous fuel injection nozzle 31 includes a nozzle receiving member 34 formed of a hollow round bar disposed between the front and rear walls 21 a, and a lower portion of the nozzle receiving member 33. Before and after supporting the gaseous fuel injection nozzle 31 mounted at a predetermined interval in the front-rear direction on the nozzle deflection preventing chilled structure 35 disposed on the support plate 36 disposed on the bottom surface of the chilled structure 35. It is supported by a nozzle receiving structure composed of a support material 37. Thus, by supporting the gaseous fuel injection nozzle 31 with the lattice structure 35, the sectional modulus in the vertical direction can be improved, and the bending of the gaseous fuel injection nozzle 31 can be prevented.

  And between the adjacent gaseous fuel injection nozzles 31, as shown in FIG. 8, the gaseous fuel injection port 31 a of one gaseous fuel injection nozzle 31 is in the middle position between the gaseous fuel injection ports 31 a of the other gaseous fuel injection nozzle 31. The gas fuel injection ports 31a are horizontally arranged between the adjacent gas fuel injection nozzles 31 in a staggered manner. For this reason, the gaseous fuels injected by the adjacent gaseous fuel injection nozzles 31 do not interfere with each other, are uniformly dispersed, injected onto the charging layer 9, and mixed with air to form the diluted gaseous fuel 38. Then, using the suction force of a wind box (not shown) under the sintering machine pallet 8, the sintered cake generated on the surface layer of the charging layer 9 is introduced to the deep part (lower layer) of the charging layer. The

  Further, as shown in FIGS. 5 and 6, the gas fuel supply unit 32 has a valve stand for supplying city gas and purge nitrogen gas as gas fuel supplied from the city gas supply main pipe 41 and the nitrogen gas supply main pipe 42. 43. Although detailed explanation is omitted, the valve stand 43 is provided with various instruments such as a pressure gauge and a flow meter, and a distribution unit that distributes the gaseous fuel to each gaseous fuel injection nozzle 31 and the distribution unit. An adjustment valve or the like for adjusting the flow rate and pressure of each distributed gaseous fuel is disposed, and the gaseous fuel with the adjusted pressure and flow rate output from the valve stand 43 is supplied to each gaseous fuel via the city gas branch pipe 44. It is supplied to the injection nozzle 31.

Thus, the gaseous fuel supply device 12i causes the gaseous fuel to be discharged into the atmosphere at a high speed above the charging layer 9, thereby mixing with the surrounding air in a short time, and the lower limit concentration of combustion of the gaseous fuel. It is necessary to dilute to the following concentration and then introduce the diluted gaseous fuel 38 into the charge bed.
As described above, the reason why the gaseous fuel is diluted to a concentration lower than the lower combustion limit concentration is as follows.

Table 1 shows the lower combustion limit concentration, supply concentration, and the like of typical gaseous fuels that can be used in the present invention. In order to prevent the occurrence of fire, the gas concentration when supplying gaseous fuel into the sintered raw material is safer as it is lower than the lower combustion limit concentration. That is, it is necessary for safety to supply the fuel so that it does not burn (cannot) at room temperature. In this respect, city gas has a lower combustion limit concentration that is similar to that of C gas (coke oven gas), but since the amount of heat is higher than that of C gas, the supply concentration can be lowered. Furthermore, since C gas is mainly composed of H ₂ , the flashback speed is much faster than that of city gas, which is dangerous compared to city gas. Therefore, from the viewpoint of ensuring safety, city gas capable of lowering the supply concentration and city gas having a low flashback rate are superior to C gas.

  Table 2 shows the combustion components (hydrogen, CO, methane) contained in the gaseous fuel, the lower and upper combustion concentrations of these components, laminar flow, combustion speed during turbulent flow, and the like. In order to prevent the occurrence of fire during sintering, that is, to prevent the occurrence of fire due to gaseous fuel supplied during sintering, it is necessary to prevent backfire, but for that purpose, at least laminar combustion The gaseous fuel may be discharged at a speed higher than the speed, preferably higher than the turbulent combustion speed. For example, when methane, which is a main combustion component of city gas, is used as a gaseous fuel, there is no fear of backfire if it is discharged at a speed exceeding 3.7 m / s.

  On the other hand, since hydrogen gas has a higher turbulent combustion speed than CO and methane, it is necessary to discharge hydrogen gas at a higher speed in order to ensure safety. From this point, when comparing the gaseous fuel shown in Table 1, the city gas that does not contain the hydrogen component can slow down the discharge speed compared to the C gas containing 59 vol% of the hydrogen component. Is advantageous.

  Moreover, since city gas does not contain a CO component, it is safe without causing gas poisoning. Therefore, from the viewpoint of ensuring safety, it can be said that city gas has favorable characteristics when used as gaseous fuel. C gas can also be used as a gaseous fuel, but has the above-mentioned problems and is difficult. In the present invention, these points are also solved.

  Table 3 shows the results of evaluating the advantages and disadvantages of the type of supplying the gaseous fuel. In the table, direct top blowing means that gas fuel such as city gas or C gas is supplied (discharged) as it is, and is diluted to a predetermined concentration by entraining the surrounding atmosphere and sucked into the charging layer (introduced) The premixed blowing is a so-called pre-mixing method in which air and gaseous fuel are mixed in advance and diluted to a predetermined concentration and supplied to the charging layer and sucked (introduced) into the charging layer. Refers to the mix format. In the direct injection type, it is easy to prevent backfire if gaseous fuel is discharged at a speed higher than the turbulent combustion rate described above, but in the premixed injection type, when a concentration deviation occurs, backfire is caused. there is a possibility. On the other hand, in the direct-injection type, when gaseous fuel is mixed with the surrounding atmosphere and diluted, uneven concentration tends to occur, so there is a possibility of causing uneven combustion in the charged layer compared to the premixed injection type. large. However, in the case of comprehensive evaluation including equipment costs, direct injection of city gas is the most advantageous.

  Further, in the present invention, the gaseous fuel is supplied to the gaseous fuel by the gaseous fuel supply device 12i above the charging layer 9 into the atmosphere at a high speed, thereby mixing with the surrounding air in a short time. The reason why it is necessary to dilute to a concentration below the lower combustion limit concentration and then introduce the diluted gaseous fuel into the charge layer is as follows.

  As shown in FIG. 9 (a), a sintered pan having an inner diameter of 300 mmφ × a height of 400 mm is filled with a sintered cake, and a nozzle is embedded at a position of 90 mm in depth from the center of the sintered cake, Table 4 shows the results of measuring the methane gas concentration in the circumferential direction and the depth direction in the sintered cake by blowing 100% methane gas to 1 vol% against air. On the other hand, as shown in FIG. 9B, the result of measuring the distribution of the methane gas concentration in the same manner as described above for the case where methane gas is supplied from a position 350 mm above the sintered cake using the same nozzle is shown. This is shown in FIG. From these results, when methane gas was directly introduced into the sintered cake, the lateral diffusion of methane gas was insufficient, whereas when methane gas was supplied above the sintered cake, It can be seen that the methane gas concentration in the cake is almost uniform and diffuses sufficiently in the lateral direction. From the above results, it is understood that the gaseous fuel is preferably diluted uniformly before being introduced into the charging layer by supplying it into the air above the sintered cake.

  Next, in the present invention, the speed at which the gaseous fuel is ejected from the outlet of the gaseous fuel supply pipe of the gaseous fuel supply apparatus, such as a slit or nozzle, needs to be discharged at a high speed from the viewpoint of preventing flashback. is there. That is, the gaseous fuel is diluted by the stage of being sucked and introduced into the surface layer of the charging layer and is below the lower limit of combustion concentration. In the sintering operation of the present invention, combustion and melting are performed in the sintering pallet. Gas fuel is supplied above the charging layer in a state where there is a sintered layer forming or forming a band and always has a fire type. Accordingly, when the gaseous fuel supplied from the gaseous fuel supply device 12i is ignited by some kind of fire, if the flow rate of the gaseous fuel discharged from the nozzle or the like is slow, a backfire occurs, and the gaseous fuel supply device 12i or the gaseous fuel supply There is a risk of explosion and combustion in the pipe. Therefore, in order to prevent backfire even if the gaseous fuel is ignited, the ejection speed of the gaseous fuel is discharged at a speed higher than the combustion speed of the gaseous fuel, more preferably at a speed higher than the turbulent combustion speed. Is considered desirable. Incidentally, the laminar combustion speed of methane gas is about 0.4 m / s, and the turbulent combustion speed is about 4 m / s.

Therefore, an experiment was conducted to confirm the conditions under which the blowout actually occurs at the above burning rate.
In this experiment, as shown in FIG. 10, a jet outlet having an opening diameter of 1 mmφ, 2 mmφ, and 3 mmφ is processed in a pipe of 25A, LNG gas is supplied to the pipe, and LNG gas is jetted from the jet outlet. The ejected LNG gas was ignited using an ignition source, and then the ejection speed at which blow-off occurred when the ignition source was separated was measured. Here, the ejection speed was controlled by changing the header pressure of the LNG gas.

