Patent Grant
11041621
The present disclosure relates to an auxiliary burner attached to an electric furnace for manufacturing molten iron by melting iron scrap.
When melting iron scrap using an electric furnace, the iron scrap around the electrode melts quickly; and the iron scrap located away from the electrode, that is, the iron scrap at cold spots melts slowly, resulting in inhomogeneity in melting speed of the iron scrap in the furnace. For this reason, the operating time of the whole furnace has been limited by the melting speed of the iron scrap at the cold spots.
Therefore, in order to solve the inhomogeneity in melting speed of such iron scrap and to melt the iron scrap in the whole furnace in a well-balanced manner, a method of installing auxiliary burners at the cold spots to preheat, cut, and melt the iron scrap located at the cold spots has been adopted.
As such an auxiliary burner, for example, JPH10-9524A (PTL 1) proposes an auxiliary burner having a triple tube structure that ejects oxygen gas for splattering incombustibles and cutting iron scrap from a center part, ejects fuel from the outer circumference of the oxygen gas, and ejects oxygen gas for combustion from the outer circumference of the fuel. This auxiliary burner is a high-speed pure oxygen auxiliary burner for an electric furnace in which a reduced part is provided on the tip of the oxygen gas ejection tube at the center part so as to increase the speed of the oxygen gas to be ejected from the center part, and swirl vanes are installed in an annular space formed by the fuel ejection tube and the combustion oxygen gas ejection tube so as to swirl the oxygen gas for combustion to be ejected from the outermost circumference.
Additionally, JP2003-004382A (PTL 2) proposes a burner facility for an electric furnace that spreads the directivity of the burner flame over a wide range by eccentrically placing the nozzle tip of the auxiliary burner and rotating the burner.
PTL 1: JPH10-9524A
PTL 2: JP2003-004382A
By using the techniques described in PTL 1 and PTL 2, it is possible to efficiently preheat and melt iron scrap using an auxiliary burner. However, in PTL 1 and PTL 2, there is a problem that the fuel to be used is restricted to expensive gas fuel. Examples of inexpensive fuel include solid fuels such as coal. However, it is generally difficult to burn solid fuel faster than gas fuel, and moreover, depending on conditions, an accidental fire may be caused, making it difficult to use solid fuel in an auxiliary burner.
An object of the present disclosure is to provide an auxiliary burner for an electric furnace capable of increasing and homogenizing the heating effect of iron scrap by suitably and efficiently burning solid fuel along with gas fuel.
The inventors conducted studies on an auxiliary burner for an electric furnace capable of using solid fuels such as coal. Through the studies, the inventors discovered that, in a multiple tube structure auxiliary burner using gas fuel and solid fuel as fuel, by swirling the combustion-supporting gas injected from the outermost circumference under specific conditions, the solid fuel can be burned suitably and efficiently along with the gas fuel, and as a result, the scrap heating effect is improved, and the flame temperature of the burner is homogenized.
The present disclosure was completed on the basis of such findings, and has the following subject.
[1] An auxiliary burner for an electric furnace for manufacturing molten iron by melting iron scrap, which is attached to the electric furnace and uses a gas fuel and a solid fuel as fuel, comprising:
a solid fuel injection tube defining a first flow path through which the solid fuel passes and configured to inject the solid fuel from a tip of the first flow path;
a gas fuel injection tube arranged around the solid fuel injection tube, defining a second flow path through which the gas fuel passes between the gas fuel injection tube and an outer wall of the solid fuel injection tube, and configured to inject the gas fuel from a tip of the second flow path;
a combustion-supporting gas injection tube arranged around the gas fuel injection tube, defining a third flow path through which a combustion-supporting gas passes between the combustion-supporting gas injection tube and an outer wall of the gas fuel injection tube, and configured to inject the combustion-supporting gas from a tip of the third flow path; and
a plurality of swirl vanes for swirling the combustion-supporting gas arranged in the third flow path at a predetermined interval in a circumferential direction of the third flow path, wherein
the plurality of swirl vanes form an angle θ of 5° or more and 45° or less with a burner axis.
[2] The auxiliary burner for an electric furnace according to [1], wherein the angle θ is 10° or more and 30° or less.
[3] The auxiliary burner for an electric furnace according to [1] or [2], wherein when each of the swirl vanes has a length Q in the circumferential direction and the plurality of swirl vanes have an installation interval P in the circumferential direction, Q/P is 1.0 or more and 1.2 or less.