As a result, when the opening diameter of the jet port is 1 mmφ, the header pressure of the LNG gas is 300 mmH ₂ O or more, the jet velocity of the gaseous fuel is 70 m / s or more, and when the opening diameter is 2 mmφ, It was found that blowout occurred when the header pressure was 550 mmH ₂ O or higher and the gas fuel injection speed was 130 m / s or higher. On the other hand, with an opening diameter of 3 mmφ, even if gaseous fuel is ejected at a speed exceeding the speed of sound by setting the header pressure of the LNG gas to 2000 mmH ₂ O, combustion of the gaseous fuel at the ejection outlet can be prevented, but the downstream low speed A so-called bonfire, which causes combustion in the part, occurred and could not be blown out reliably. As a reference, the experimental results when the opening diameter is 1 mmφ are shown in FIG.

  As described above, when using a LNG gas or a fuel gas having a burning rate equivalent to that of the LNG gas (for example, methane, ethane, propane gas, etc.), in order to prevent blowback and prevent backfire, at least open it. It was found that the aperture needs to be less than 3 mmφ. Moreover, even if the jet speed of the gaseous fuel is simply set to be equal to or higher than the combustion speed, combustion at the jet outlet cannot be prevented even though combustion at the jet outlet can be prevented. . Therefore, in the present invention, in order to prevent such a fire, the gaseous fuel is ejected from the ejection port at a speed higher than the speed at which the blow-off phenomenon occurs. In order to cause this blow-off phenomenon, it is necessary to jet the gaseous fuel at a high speed with the gas outlet being less than the opening diameter of 3 mmφ. For example, when the opening diameter is equivalent to 1 mmφ, 70 m / s As described above, it is preferable to eject at a high speed of 100 m / s or more when the opening diameter is equivalent to 1.5 mmφ, and 130 m / s or more when the opening diameter is 2 mmφ.

  A preferable opening diameter when the present invention is applied to an actual machine is in the range of 0.8 to 1.5 mmφ. If it is less than 0.8 mmφ, it is difficult to drill a hole in the pipe, and it is easy to cause clogging by dust contained in the gas. On the other hand, if it exceeds 1.5 mmφ, a relatively large ejection speed is required to cause blowout, and therefore it is preferable that the ejection speed be low in order to ensure safety.

  By the way, in the above description, the shape of the jet outlet is assumed to be a circle and the size is described by its diameter. However, the shape of the open jet outlet is not particularly limited to a circle as long as it has the same opening area. For example, an elliptical shape or a groove shape (slit) may be used.

In addition, since the ejection speed of the gaseous fuel changes depending on the supply pressure of the gaseous fuel in addition to the opening diameter, in order to secure the ejection speed at which the blowout occurs, the nozzle pressure and nozzle flow velocity (ejection Control may be performed based on the relationship of (speed). FIG. 12 shows the relationship between the nozzle pressure and the nozzle flow velocity, taking the case of jetting air as an example. If the gas density (ρ) of the gaseous fuel is substituted, the following formula:
ΔP = ρ · V ² / (2 · g)
Here, ΔP: Nozzle differential pressure (mmH ₂ O), ρ: Gaseous fuel density (kg / m ³ ) at 30 ° C., V: Nozzle flow velocity (m / s), g: Gravitational acceleration (m / s ² ) It is.
Can be used to determine the nozzle flow rate.

When LNG gas is ejected from a hole having an opening diameter of 1 mmφ, it is ejected at a speed of 70 m / s at 300 mmH ₂ O, and when ejected from a hole at 1.5 mmφ, it is ejected at a speed of 100 m / s at 700 mmH ₂ O. Yes, it can be blown out.

In addition, when the piping for discharging the gaseous fuel is long, it is generally expected that the jetting speed is higher as the gas fuel is closer to the supply source, and the jetting speed is lower as the distance from the supply source is longer. Therefore, as shown in the photograph of FIG. 13, 76 jet nozzles having an opening diameter of 1 mmφ are opened at a pitch of 160 mm, and a 6 m long pipe (25A) with a closed end is used, and air is supplied from one end of this pipe. Was supplied in a range of 0.1 to 1.00 kg / cm ² · G of the original pressure, and air was ejected from the ejection port, and the pressure change in the pipe length direction at this time was measured. The results of the experiment are shown in Table 6, but within the range of this experimental condition (pipe diameter, jet outlet), there is almost no difference between the original pressure and the pressure at the end of the pipe. I found out.

However, under conditions that deviate from the above experimental range, there is a possibility that the difference between the original pressure and the pressure at the end of the pipe becomes large. So, in such a case,
(A) Use a tapered pipe with a gradually reduced cross-sectional area in the pipe. (B) Increase the opening cross-sectional area as it is farther from the fuel supply header. (C) Opener and nozzle as it is farther from the fuel supply header. Narrow the pitch and increase the sum of openings or nozzle cross-sectional area per unit pipe length.
By applying any one of these, or applying them in combination, the fuel can be supplied evenly.

In addition, it is preferable to discharge gaseous fuel with the said gaseous fuel supply apparatus at the height of 300 mm or more above the charging layer surface. The reason is as follows.
As shown in FIG. 14, gas supply pipes having openings with a diameter of 1 mmφ opened at both sides of a pipe of 25A at a pitch of 112 mm on both sides of the pipe of 25A so that the jet direction of the gaseous fuel is horizontal, are sintered beds (charges). Is arranged in parallel with the pallet traveling direction at a distance of 400 mm at a position of 500 mm above the layer), and LNG is ejected from the above-mentioned jet outlet into the atmosphere at a speed of 200 m / s and mixed with the surrounding air. A simulation was conducted of the homogenization situation when the solution was diluted to a target concentration of 0.8%. The gas supply pipes were arranged so that the jet outlets of adjacent pipes were shifted by 56 mm from each other so that the ejected gaseous fuel did not collide. In addition, imitating an actual sintering machine, air was sucked downward at a suction speed of 0.9 m / s on the upper surface of the sintering bed.

  FIG. 15 shows a state in which LNG ejected at a speed of 200 m / s from a spout having an opening diameter of 1 mmφ is mixed with ambient air and diluted above the sintering bed. From this figure, it can be seen that the concentration of LNG ejected under the above conditions is about 100 mm from the jet outlet and diluted to 4.3%, which is the lower combustion limit concentration of LNG. It is understood that there is no possibility of causing combustion in theory.

  Further, FIG. 16 shows how LNG spouted from a spout having an opening diameter of 1 mmφ is diffused and diluted until reaching the surface of the sintering bed and in the sintering bed layer. It shows how to go. From this figure, under the above-mentioned ejection conditions, LNG is 0.28 to 1.14% at a position 200 mm above the sintering bed (300 mm below the ejection port), and 0 when reaching the sintering bed surface. It is diluted to 51 to 1.14%, further 0.69 to 0.87% by the middle of the sintered bed layer, and 0.75 to 0.00 by the bottom of the sintered bed. It turns out that it is diluted to 81%.

  From the above results, LNG is jetted into the air at a high speed above the sintering bed, so that it is sufficiently mixed with air and diluted uniformly, especially at the bottom of the jet 300 mm. I found out. Therefore, in the present invention, in consideration of this result and the rebound of the ejected gaseous fuel on the charged layer surface, the gaseous fuel is supplied to the atmosphere at a height of 300 mm or more above the charged layer surface. To do.

  In the present invention, the gaseous fuel supplied into the charging layer includes blast furnace gas (B gas), coke oven gas (C gas), mixed gas of blast furnace gas and coke oven gas (M gas), city gas, natural gas Either gas (LNG) or methane, ethane, propane, butane gas, or a mixed gas thereof can be used. In the present invention, any one of these gaseous fuels is discharged into the air at a high speed, mixed with air to form a diluted gaseous fuel, and supplied (introduced) into the charging layer.

  The diluted gaseous fuel is preferably a gaseous fuel in which the concentration of the combustible gas (combustion component) contained therein is diluted to 75% or less of the lower limit concentration of combustion at normal temperature in the atmosphere, and more preferably the lower limit of combustion. It is preferably diluted to a concentration of 60% or less of the concentration, more preferably 25% or less of the lower combustion limit concentration. There are two reasons for using the combustible gas diluted to 75% or less below the lower combustion limit concentration.

(A) The supply of a high concentration of combustible gas to the upper part of the charging layer may sometimes cause explosive combustion, and at least at room temperature, it is necessary to keep it from burning even if there is a fire type.
(B) Even if it reaches the electrostatic precipitator etc. downstream of the windbox without burning completely in the charge layer, it must not be burned by the discharge of the electrostatic precipitator. It is.