[4] The auxiliary burner for an electric furnace according to any one of [1] to [3], wherein the tip of the third flow path has a discharge area such that a combustion-supporting gas discharge speed at a minimum supply amount of the combustion-supporting gas is 10 m/s or more.
According to the auxiliary burner of the present disclosure, it is possible to increase and homogenize the heating effect of iron scrap by suitably and efficiently burning the solid fuel along with the gas fuel.
In the accompanying drawings:
Hereinafter, an auxiliary burner 100 for an electric furnace according to an embodiment of the present disclosure is described with reference to
In the auxiliary burner 100, the body part for supplying fuel and combustion-supporting gas has a triple tube structure in which a solid fuel injection tube 1, a gas fuel injection tube 2, and a combustion-supporting gas injection tube 3 are arranged coaxially in the stated order from the center side. The solid fuel injection tube 1 defines a solid fuel flow path 10 (first flow path) through which solid fuel passes, and injects solid fuel from a circular solid fuel discharge port 11 which is the tip of the solid fuel flow path 10. The gas fuel injection tube 2, which is arranged around the solid fuel injection tube 1, defines a gas fuel flow path 20 (second flow path) through which gas fuel passes between the gas fuel injection tube 2 and the outer wall of the solid fuel injection tube 1, and injects gas fuel from a ring-shaped gas fuel discharge port 21 which is the tip of the gas fuel flow path 20. The combustion-supporting gas injection tube 3, which is arranged around the gas fuel injection tube 2, defines a combustion-supporting gas flow path 30 (third flow path) through which combustion-supporting gas passes between the combustion-supporting gas injection tube 3 and the outer wall of the gas fuel injection tube 2, and injects combustion-supporting gas from a ring-shaped combustion-supporting gas discharge port 31 which is the tip of the combustion-supporting gas flow path 30.
The tip of the auxiliary burner 100 is such that, the tips of the solid fuel injection tube 1 and the gas fuel injection tube 2 are located at the same position along the burner axis, and only the tip of the outermost combustion-supporting gas injection tube 3 protrudes by about 10 mm to 200 mm. The inner diameter of each of the injection tubes 1, 2 and 3 is not particularly limited; and generally, the inner diameter of the solid fuel injection tube 1 is about 10 mm to 40 mm, the inner diameter of the gas fuel injection tube 2 is about 20 mm to 60 mm, and the inner diameter of the combustion-supporting gas injection tube 3 is about 40 mm to 100 mm. Also, the thickness of each injection tube is not particularly limited, and is generally about 2 mm to 20 mm.
On the rear end side of the burner, a combustion-supporting gas supply port 32, through which combustion-supporting gas is supplied to the combustion-supporting gas flow path 30, is provided on the burner rear end side of the combustion-supporting gas injection tube 3. Similarly, a gas fuel supply port 22, through which gas fuel is supplied to the gas fuel flow path 20, is provided on the burner rear end side of the gas fuel injection tube 2. Also similarly, a solid fuel supply port 12, through which solid fuel is supplied along with carrier gas to the solid fuel flow path 10, is provided on the burner rear end side of the solid fuel injection tube 1.
A combustion-supporting gas supply mechanism (a combustion-supporting gas feeder being not illustrated), which supplies combustion-supporting gas to the combustion-supporting gas supply port 32, is connected to the combustion-supporting gas supply port 32. Also, a gas fuel supply mechanism (a gas fuel feeder being not illustrated), which supplies gas fuel to the gas fuel supply port 22, is connected to the gas fuel supply port 22. Additionally, a solid fuel supply mechanism and a carrier gas supply mechanism (a solid fuel feeder and a carrier gas feeder both being not illustrated), which supply solid fuel and carrier gas to the solid fuel supply port 12, is connected to the solid fuel supply port 12.
Further, although it is not illustrated, an inner tube and an outer tube are further arranged coaxially outside the combustion-supporting gas injection tube 3; and cooling fluid flow paths (a forward path and a return path for cooling fluid) communicating with each other are formed between the outer tube and the inner tube, and between the inner tube and the combustion-supporting gas injection tube 3.
Examples of fuels that can be used in the auxiliary burner of the present embodiment are as follows. Examples of the gas fuel include LPG (Liquefied Petroleum Gas), LNG (Liquefied Natural Gas), hydrogen, steelworks by-product gases (Cokes Oven gas, Blast Furnace gas and the like), and mixed gases including two or more thereof; and one or more thereof can be used. Further, examples of the solid fuel include powdered solid fuels such as coal (pulverized coal) and plastic (granular or powdery ones including waste plastic); and one or more thereof can be used. However, coal (pulverized coal) is particularly preferred. Furthermore, examples of the combustion-supporting gas include pure oxygen (industrial oxygen), oxygen-enriched air, and air; and anyone thereof may be used. However, pure oxygen is preferred. As the carrier gas, for example, nitrogen can be used.