  Furthermore, the concentration of the diluted gas fuel causes a shortage of oxygen due to the consumption of oxygen due to the combustion of the diluted gas fuel, leading to a shortage of oxygen necessary for the combustion of the total fuel (solid fuel + gas fuel) contained in the sintering raw material. It must be diluted to such an extent that it does not cause However, the concentration of the diluted gas fuel is preferably 2% or more of the lower combustion limit concentration. This is because if the concentration is less than 2%, the amount of heat generated by combustion is insufficient, and the strength of the sintered ore and the yield cannot be improved.

In the sintering machine of the present invention, it is also possible to supply (introduce) diluted gaseous fuel into the charging layer immediately after igniting the carbonaceous material in the charging layer. Diluted gas fuel can be supplied by supplying gas fuel that causes blowout, so that sintering can be completed if a sintered cake layer is formed on the upper surface of the charging layer without fear of flashback. Can be performed at any position up to.
Another reason why the diluted gas fuel is preferably supplied after the sintered cake layer is formed on the surface of the charging layer is that the diluted gas fuel is supplied to the upper portion of the charging layer in a state where no sintered cake is formed. This is because only the combustion occurs on the charging layer. This is because it is preferable to supply the diluted gas fuel to a portion where it is necessary to improve the yield of the sintered ore, that is, to supply combustion to a portion where it is desired to increase the strength of the sintered ore. .

  In addition, in order to supply diluted gas fuel into the charged layer after ignition and control either or both of the highest attained temperature and the high temperature region holding time in the charged layer, the thickness of the combustion / melting zone must be at least It is preferable to supply the diluted gas fuel in a state where it is 15 mm or more, preferably 20 mm or more, more preferably 30 mm or more. When the thickness of the combustion / melting zone is less than 15 mm, the cooling effect by the air sucked through the sintered layer (sintered cake) and the diluted gas fuel makes the effect insufficient even if the gas fuel is burned, and combustion / melting. The band thickness cannot be increased. On the other hand, when the diluted gas fuel is supplied at a stage where the thickness of the combustion / melting zone is 15 mm or more, preferably 20 mm or more, more preferably 30 mm or more, the thickness of the combustion / melting zone is increased and the holding time of the high temperature region is extended. This is because it can be realized and a high-strength sintered ore can be obtained. The thickness of the combustion / melting zone can be confirmed using a vertical tubular test pan with a transparent quartz window, as will be described later. The sintering test using this test pan is an effective means for determining the supply position of the diluted gas fuel.

  In addition, the introduction of the diluted gas fuel into the charging layer is performed at a position where the combustion front is lowered below the surface layer and the combustion / melting zone is lowered from the surface layer by 50 mm or more, preferably 100 mm or more, more preferably 200 mm or more. It is preferable to carry out for the middle and lower layer regions of the layer. That is, the diluted gas fuel passes through the sintered cake region (sintered layer) generated in the surface layer of the charging layer without burning, and is supplied so as to be burned when the combustion front moves 50 mm or more from the surface layer. Is preferred. The reason is that if the combustion front is at a position lower than the surface layer by 50 mm or more, the adverse effect of cooling by air sucked through the sintered layer is reduced, and the thickness of the combustion / melting zone can be increased. This is because the thickness of the melting zone can be effectively expanded. In addition, since the gaseous fuel is ejected at a high speed at which the blow-off phenomenon occurs as described above, even if the gaseous fuel is supplied immediately after ignition in the ignition furnace, it can be realized without causing a backfire.

For the above reasons, the gaseous fuel supply device that generates the diluted gaseous fuel varies depending on the size of the sintering machine. For example, the gaseous fuel supply amount is 1000 to 5000 m ³ (standard) / hr, and the production amount is about 1.times. In a sintering machine having a scale of 50,000 t / day and a length of 90 m, it is preferable to arrange the sintering machine immediately after the ignition furnace exit side or at a position on the downstream side about 5 m or later.

  As described above, in the sintering machine according to the present invention, the dilution gas fuel supply position (introduction position to the charging layer) is the so-called combustion after the sintered cake is formed downstream of the ignition furnace in the pallet moving direction. It is preferable to carry out at one or more arbitrary positions between the position where the front line has progressed under the surface layer and the completion of sintering. This means that the introduction of the gaseous fuel starts when the combustion front moves below the surface of the charging layer, and therefore the combustion of the gaseous fuel takes place inside the charging layer and gradually moves to the lower layer. Therefore, it means that there is no risk of explosion and safe sintering operation becomes possible.

  Moreover, in the manufacturing method of the sintered ore in this invention, introduction | transduction of the diluted gas fuel in a charging layer means that reheating of the produced | generated sintered cake is accelerated | stimulated. That is, the supply of the diluted gaseous fuel is originally a gas fuel that is more reactive than solid fuel for the portion where the cold strength of the sintered ore tends to be low due to the short holding time in the high temperature range. It is because it plays a role of replenishing the combustion / melting zone to compensate for the shortage of combustion heat by supplying.

  Further, in the method for producing sintered ore according to the present invention, the supply of the diluted gas fuel from the upper part of the charging layer is caused to reach the combustion / melting zone with the diluted gas fuel introduced into the charging layer unburned. Therefore, it is preferable to compensate for the heat of combustion by burning the fuel there. This is because the supply (introduction) of diluted gas fuel into the charging layer is considered to be more effective not only in the upper part of the charging layer but also in the combustion / melting zone in the central part in the thickness direction. . In other words, if the supply of gaseous fuel is carried out in the upper layer of the charging layer, which tends to be short of heat (insufficient holding time in the high temperature region), sufficient combustion heat is provided to this part, so the quality of the sintered cake is improved. Can be achieved. Furthermore, if the effect of the diluted gas fuel is extended to the zone below the middle layer, it is equivalent to forming the combustion / melting zone by the diluted gas fuel on the combustion / melting zone formed by the original carbon material. As a result, the combustion / melting zone is widened in the vertical direction, and the holding time in the high temperature range can be extended without increasing the maximum temperature, so that sufficient calcination can be achieved without reducing the pallet movement speed. A result can be obtained. As a result, the quality is improved over the entire charged layer (improving cold strength), so that it is possible to improve the yield and productivity of the product sintered ore.

  Further, according to the present invention, the supply position of the diluted gaseous fuel is determined from the viewpoint of where in the charging layer the action / effect of the gaseous fuel supply is exerted. In addition, by supplying gaseous fuel, the maximum temperature reached and the high temperature region holding time in the charging layer are controlled according to the amount of solid fuel under a constant amount of heat. Accordingly, in the present invention, when the diluted gas fuel is introduced (supplied) into the charging layer, not only the supply position is adjusted, but also the form of the combustion / melting zone itself is controlled, and the combustion / melting zone is controlled. It is preferable to control at least one of the maximum attained temperature and the high temperature region holding time in.

  Generally, in the charged layer after ignition, the combustion (flame) front gradually expands forward (downstream) and downward as the pallet moves, so the position of the combustion / melting zone is as shown in FIG. It changes as shown in a). And as shown in FIG. 41 (b), the thermal history of the sintered layer upper layer, middle layer, and lower layer received during the sintering process is greatly different, and therefore, the upper layer to the lower layer have a high temperature region holding time (about 1200 ° C. or more). Time) is also very different. As a result, the yield according to position of the sintered ore in the pallet shows a distribution as shown in FIG. That is, the yield of the surface layer portion (upper layer portion) is low, and the yield is high in the middle layer and lower layer portions. Therefore, when the gaseous fuel is supplied according to the present invention, the vertical thickness of the combustion / melting zone and the width in the pallet traveling direction are expanded, which leads to improvement in quality of the product sintered ore. Further, since the middle layer portion and the lower layer portion having a high yield distribution can further control (extend) the high temperature region holding time, the yield is further improved.

  As described above, in the present invention, by adjusting the supply (introduction) position of the gaseous fuel, the form of the combustion / melting zone, that is, the thickness in the height direction of the combustion / melting zone and the width in the pallet moving direction are adjusted. At least one of them can be controlled, and the maximum temperature reached and the high temperature region holding time can be controlled. And through these controls, sufficient firing can always be achieved, and as a result, the cold strength of the product sintered ore can be increased and quality can be improved.

  In addition, it can be said that the supply (introduction) of the diluted gas fuel into the charging layer in the present invention is for controlling the strength of the entire product sintered ore. In other words, in the present invention, the original purpose of supplying the diluted gaseous fuel is to improve the cold strength of the sintered cake (sintered ore). The cold strength (shutter index SI) of the sintered ore is about 75 to 85%, preferably 80% through the control of the high temperature range holding time during which the raw material stays in the combustion / melting zone and the control of the maximum temperature. More preferably, it is 90% or more. In general, the cold strength (SI value) of the sintered ore produced by the actual sintering machine is 10 to 15% higher than the value obtained by the pan test.