[Reason for Setting Combustion-Supporting Gas Injection Tube as the Outermost Circumference]
The combustion-supporting gas has the largest flow rate among the supplied gas amount, and in order to match the flow speed thereof with that of other supplied gases (gas fuel and carrier gas), it is necessary to make the discharge area of the combustion-supporting gas discharge port 31 larger than that of the gas fuel discharge port 21 and the solid fuel discharge port 11. From the above viewpoint, it is optimal to set the combustion-supporting gas injection tube 3 as the outermost circumference. Hereinafter, an example in which oxygen as the combustion-supporting gas, LNG as the gas fuel, and pulverized coal as the solid fuel are used is described.
Initially, the amount of oxygen required for combustion is calculated by the following equation (1):
amount of oxygen required for combustion=oxygen ratio (coefficient)×[flow rate of LNG×theoretical oxygen amount of LNG+supply amount of pulverized coal×theoretical oxygen amount of pulverized coal] (1).
The amount of oxygen required for combustion is specifically calculated under the following conditions. That is, as calculation conditions, the amount of heat generated by LNG is set to 9700 kcal/Nm3, and the amount of heat generated by pulverized coal, the solid fuel, is set to 6250 kcal/kg. In addition, the total energy of the auxiliary burner is set such that, 90% thereof is supplied by the solid fuel, and 10% thereof is supplied by the gas fuel. For example, when LNG is supplied at 10 Nm3/h, the amount of heat generated is 97 Mcal/h. In this case, it is necessary to supply 873 Mcal/h, which is the difference from 970 Mcal/h, the total amount of heat to be generated by the burner, from pulverized coal, and therefore the supply amount of pulverized coal is about 140 kg/h. Further, the theoretical oxygen amount is calculated from the carbon content and the hydrogen content in the fuel; and particularly, the theoretical oxygen amount of LNG is about 2.25 Nm3/Nm3, and the theoretical oxygen amount of pulverized coal is about 1.5 Nm3/kg.
Generally, the oxygen ratio is under an oxygen excess condition of 1.0 to 1.1; and when the oxygen ratio is 1.05, the amount of oxygen required for combustion is calculated as 244 Nm3/h (=1.05×[10×2.25+140×1.5] according to the above equation (1). Accordingly, when pure oxygen is used, about 24.4 times the flow rate of the LNG fuel is necessary. In addition, compared with nitrogen for carrying the pulverized coal, the nitrogen flow rate is about 11 Nm3/h when the solid-gas ratio (supply speed of solids per unit time/supply speed of carrier gas per unit time) is 10, and therefore, about 22 times the flow rate is necessary. Accordingly, in order to make the discharge speed of oxygen equal to the discharge speed of fuel gas and pulverized coal, the combustion-supporting gas discharge port 31 needs to have a discharge area (radial cross-sectional area) 20 times or more that of the gas fuel discharge port 21 and the solid fuel discharge port 11. Therefore, in view of the layout of the burner, it is reasonable to arrange the combustion-supporting gas discharge port 31 at the outermost circumferential part of the burner. When air is used instead of pure oxygen as the combustion-supporting gas, a further 5 times the flow rate is necessary. Also in this case, it is reasonable to arrange the combustion-supporting gas discharge port 31 at the outermost circumferential part of the burner for the same reason.
[Swirl Vanes]
In the combustion-supporting gas flow path 30, a plurality of swirl vanes 4 for swirling (in the burner circumferential direction, which shall also apply thereafter) the combustion-supporting gas are provided at predetermined intervals in the circumferential direction thereof. By swirling the combustion-supporting gas, the solid fuel can be suitably and efficiently burned, and thereby the scrap heating effect is improved, and the flame temperature of the burner is homogenized. As a result, the scrap within the electric furnace can be efficiently heated or melted.
Elements necessary for combustion include combustible substance, oxygen, and temperature (fire source). Regarding the state of the combustible substance, the ease of combustion is in the order of gas, liquid and solid. This is because when the combustible substance is in a gaseous state, it is easy to mix the combustible substance with oxygen such that the combustion is continued (chain reaction).