  According to the present invention, this strength level is determined according to the concentration, supply amount, supply position, and supply range of the diluted gas fuel, preferably taking into account the amount of carbonaceous material in the sintered raw material (the amount of heat input is kept constant). Can be achieved inexpensively by adjusting (under conditions). On the other hand, the improvement of the cold strength of sintered ore may lead to an increase in ventilation resistance and a decrease in productivity. In the present invention, such problems are controlled by controlling the maximum temperature and the high temperature range holding time. Can be solved.

  Therefore, in the sintering machine of the present invention, the introduction position of the diluted gas fuel into the charging layer is set so that the sinter ore is cooled in any zone between the sintered cake formed in the charging layer and the wet zone. It is determined in consideration of how to control the interstitial strength. From this viewpoint, in the present invention, the scale (size), number, position (distance from the ignition furnace), gas concentration of the gaseous fuel supply device, preferably the amount of carbonaceous material (solid fuel) in the sintered raw material By adjusting according to the temperature, not only the size of the combustion / melting zone (the thickness in the vertical direction and the width in the pallet movement direction), but also the high temperature reached temperature and the high temperature range holding time are controlled, and the generated firing The strength of the cake (sintered ore) is improved.

  In the sintering machine of the present invention, as described above, the gaseous fuel supplied into the charging layer is blast furnace gas, coke oven gas, blast furnace / coke oven mixed gas, city gas, natural gas or methane gas, ethane gas, propane. Either gas, butane gas, or a mixed gas thereof can be used. Among the gaseous fuels, it is preferable to use one having a CO content of 50 massppm or less. That is, CO gas is harmful to the human body, and if gaseous fuel supplied onto the charging layer is not introduced into the charging layer in its entirety, it may cause human injury if it leaks out of the machine. Because there is. Specifically, the use of city gas 13A or propane gas is preferable from the viewpoint of cost as well as safety.

  Furthermore, in the sintering machine of the present invention, in addition to the gaseous fuel, the ignition temperature in the gaseous state is higher than the temperature of the surface layer of the sintering bed, alcohols, ethers, petroleums, other hydrocarbon compounds, etc. The liquid fuel vaporized can also be used. Table 7 shows liquid fuels that can be used in the present invention and their characteristics. Since the gas fuel vaporized from such a liquid fuel has an ignition temperature higher than that of the gas fuel described above, it burns inside the charging layer, which is higher than the temperature of the sintered bed surface layer, It is effective for expanding the temperature of the burning / melting zone at the blowing position. In particular, the effect is large when the ignition temperature is close to 500 ° C. In addition, when using the gaseous fuel which vaporized liquid fuel, it is preferable to hold | maintain gas supply piping to the temperature more than the boiling point of this liquid fuel and less than ignition temperature so that the vaporized fuel may not re-liquefy.

  In addition, since waste oil etc. may contain the component which is easy to ignite, and the component with low ignition temperature, it is unpreferable for using by this invention. When liquid fuel such as waste oil containing components with low ignition temperature and flash point is vaporized in advance and supplied onto the sintering material bed, the upper part of the material bed surface before reaching the vicinity of the combustion zone in the material bed This is because it burns in the space or in the vicinity of the surface layer of the raw material bed, so that the effect of extending the high temperature holding time by burning in the vicinity of the combustion zone of the sintered raw material bed intended by the present invention cannot be obtained.

  The gaseous fuel supply device 12i in the sintering machine of the present invention is preferably disposed so as to straddle both sidewalls 8a of the pallet 8 along the width direction of the sintering machine. That is, in the gaseous fuel supply apparatus, a hood 21 is disposed so as to straddle both sidewalls 8a of the pallet 8, and one or more pipes for supplying gaseous fuel are provided therein, preferably 2 to 2. Fifteen, arranged in parallel or perpendicular to the direction of pallet travel, each of which has a plurality of slits, jet holes or nozzles for supplying gaseous fuel to the atmosphere at high speed Preferably, it is configured.

  One or more of the gaseous fuel supply devices 12i are disposed at any position in the pallet traveling direction, downstream of the ignition furnace 11 and in a process (state) in which the combustion / melting zone is proceeding in the charging layer. In that position, it is preferable to supply the diluted gas fuel into the charging layer. That is, this apparatus is arranged at one or a plurality of arbitrary positions after the combustion front advances below the surface layer on the downstream side of the ignition furnace. From the viewpoint of adjustment, the size, position, and number are determined.

The gaseous fuel supplied from the gaseous fuel supply device 12 may be supplied under a piping system that is independent from the ignition furnace 11, and as the same type as the ignition furnace fuel pipe, You may comprise so that it may connect on the extension of a gas supply pipe (not shown).
Next, Table 8 shows the contents and heat values of hydrogen, CO, methane, ethane, and propane contained as combustion components in C gas, LNG, and B gas.

  In the present invention, a diluted combustible gas is used as the gaseous fuel introduced into the charging layer. The degree of dilution will be described below. Table 9 shows the lower combustion limit concentration and upper combustion limit concentration of blast furnace gas, coke oven gas, mixed gas (M gas), propane, methane, and natural gas. For example, when a gas having such a combustion limit is directed to the exhaust fan without being burned in the charging layer, there is a risk of causing an explosion or combustion in the middle of the electrostatic precipitator. Therefore, as a result of trial and error, the inventors decided to introduce a gaseous fuel diluted to a concentration at which there is no danger, that is, below the lower limit concentration of combustion, into the charging layer, and to further improve safety, As a result of many experiments using a diluted gas fuel having a concentration of 75% or less of the lower combustion limit concentration, it was confirmed that no problem occurred.

  For example, as shown in Table 9, the concentration range at which the blast furnace gas burns in the atmosphere and at room temperature has a combustion lower limit of 40 vol% and a combustion upper limit of 71 vol%. That is, if it is less than 40 vol%, it does not burn, and if it exceeds 71 vol%, it means that the blast furnace gas concentration becomes too high, and in this case also, no combustion occurs. Below, the basis of this numerical value is demonstrated based on drawing.

FIG. 17 illustrates an example of a method for obtaining the combustion limit of blast furnace gas.
The ratio of the combustion component (combustible gas) and other components (inert: inert gas) contained in the blast furnace gas in the figure is as follows when examined in combination with H ₂ and CO ₂ and CO and N ₂ It is.
(1) The ratio of (inert gas) / (combustible gas) for the combination of the “H ₂ and CO ₂ ” portions is 20.0 / 3.5 = 5.7.

Therefore, when the portion (flammability limit) where the H ₂ + CO ₂ curve intersects the axis of 5.7 on the horizontal axis indicating the ratio of (inert gas) / (combustible gas) in this combustion limit diagram is obtained, the lower limit is 32 vol%, and the upper limit is 64 vol%. That is, the lower limit concentration of the combustion limit of H ₂ + CO ₂ is 32 vol%, and the upper limit concentration is 64 vol%.
(2) On the other hand, the ratio of (inert gas) / (combustible gas) in the case of the combination of the remaining combustion components “CO and N ₂ ” is 53.5 / 23.0 = 2.3. Similarly, the lower limit: 44 vol% and the upper limit: 74 vol% are obtained from the point where the horizontal axis 2.3 intersects with the curve of CO + N ₂ from FIG. Therefore, the lower limit concentration of the combustion limit in this case is 44 vol%, and the upper limit concentration is 74 vol%.
(3) Further, the lower combustion concentration of blast furnace gas containing both combustion components can be obtained by the equation on the lower left side in FIG. Further, if the upper limit values of (1) and (2) are applied in the same formula, the combustion upper limit concentration can be obtained. In this way, the lower combustion limit concentration and upper combustion limit concentration of the blast furnace gas can be obtained.

  In the present invention, another reason for focusing on the lower limit of combustion of gaseous fuel is that the combustion limit has temperature dependence. In the Fuel Handbook (edited by the Japan Fuel Association), as the effect of temperature, the heat dissipation rate slows down when the temperature is high, so the intersection of both the heat generation and dissipation velocity curves becomes deeper and the explosion range ( Explains that the (combustion range) extends to the left and right. That is, although the combustion limit is obtained as described above, the combustion limit is temperature-dependent, and as a result of the temperature in the combustion range of methane gas, Table 10 The example described in is shown. When this is plotted as the temperature dependence of the lower combustion limit concentration, it is as shown in FIG. The ● marks in the figure are examples of methane gas listed in Table 5.

  FIG. 19 shows the relationship between the concentration of combustion components (combustion gas) of gaseous fuel and temperature at normal temperature in the atmosphere. Although the combustion limit is obtained as described above, the combustion limit is temperature-dependent, and the temperature-dependent tendency is exemplified by the lower limit of combustion at room temperature (corresponding to the combustion gas concentration in the figure). Even if it is approximately 40 vol%, it varies from 26 to 27 vol% in the 200 ° C. region, and it burns even if it is several percent in the 1000 ° C. region and less than 1 vol% in the 1200 ° C. region.

From this, it is safer that the concentration of gaseous fuel (combustion component content) supplied to the charging layer is lower than the lower limit of combustion at room temperature, and the concentration of the diluted gas is within an appropriate range. It was found that the combustion position in the thickness direction in the charged layer of the gaseous fuel can be freely controlled by adjusting.
The combustion range of the gaseous fuel is thus temperature dependent. For example, the combustion range expands as the ambient temperature increases, and the combustion range of the sintering machine burns well in the temperature field near the combustion / melting zone of the sintering machine. It has also been found that in a temperature field of about 200 ° C. in an electrostatic precipitator on the downstream side of the sintering machine, combustion does not occur at a gaseous fuel concentration as shown in the preferred embodiment of the present invention.

  By the way, in producing the sintered ore, the diluted gas fuel supplied into the charging layer 9 of the sintering raw material is sucked by the wind box 16 under the sintering pallet 8 and solids in the charging layer 9 are obtained. It burns in the high temperature region of the combustion / melting zone formed by the combustion of fuel (powder coke). Accordingly, the supply of the diluted gas fuel can be adjusted by adjusting the amount of the diluted gas fuel, the supply amount, etc. under the condition that the amount of heat input to the charging layer is constant ( Decrease). Further, the adjustment of the concentration of the diluted gaseous fuel means that the combustion of the gaseous fuel is controlled to occur at a predetermined position (concentration region) in the charging layer.

  In this sense, the combustion / melting zone in the charging layer in the prior art is a zone where only solid fuel (powder coke) burns, but the combustion / melting zone in the present invention is in addition to the combustion of the powder coke. Furthermore, it can be said that the gas fuel is also a zone where the fuel is burned in parallel. Therefore, in the present invention, if the concentration, supply amount, and other supply conditions of the diluted gas fuel are premised on that there is coke breeze as part of the fuel, if it is suitably changed in relation to this, the maximum temperature reached And / or desirable control of the high temperature holding time is possible, leading to improved strength of the sintered cake.

  Furthermore, another reason for using the diluted gaseous fuel in the sintering machine of the present invention is to control the strength and yield of the sintered cake through the above-described sintering / melting zone shape control. The role of this diluted gas fuel functions effectively in controlling how long the sintered cake is kept in the high temperature zone (combustion / melting zone) and how much temperature is reached. Because it does. In other words, the use of the diluted gas fuel means that the high temperature range holding time of the sintered raw material is long and the maximum attained temperature is controlled to be appropriately high. Such control is diluted and adjusted so that the amount of combustion-supporting gas (air or oxygen) is not excessive or insufficient in the combustion atmosphere with respect to the solid fuel amount (powder coke amount) in the sintered raw material. This means using a gaseous fuel. In this regard, in the conventional technology, the amount of combustible gas is commensurate with the amount of solid fuel or combustible gas because the combustible gas is blown without adjusting the concentration, regardless of the amount of solid fuel in the sintering raw material. (Oxygen) was not supplied, causing poor combustion, or conversely causing partial overcombustion, leading to variations in strength. On the other hand, in the present invention, such a problem is avoided by diluting the gaseous fuel and adjusting the concentration.

  Further, the sintering reaction is summarized as shown in the schematic diagram of FIG. 20 according to “Mineral engineering” (Hideki Imai, Toshihisa Takeuchi, Yoshinori Fujiki, 1976, 175, Asakura Shoten). Table 11 shows the values of tensile strength (cold strength) and reducibility of various minerals generated during the sintering process.

  As apparent from FIG. 20, in the sintering process, in the low temperature firing region of 1400 ° C. or lower, firstly, primary hematite (original ore) contained in the iron ore is generated and then magnetite is formed from the primary hematite. Generated. Then, a melt starts to be generated at 1200 ° C., and iron ore and limestone react to generate calcium ferrite having the highest strength among the constituent minerals of the sintered ore and relatively high reducibility. Further, when the temperature rises to a high temperature firing region exceeding about 1380 ° C., the calcium silicate has the lowest cold strength and reducibility, and the secondary hematite that is easily reduced to powder. Disassembled into In addition, as shown in FIG. 21, calcium ferrite reacts with iron ore and limestone at 1200 ° C. to produce acicular calcium ferrite, and this acicular calcium ferrite is maintained up to 1350 ° C. When the temperature exceeds 1350 ° C. It changes to columnar calcium ferrite and this state is maintained up to 1380 ° C., but when it exceeds 1380 ° C., it decomposes into amorphous silicate (calcium silicate) and secondary hematite.

Therefore, in order to improve the cold strength of sintered ore and the reduction powder reduction index (RDI), it is important whether or not calcium ferrite can be stably produced without decomposition. Become.
As shown in FIG. 22, the quality of the sintered ore required from the blast furnace 64 includes the shutter strength (cold strength) that does not pulverize when the sintered ore is charged into the blast furnace 64 and the shaft upper portion (about 550 ° C.). ) And reduced index (RDI) that does not reduce powder, and reducibility (RI) that is easy to reduce gas in a heat storage zone (about 900 ° C.).

  As shown in FIG. 23, the demand for sintered ore quality is increased, and high strength sintered ore is required for improving the air permeability in the furnace, as shown in FIG. Low-reduction dusting (RDI) sintered ore is required to expand the low-temperature reduced-powdering area due to the rise (decrease in coke ratio), and the ratio of iron ore / coke is increased to increase the unreduced layer Therefore, a highly reducible sintered ore is required, and a good burn-off characteristic is required.

As shown in FIG. 24, the quality of sintered ore required from the blast furnace 64 includes shutter strength (SI) or tumbler strength (TI) representing the strength of sintered ore as a quality guarantee, low-temperature reduced powdering property (RDI). ) And reducibility (RI), the particle size (mm) and weight (kg) and the measurement method are set. Here, the shutter strength (SI) is a weight ratio of a product sintered ore having a particle size of 10 to 50 mm and a weight of 20 kg, which is left on a 10 mm sieve after dropping 4 subordinates from a height of 2 m. In addition, the tumbler strength (TI) is measured by measuring a weight ratio of a product sintered ore having a particle size of 10 to 40 mm and a weight of 15 kg remaining on a 6.3 mm sieve after 200 rotations with a 1 mφ drum (25 rpm). Further, the low temperature reduced powdering property (RDI) is obtained by measuring a product sintered ore having a particle size of 16 to 20 mm and a weight of 0.5 kg at 550 ° C. with CO / N ₂ = 30/70 vol. After reducing with 30% reducing gas for 30 minutes, a weight ratio of 2.8 mm or less after 900 revolutions with a 130 mmφ drum (30 rpm) is measured. Furthermore, the reducibility (RI) is obtained by measuring a product sintered ore having a particle size of 19 to 21 mm and a weight of 0.5 kg at 900 ° C. with CO / N ₂ = 30/70 vol. The weight loss after 180 minutes of reduction with% reducing gas is measured.

For the reducing powder index (RDI) and the reducibility (RI), a structure of primary hematite and acicular calcium ferrite is preferable.
In addition, according to the above-mentioned publication “Mineral Engineering”, the precipitation behavior of secondary hematite, which is the starting point of reduced powdering of sintered ore, is explained by the CaO—Fe ₂ O ₃ binary phase diagram shown in FIG. Yes. According to the explanation, in the result of the mineral synthesis test, the skeletal secondary hematite that is the starting point of the reduction powdering is Mag. + Liq. In order to precipitate after cooling up to the region and cooling, on the phase diagram, not the route of (1) exceeding 1400 ° C, but the route of formation of (2) magnetite of less than 1380 ° C or less than 1358 ° C ( It is said that reducing powdering properties can be suppressed by producing sintered ore through a path in which magnetite of 3) is not formed.

  And when the change of the mineral structure in the sintering process of FIG. 20 mentioned above was investigated by the electric furnace experiment, the result shown in FIG. 26 was obtained. FIG. 26 shows the result of quantitative determination of the mineral composition ratio after sintering at each temperature by a powder X-ray diffraction method. When the sintering temperature is held at 1200 ° C. for 250 seconds, hematite is 50%, calcium ferrite. Is 45% and the remainder is magnetite and calcium silicate. When the sintering temperature is held at 1250 ° C. for 250 seconds, the weight ratio is not much different from that when the sintering temperature is held at 1200 ° C. for 250 seconds, but when the sintering temperature is held at 1300 ° C. for 250 seconds, magnetite and Calcium silicate increases and calcium ferrite decreases accordingly. Further, when the sintering temperature is held at 1350 ° C. for 250 seconds, the calcium silicate is 10% and the magnetite is 5%, and the calcium ferrite is further reduced by this amount. Furthermore, when the sintering temperature is maintained at 1400 ° C. for 250 seconds, calcium silicate exceeds 30%, magnetite also exceeds 10%, and calcium ferrite decreases to less than 10%.