When a gas fuel is burned as a combustible substance using an auxiliary burner, generally, the gas fuel burns immediately after being injected from the tip of the burner, although it depends on the oxygen concentration, the flow speed of the gas fuel, and the shape of the burner tip. On the other hand, when a solid fuel typified by coal is used as a combustible substance, it is difficult for it to burn as quickly as a gas fuel. This is due to the fact that it is necessary to maintain the ignition temperature of coal, which is about 400° C. to 600° C., and it takes time to raise the temperature up to the ignition temperature.
The heat-up time for a solid fuel to reach its ignition temperature depends on the particle size (specific surface area) of the solid fuel, and it is possible to shorten the ignition time by making the particles finer. This is because combustion reaction proceeds by maintaining the ignition temperature and reacting the combustible substance with oxygen. In order to efficiently proceed the combustion reaction, it is important to heat the coal efficiently and then react the coal with oxygen.
The auxiliary burner of the present embodiment, by swirling the gas, improves the aforementioned efficient heating of coal and reaction of a combustible substance and oxygen.
Hereinafter, an example in which LNG (Liquefied Natural Gas) as the gas fuel, coal (pulverized coal) as the solid fuel, and pure oxygen as the combustion-supporting gas are used is described. Note that the ignition temperature of fuel is generally solid fuel>liquid fuel>gas fuel.
When LNG and coal are used as the fuel of the auxiliary burner, a combustion field above the ignition temperature of coal is created due to the combustion of LNG and pure oxygen, and as the coal is fed into the combustion field, the temperature of the coal rises to the ignition temperature, and thus combustion of the coal (vaporization ignition) occurs. Although the flame temperature drops due to the fact that the amount of heat required to raise the temperature of the coal is consumed, the temperature rises in the region where ignition of the coal occurs.
The reaction of LNG and coal as the fuel and oxygen generates carbon dioxide, an incombustible gas. An incombustible gas inhibits continuation of combustion (chain reaction), which causes deterioration in combustibility. Further, the coal is supplied along with a carrier gas. When the flow rate of the carrier gas is high, the temperature drops corresponding to the specific heat of the carrier gas. Therefore, generally, the combustibility can be improved by increasing the solid-gas ratio. However, the state in which the solid-gas ratio is large is such that the coal is dense, and it is difficult for external heat and reaction with oxygen to be transmitted to the center part. In order to efficiently burn the coal, it is important to create a condition under which heat and oxygen are sufficiently present around the coal in the combustion field of the coal.
As a result of studies by the inventors, it was found that by swirling the oxygen under specific conditions, it is possible to create the condition under which heat and oxygen are sufficiently present around the coal in the combustion field. Thereby, the coal is efficiently heated, the coal (and the LNG) and the oxygen react rapidly, and the carbon dioxide generated by the reaction is diffused by the swirling of the oxygen. Therefore, the combustibility of the coal is improved.
That is, in the present embodiment, it is necessary that the plurality of swirl vanes 4 form an angle θ (see
No particular limitations are placed on the number and the thickness of the swirl vanes 4; however, in order to swirl the combustion-supporting gas sufficiently without disturbing the combustion-supporting gas flow and causing the vanes to deform, it is appropriate that the number of the swirl vanes 4 is 8 or more and 16 or less, and the thickness of the vanes is about 1 mm to 10 mm.
Also, no particular limitations are placed on the installation position of the swirl vanes in the burner axis direction, as long as they are within the combustion-supporting gas flow path 30; however, if they are located too far from the tip of the combustion-supporting gas flow path 30 (the combustion-supporting gas discharge port 31), there is a possibility that the intended swirl angle cannot be maintained before the combustion-supporting gas that has passed through the swirl vanes 4 mixes with the gas fuel. On the other hand, if the installation position of the swirl vanes 4 is too close to the tip of the combustion-supporting gas flow path 30 (the combustion-supporting gas discharge port 31), since the run-up time for maintaining the swirl angle is short, a swirl flow (combustion-supporting gas flow) holding the intended swirl angle is less likely to occur. Therefore, it is preferable that, the distance LB between the tip on the combustion-supporting gas discharge port 31 side of each swirl vane 4 and the combustion-supporting gas discharge port 31 in the burner axis direction is about 10 mm to 50 mm.
Further, it is preferable that each swirl vane 4 has a length LA of 40 mm or more in the burner axis direction, such that a stable swirl flow can be obtained. In addition, it is preferable that the length LA is 100 mm or less from the viewpoint of manufacturing cost of the vanes.