As a result, it was demonstrated that calcium ferrite was generated from 1200 ° C. and decomposed and melted into calcium silicate + hematite at 1400 ° C. or higher.
Therefore, in order to produce a sintered ore having both low RDI and high strength, it can be maintained for a long time within the range of 1200 ° C. (solidus temperature of calcium ferrite) and about 1380 ° C. (transition temperature). It is important to realize the heat pattern in the charging layer.

  By the way, in the conventional sintering machine which does not use the gaseous fuel supply devices 12a to 12d like the sintering machine of the present invention, as shown in FIG. 11, hot air of about 250 ° C. is blown in a heat retaining furnace 13 adjacent to the downstream side, and the combustion melting zone is sequentially moved to the lower layer as the pallet 8 moves to form a sintered cake.

  In this case, when the amount of coke breeze is set to 5%, as shown by the broken line in FIG. 27 (c), after about 7 minutes have elapsed after ignition in the ignition furnace 11, the temperature in the layer suddenly increases to 1200 ° C. After the temperature exceeds about 2 minutes, the temperature drops below 1200 ° C, and the maximum temperature reaches about 1300 ° C. Therefore, the high temperature holding time for maintaining the state of 1200 ° C. or higher is as short as about 2 minutes.

  If the amount of coke breeze is increased to 6% in order to lengthen this high temperature holding time, the holding time can be increased to about 4 minutes as shown by the solid line in FIG. 27 (c). Exceeds 1400 ° C., and calcium ferrite is decomposed into amorphous silicate (calcium silicate) having the lowest cold strength and reducibility and secondary hematite that is easily reduced to powder.

The relationship between the amount of powder coke (%), the strength of sintered ore (%), and the reducibility (%) is as shown in FIG.
Here, the strength of the sintered ore is maintained at about 70% when the amount of coke breeze is between 5.0% and 5.5%, but if it is less than 5.0%, the high temperature holding time is shortened, so that the powder coke is reduced. As the amount of sinter decreases, the strength of sinter decreases, and when it exceeds 5.5%, amorphous silicate (calcium silicate) is generated due to the highest temperature exceeding 1400 ° C. The sinter strength decreases with the increase.

On the other hand, the reducibility exceeds 70% when the amount of coke breeze is 4.0%. However, when the amount of powder coke is increased, the reducibility gradually decreases accordingly, and the powder coke is reduced. The amount becomes 65% at 5.0% and decreases to 62% at 5.5%, and then the reducibility is further reduced in accordance with the increase in the amount of powder coke.
By the way, improvement of strength and reducibility of sintered ore is effective for reducing CO ₂ in the sintering / blast furnace process. However, as described above, when sintering is performed using only powder coke, as shown in FIG. 27 (a), in order to improve the cold strength of the sintered ore, Increasing the coke ratio is effective, and blowing hot air in the heat insulation furnace 13 is effective although it is less effective. However, increasing the powder coke ratio for sintering to improve the strength of the sintered ore results in the formation of amorphous silicate (calcium silicate) due to the highest reached temperature exceeding 1400 ° C. The nature will decline.

On the other hand, if a porous ore is used to improve the reducibility of the sintered ore, the cold strength is lowered. It is difficult to improve both the cold strength and the reducibility only by the amount of powder coke, and the CO ₂ reduction effect in the sintering / blast furnace process cannot be improved.
In the conventional sintering machine, in order to manage the shutter strength, reducibility (RI) and reduction powder index (RDI), as shown in FIG. 28, the shutter strength, reducibility (RI) and reduction Since there is a correlation between the pulverization index (RDI) and the FeO ratio in the product sintered ore, the FeO ratio in the product sintered ore is measured once every 2 hours, for example, as a management index.

In general, the FeO ratio in the sintered product ore represents the heat level in the sintered layer, and as one of the management indicators for achieving a predetermined cold strength (shutter strength), the measurement is, for example, for FeO measurement. By applying a magnetic balance (Evans method), it is faster and simpler than strength, reducibility, and reduced powder index (RDI).
For this reason, in the conventional sintering machine, as shown in FIG. 28, when the shutter strength is set to a high value, for example, 89%, the target value of FeO (%) in the product sintered ore is set to 6.4. The amount of coke breeze is adjusted to maintain this target value.

  However, in the conventional sintering machine, as described above, when the maximum attainable temperature is controlled to be 1200 ° C. or higher and lower than 1400 ° C., for example, as shown in FIG. When set to 0%, a high temperature holding time in which the combustion / melting zone is present in the middle portion of the charging layer 9 and continues above 1200 ° C. as shown by the broken line in the graph showing the time with respect to the temperature in the layer Shorter. If the amount of coke breeze is increased to 6.0% in order to lengthen this high temperature holding time, the high temperature holding time of 1200 ° C. or more becomes longer as shown by the solid line in the graph showing the time with respect to the temperature in the layer, but the maximum The reached temperature exceeds 1400 ° C. For this reason, calcium ferrite is decomposed and melted into calcium silicate and hematite, and the sinter strength and the reduced powder index RDI are lowered. A good sintered ore cannot be obtained.

  On the other hand, in the sintering machine of the present invention, as shown in FIG. 29 (b), the amount of coke breeze is reduced from 5% to 4.6%, and diluted liquefied natural gas (LNG) instead. ) Is injected from above the charging layer 9 and sucked into the charging layer 9 by the wind box 16, the sucked diluted liquefied natural gas (LNG) burns above the combustion / melting zone. To do. For this reason, as shown by the solid line in the graph showing the time with respect to the temperature in the layer in FIG. 29B, the maximum attained temperature is 1200 ° C. or higher compared to the case where the temperature is controlled only with the amount of powder coke 5% shown in the broken line. The high temperature holding time can be increased by a factor of 2 or more while keeping the temperature below 1380 ° C. As a result, it is possible to reliably prevent calcium ferrite from being decomposed and melted into calcium silicate and secondary hematite, and to improve the sinter strength.

  Thus, in the present invention, the amount of carbon material to be added is reduced, the shortage is adjusted by supplying gaseous fuel, and the maximum temperature reached in the charging layer is controlled to a range of 1200 ° C. or more and less than 1380 ° C. It is important to reduce the reduced powdering property (RDI) and improve the reducibility (RI). .

  FIG. 30 compares the sintering method of the present invention using a diluted gaseous fuel obtained by diluting a city gas vaporized LNG as a gaseous fuel below the lower combustion limit concentration and a conventional sintering method in which gaseous fuel is not injected. The experimental results are shown. In addition, in the conventional sintering example in which the diluted gas fuel is not injected, the amount of added powder coke is 5 mass%, while in the present invention example in which the diluted gas fuel equivalent to 0.4 mass% of powder coke is injected, the total heat amount is constant. Therefore, the amount of powdered coke added was 4.6 mass%. As can be seen from FIG. 30, when the diluted gas fuel is used, the combustion / melting zone width is 150 mm, which is about 2.5 times longer than the conventional example, and the cold strength (shutter strength), product yield, and productivity are increased. Improvement was observed. As described above, in the use example of the diluted gas fuel, the reason why the shutter strength, the product yield, and the like are improved is considered to be due to the expansion of the combustion / melting zone and the extension of the high temperature region holding time.

Next, the influence by the kind of gaseous fuel is shown.
FIG. 31 shows the sintering method of the present invention using diluted gaseous fuel obtained by diluting three types of gaseous fuels of propane gas, coke oven gas (C gas) and city gas vaporized LNG to below the lower combustion limit concentration, The experimental result compared with the conventional sintering method which does not inject a fuel is shown. In addition, in the conventional sintering example in which the diluted gas fuel is not injected, the amount of added powder coke is 5 mass%, while in the present invention example in which the diluted gas fuel equivalent to 0.8 mass% of powder coke is injected, the total heat amount is constant. Therefore, the amount of powdered coke added was 4.2 mass%. As can be seen from FIG. 31, when diluted gas fuel was used, improvement in shutter strength, product yield, and productivity was observed in all examples. As described above, in the use example of the diluted gas fuel, the reason why the shutter strength, the product yield, and the like are improved is considered to be due to the expansion of the combustion / melting zone and the extension of the high temperature region holding time.

Although there is no significant difference depending on the type of gaseous fuel from the results of FIG. 31, city gas having a low combustion lower limit concentration and a high calorific value is advantageous for fire prevention. In order to prevent reverse fire, city gas (CH ₄ main component) having a flame propagation speed slower than C gas (H ₂ main component) is superior. Furthermore, city gas does not contain CO, and city gas is superior from the viewpoint of gas poisoning. Furthermore, since city gas can be supplied at high pressure, it is advantageous in terms of construction cost.

For this reason, it is preferable to employ city gas as gaseous fuel for safety and disaster prevention and construction costs.
As described above, after igniting the carbon material of the charging layer 9 in the ignition furnace 11, the gaseous fuel is injected from the upper surface side of the charging layer 9 and mixed with air by the gaseous fuel supply devices 12a to 12d. The diluted gas fuel 38 is sucked by the wind box 16 and introduced into the charging layer 9, thereby expanding the combustion / melting zone while controlling the maximum temperature of the combustion / melting zone to less than 1380 ° C. The holding time can be lengthened, and reduced powdering property (RDI) can be suppressed while improving shutter strength and reducibility (RI).

As described above, in the present invention, the combined sintered ore that represents the heat level in the sintered layer and is one of the management indices for achieving a predetermined cold strength by using the coke breeze and the gaseous fuel together. As shown in FIG. 32, the relationship between the FeO ratio (%), shutter strength (%), reducibility (RI), and reduced dustability (RDI) in the gas fuel described with reference to FIG. In order to obtain an equivalent shutter strength of 89% as compared with the sintering method using only the powder coke of the conventional example not including, the FeO ratio in the product sintered ore is about 6.4% to about 5.4. % Can be reduced by about 1%. For this reason, it is possible to control the cold intensity (shutter intensity) by setting a target value for the low FeO ratio. Here, reducing the FeO ratio by about 1% makes it possible to reduce the powder coke ratio in the sintering machine 3 by about 5 kg / t, and can reduce the amount of CO ₂ generated in the sintering process. .

  For this reason, in this invention, as shown in FIG. 33, the gaseous fuel supply part 32 makes the city gas as gaseous fuel supplied from the city gas supply main pipe | tube 41 the city gas to each gaseous fuel supply apparatus 12a-12d. It branches into the supply branch pipes 42a-42d, and is supplied to the separate gaseous fuel control parts 43a-43d. In the individual gas fuel control unit 43 a, a shutoff valve 44 is inserted in the city gas supply branch pipe 42 a, and a branching portion 45 is disposed on the downstream side of the shutoff valve 44. In this branching portion 45, the city gas supplied through the shutoff valve 44 is branched into seven branch pipes 46 in order to supply them to the seven gaseous fuel injection nozzles 31, and each branch pipe 46 has a flow meter. 47 and the flow control valve 48 are inserted in that order, and the gaseous fuel injection nozzle 31 is connected to the downstream side of the flow control valve 48. The other individual gas fuel control units 43b to 43d also have the same configuration as the individual gas fuel control unit 43a, although detailed description thereof is omitted.

Then, the shutoff valve 44 and the flow rate adjustment valve 48 of each of the individual gas fuel control units 43 a to 43 d are controlled by the control device 50.
As shown in FIG. 33, flow rate detection data of the flowmeter 47 of the individual gaseous fuel control units 43 a to 43 d of the gaseous fuel supply devices 12 a to 12 d is input to the control device 50, and inside the hood 21. The ignition detection signal of the ignition detector 51 disposed between the upper surface of the charging layer 9 of the sintering pallet 8 and the gaseous fuel injection nozzle 31 and the leakage of the leakage detector 52 disposed at the upper end of the hood 21. A detection signal is input, and further, FeO ratio data of an FeO measuring device 53 configured by, for example, a FeO measuring magnetic balance (Evans method) for measuring the FeO ratio of the sintered product ore is input.

  Further, the control device 50 is connected to the output side thereof with a shutoff valve drive circuit 54 for driving and controlling the shutoff valve 44 inserted in the gas fuel supply branch pipes 44a to 44d of the individual gas fuel supply units 42a to 42d. A control valve drive for controlling the flow rate control valve 48 for controlling the flow rate to the gaseous fuel injection nozzles 31 of the individual gaseous fuel supply units 42a to 42d, while outputting a cutoff valve control signal for controlling the cutoff valve drive circuit 54. A circuit 55 is connected to output a flow control command value for controlling the flow control valve drive circuit 55.

  And in the control apparatus 50, as shown in FIG. 34, a gaseous fuel supply control process is performed. This gaseous fuel supply control process is executed as a timer interrupt process at predetermined intervals. First, in step S1, detection signals detected by the ignition detector 51 and the leak detector 52 are read, and then the process proceeds to step S2. Then, it is determined whether or not the detection signal of the ignition detector 51 detects an ignition state, and when the ignition state is detected, the process proceeds to step S3, and the gaseous fuel supply device 12i ( The gaseous fuel control process is terminated after outputting an on-state control signal SC for controlling the shut-off valve 44 disposed at i = a, b, c, d) to be closed.

  On the other hand, when the determination result of step S2 is not detecting the ignition state by the ignition detector 51, the process proceeds to step S4, and it is determined whether or not the leakage state is detected by any of the leakage detectors 52, When any one of the leak detectors 52 detects a leak state, the process proceeds to step S5, and the shutoff valve 44 disposed in the gas supply device 12i in which the leak detector 52 that has detected the leak state is disposed is closed. After the control signal SC in the off state for controlling the state is output, the gaseous fuel control process is terminated.

  Further, when the determination result of step S4 does not detect the leakage state in all the leakage detectors 52, the process proceeds to step S6 to determine whether or not the FeO ratio data is input from the FeO measurement device 53, and FeO When the ratio data is not input, the timer interrupt process is terminated as it is, and the process returns to the predetermined main program. When the FeO ratio data is input, the process proceeds to step S7.

  In this step S7, from the target value 6.4% when the inputted FeO ratio data in the sintered product ore does not have the gas fuel supply devices 12a to 12d set in advance based on the result of FIG. It is determined whether or not the target value 5.4% lower by about 1% is within an allowable range (5.4% ± α) provided with an allowable range ± α. It is determined that the gaseous fuel supply amount from 12a to 12d is in an appropriate state, and the timer interruption process is terminated as it is. When it is outside the allowable range, the process proceeds to step S8.

  In this step S8, it is determined whether or not the FeO ratio data exceeds the upper limit value of the allowable range. If the upper limit value of the allowable range is exceeded, the process proceeds to step S9, and each gaseous fuel supply device 12a. A value obtained by subtracting a predetermined amount ΔF1 from the previous flow rate command SF (n−1) for setting the flow rate of the flow rate adjustment valve 48 of the individual gas fuel control units 43a to 43d of 12d to the new flow rate command SF (n). Then, the process proceeds to step S10, the calculated flow rate command SF (n) is output to each control valve drive circuit 55, and the timer interruption process is terminated.

On the other hand, when the determination result of step S8 is that the FeO ratio data does not exceed the upper limit value of the allowable range, it is determined that the FeO ratio data is below the lower limit value of the allowable range, and the process proceeds to step S11. A value obtained by adding a predetermined amount ΔF2 to the flow rate command value SF (n-1) is calculated as a new flow rate command value SF (n), and then the process proceeds to step S10.
Therefore, in the control device 50, the ignition detector 51 of the gaseous fuel supply devices 12a to 12d does not detect ignition by the gaseous fuel supply processing shown in FIG. 34, and the leakage detector 52 also detects the leakage of gaseous fuel. In a normal state that is not, the process proceeds to step S6 through step S1, step S2, and step S4. In this step S6, it is determined whether or not the FeO ratio data is input from the FeO measuring device 53. When the FeO ratio data is not input, the timer interrupt process is terminated as it is and the process returns to the predetermined main program.

  However, when FeO (%) in the sintered product ore is measured by the FeO measuring device 53 and the FeO ratio data as the measurement result is output and input to the control device 50, the process proceeds from step S6 to step S7. When the transition is made and the FeO ratio data is within a preset allowable range (5.4% ± α), it is determined that the supply of the gaseous fuel from each of the gaseous fuel supply devices 12a to 12d is in a normal state, The timer interruption process is terminated as it is, and the current gaseous fuel supply flow rate in each of the gaseous fuel supply devices 12a to 12d is maintained.

  However, for some reason, when the FeO ratio data exceeds the upper limit of the allowable range, the heat level of the charging layer (sintered layer) 9 increases, and the cold strength increases from the target cold strength. Therefore, the flow rate command SF (n) for the flow rate adjustment valve 48 provided in the individual gaseous fuel supply units 43a to 43d in each of the gaseous fuel supply devices 12a to 12d is predetermined from the previous flow rate command (n-1). The value ΔF1 is calculated as a value obtained by subtraction (= SF (n−1) −ΔF1) (step S9), and the calculated flow rate command SF (n) is output to the control valve drive circuit 55 (step S10).

For this reason, the opening degree of the flow rate adjustment valve 48 of each of the gaseous fuel supply devices 12a to 12d is controlled to be small, and the gaseous fuel supplied to the fuel injection nozzle 31 is reduced by a predetermined amount. ) The heat level of 9 is lowered by a predetermined amount, the proportion of FeO in the sintered product ore is lowered and returned to the allowable range.
Conversely, when the FeO ratio data falls below the lower limit of the allowable range, it is determined that the heat level of the charging layer (sintered layer) 9 has decreased and the cold strength has decreased from the target cold strength. The flow rate command SF (n) for the flow rate adjustment valve 48 provided in the individual gaseous fuel supply units 43a to 43d in each of the gaseous fuel supply devices 12a to 12d is set to a predetermined value ΔF2 for the previous flow rate command (n-1). The calculated value (= SF (n−1) + ΔF2) is calculated (step S11), and the calculated flow rate command SF (n) is output to the control valve drive circuit 55 (step S10).

  For this reason, the opening degree of the flow rate adjustment valve 48 of each of the gaseous fuel supply devices 12a to 12d is largely controlled, and the gaseous fuel supplied to the fuel injection nozzle 31 is increased by a predetermined amount, whereby the charging layer (sintered layer) ) The heat level of 9 is increased by a predetermined amount, the proportion of FeO in the sintered product ore is increased, and the proportion of FeO is returned to the allowable range.

  In this way, by controlling the FeO ratio within the allowable range (5.4% ± α), the shutter strength can be maintained at 89% of a favorable value as shown in FIG. 32 described above. . Moreover, in order to control the shutter intensity to the target value, control is performed based on the FeO ratio in the product sintered ore, so the FeO ratio in the product sintered ore can be measured easily and quickly with the FeO measuring device 53. Since the measurement result can be obtained in a shorter time than when actually measuring the shutter strength, the control accuracy of the shutter strength can be improved.

FIG. 35 shows the case where the diluted gas fuel is not supplied and the gaseous fuel supply devices 12a to 12d during the operation of the actual sintering machine 3 in which the quick lime ratio and the raw material layer thickness are constant and the production of sintered ore is constant. For example, when a gaseous fuel made of LNG is diluted with air and supplied onto the charging layer 9 as a diluted gaseous fuel, the strength of sintered ore (%), and the basic unit of coagulated material made of powdered coke (kg / t- It is a graph showing the change of s) and to-be-reduced formation (JIS-RI). As apparent from the graph of FIG. 35, the sinter strength (%) maintains a value of around 72% in a state where LNG is not supplied from the gaseous fuel supply devices 12a to 12d, but the LNG is, for example, 250 Nm ³ / With the flow rate of hr, through the supply, the sinter strength (%) was maintained at about 74%, and the sinter strength (%) could be increased by about 2%.

  In addition, the basic unit of coagulation material (kg / t-s) such as coke breeze was about 59 kg / t when LNG was not supplied, but decreased to 56 kg / t when LNG started to be supplied. The reducibility (JIS-RI) (%) is 63% in the state where LNG is not supplied, whereas it can be improved by about 4%, about 67%, when LNG is supplied. . Therefore, it was confirmed that the quality of sintered ore could be improved in addition to the improvement of production rate and yield by appropriately injecting diluted gas fuel.

FIG. 36 is a graph showing the operation state before and after the supply of LNG in the sintering process for 3 months. In FIG. 36, the supply state of LNG (Nm ³ / h), the production amount (1,000 t / day), the powder coke (aggregated material) basic unit (kg / t), and the powder during transportation from the sintering process to the blast furnace It shows the transition of rate (%). As is clear from FIG. 36, although there are operational fluctuations, with the supply of LNG to the charging layer 9, the production volume is constant and the basic unit of coke breeze (the basic unit of coagulated material) is the estimated value in the first half of this year Compared to 59.2 kg / ts, it is reduced by about 3 to 4 kg / ts from 60.5 kg / ts to 56.5 kg / ts. The powder rate during the blast furnace transportation from the sintering process is also reduced. In either case, the operation could be continued while clearing the profit value.

  As shown in FIG. 36, the results of measuring the sinter cold strength, reducibility (JIS-RI), and reduced dustability (JIS-RDI) when LNG is supplied are as shown in FIG. In the state in which LNG is blown into the charging layer 9, there is no significant change in the reduced powdering property (JIS-RDI), but the sinter cold strength and reducibility (JIS-RI) Has been confirmed to be greatly improved.

  In addition, in the said embodiment, although the case where the four gaseous fuel supply apparatuses 12a-12d were provided was demonstrated, it is not limited to this, The number of gaseous fuel supply apparatuses can be set arbitrarily. Similarly, although the case where the number of the gaseous fuel injection nozzles 31 disposed in the gaseous fuel supply devices 12a to 12d is seven has been described, the number is not limited to this, and according to the width of the sintering pallet 8 Any number can be set.

  Further, the Feo measuring device 53 is not limited to the magnetic balance for measuring Feo, and an Feo measuring device such as another magnetic analyzer can be applied.

  The technique of the present invention is useful as a technique for producing sintered ore used as a raw material for iron making, particularly as a blast furnace, but can also be used as another ore agglomeration technique.

DESCRIPTION OF SYMBOLS 1a ... Iron ore powder hopper, 1b ... Limestone hopper, 1c ... Returning hopper, 1d ... Powder coke hopper, 2 ... Drum mixer, 3 ... Sintering machine, 4 ... Floor hopper, 5 ... Surge hopper, 8 ... Sinter pallet , 9 ... charging layer, 11 ... ignition furnace, 12a to 12d ... gaseous fuel injection device, 16 ... wind box, 21 ... gaseous fuel supply part surrounding hood, 21a ... front and rear walls, 21b ... left and right walls, 21c ... surrounding part, 21d ... Anti-scattering fence, 22 ... Rectifying plate, 22a-22c ... Rectifying plate row, 25 ... Outer hood portion, 26 ... Inner hood portion, 27 ... Relative movement mechanism, 31 ... Gaseous fuel injection nozzle, 31a ... Gaseous fuel injection port , 43a to 43b ... gaseous fuel supply unit, 44 ... shut-off valve, 48 ... flow control valve, 50 ... control device, 51 ... ignition detector, 52 ... leak detector, 53 ... Feo measurement Location, 54 ... shutoff valve drive circuit, 55 ... control valve driving circuit

Claims (13)

A circulating pallet,
A raw material supply device for forming a charge layer by charging a sintered raw material containing fine ore and carbonaceous material on the pallet;
An ignition furnace for igniting the charcoal of the charging layer;
A wind box disposed below the pallet;
A hood disposed on the downstream side of the ignition furnace and surrounding an upper portion of the charging layer;
A gaseous fuel supply device that injects gaseous fuel above the charging layer in the hood, mixes with air, and supplies it to the charging layer as diluted gaseous fuel;
An FeO measuring device for measuring the FeO ratio in the sintered product ore,
The FeO ratio measured by the FeO measuring apparatus is used as a management index for achieving a predetermined cold strength, and the target value of the FeO ratio is set to a lower value than that in the case where the gaseous fuel supply device is not installed to set the cold strength. A sintering machine characterized by performing a controlled operation.   2. The sintering machine according to claim 1, wherein the gaseous fuel supply device ejects the gaseous fuel at a flow velocity at which a blow-off phenomenon occurs from the ejection port.   The sintering machine according to claim 2, wherein the flow velocity at which the blow-off phenomenon occurs is a velocity exceeding a combustion rate of the gaseous fuel.   4. The sintering machine according to claim 2, wherein the gaseous fuel supply device ejects gaseous fuel from an ejection port having an opening diameter of less than 3 mmφ.   5. The sintering machine according to claim 2, wherein the gaseous fuel supply device ejects gaseous fuel from an ejection port having an opening diameter of 0.8 to 1.5 mmφ.   The said gaseous fuel supply apparatus is comprised so that at least one of the high temperature area holding time in a charging layer and a maximum attainment temperature may be controlled, The any one of Claim 1 thru | or 5 characterized by the above-mentioned. Sintering machine.   7. The gaseous fuel supply device according to claim 1, wherein the gaseous fuel supply device is a step of controlling a high temperature region holding time in the charging layer by adjusting at least one of a supply amount and a concentration of the diluted gaseous fuel. The sintering machine described in   The gaseous fuel supply device is configured to control at least one of a supply amount and a concentration of the diluted gaseous fuel so as to control a maximum attained temperature in the charging layer in a range of 1200 to 1380 ° C. The sintering machine according to any one of claims 1 to 7.   The gaseous fuel supply device controls to cause at least a part of the diluted gaseous fuel introduced from above the charging layer to reach a combustion / melting zone in the charging layer without being burned. Item 9. The sintering machine according to any one of Items 1 to 8.   The gas fuel supply device burns diluted gaseous fuel introduced from above the charging layer in the charging layer, and controls a form of a combustion / melting zone in the charging layer. The sintering machine according to any one of 1 to 9.   The gaseous fuel supply device is characterized in that the dilute gaseous fuel is introduced into the charging layer after the sintering cake is formed on the charging layer surface layer until the sintering is completed. The sintering machine according to any one of claims 1 to 10.   12. The gas fuel supply device according to claim 1, wherein the gaseous fuel supply device introduces the diluted gas fuel into the charging layer in a region where the thickness of the combustion / melting zone is 15 mm or more. The sintering machine described.   The gaseous fuel is any one combustible gas selected from blast furnace gas, coke oven gas, blast furnace / coke oven mixed gas, city gas, natural gas, methane gas, ethane gas, propane gas and mixed gas thereof. The sintering machine according to any one of claims 1 to 12, characterized in that:

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