Furthermore, when each swirl vane 4 has a length Q in the circumferential direction of the combustion-supporting gas flow path 30 (the circumferential length), and the plurality of swirl vanes 4 have intervals P in the circumferential direction of the combustion-supporting gas flow path 30, it is preferable that Q/P (the lap ratio) is 1.0 or more and 1.2 or less. When Q/P is less than 1.0, it becomes difficult to swirl the gas flow, and as a result, it is difficult to homogenize the flame temperature. On the other hand, when Q/P exceeds 1.2, the resistance when the gas flows increases, such that the pressure loss against the gas flow becomes larger and it becomes difficult for the flow to flow. As a result, it is also difficult to homogenize the flame temperature. As illustrated in
Each of the swirl vanes 4 may be incorporated into the tube body (injection tube), or may be machined to have an integral structure with the tube body.
Further, according to the findings of the inventors, when the flow speed of the combustion-supporting gas discharged from the combustion-supporting gas discharge port 31 is less than 10 m/s, the combustion of the solid fuel tends to be inhomogeneous, and there is a possibility that a phenomenon in which the solid fuel remaining unburned clogs in the flow path occurs. Therefore, it is preferable that the discharge flow speed of the combustion-supporting gas is 10 m/s or more. The discharge flow speed S of the combustion-supporting gas is determined by the combustion-supporting gas flow rate H and the discharge area A (the radial cross-sectional area) of the combustion-supporting gas discharge port 31 (S=H/A). Therefore, it is preferable that the combustion-supporting gas discharge port 31 has a discharge area (radial cross-sectional area) such that the combustion-supporting gas discharge speed from the combustion-supporting gas discharge port at the minimum combustion-supporting gas supply amount is 10 m/s or more. Note that “the minimum supply amount” refers to the minimum supply amount at which the combustion of the solid fuel does not become inhomogeneous and the solid fuel remaining unburned does not clog in the flow path.
According to the auxiliary burner 100 of the present embodiment described above, by burning the solid fuel along with the gas fuel suitably and efficiently, the scrap heating effect is improved, and the flame temperature of the burner is homogenized. Besides, the auxiliary burner 100 of the present embodiment has the following additional effects. That is, in the present embodiment, by changing the ratio of the solid fuel to the total fuel (Generated heat amount conversion, and hereinafter simply referred to as “the solid fuel ratio”), it is possible to arbitrarily adjust the flame length according to the distance to the scrap to be heated or melted. Further, generally, since the gas flow speed in an auxiliary burner is relatively small, splashes of molten iron and molten slag splattered may clog the gas discharge ports; however, in the present embodiment, since the splashes are purged by the carrier gas of the solid fuel, clogging of the gas discharge ports due to splashes is less likely to occur.
Here, the flame length varies depending on the ignition temperature of the fuel used for the auxiliary burner. Since solid fuel and gas fuel have different ignition temperatures, by changing the solid fuel ratio, the flame length of the auxiliary burner (that is, the flame temperature at a certain distance away from the burner) can be arbitrarily adjusted.
As described above, in the auxiliary burner of the present embodiment, a combustion field above the ignition temperature of the solid fuel is created due to the combustion of the gas fuel and the combustion-supporting gas. As the solid fuel is fed into this combustion field, the temperature of the solid fuel rises to the ignition temperature, and combustion of the solid fuel (vaporization ignition) occurs. Although the flame temperature decreases due to the fact that the amount of heat required to raise the temperature of the solid fuel is consumed, the temperature rises in the region where ignition of the solid fuel occurs. Accordingly, the flame generated by the auxiliary burner of the present embodiment is such that, when the solid fuel ratio is low, positions near the tip of the burner become high temperature (that is, a short flame is generated); and when the solid fuel ratio is increased, positions far from the tip of the burner also become high temperature (that is, a long flame is generated) due to the heat generation of the solid fuel after heat absorption. Therefore, by changing the solid fuel ratio, the flame length (that is, the flame temperature at a certain distance away from the burner) can be controlled.
In the operation of the electric furnace, the distance between the auxiliary burner and the scrap varies due to charging, addition and melting of the scrap. Generally, the distance between the auxiliary burner and the scrap is small at the beginning of operation and at the initial stage after addition, and increases with the progress of melting of the scrap. This is because, the scrap is melted in order from the part near the auxiliary burner, such that the distance between the unmelted scrap and the auxiliary burner gets larger with the progress of melting of the scrap. In the auxiliary burner of the present embodiment, the flame length can be adjusted (changed) by changing the solid fuel ratio according to the distance to the scrap to be heated or melted, such that regardless of the distance between the scrap and the auxiliary burner, the flame can reach the scrap. That is, when the distance between the auxiliary burner and the scrap is small, the solid fuel ratio is decreased to shorten the flame length; and when the distance between the auxiliary burner and the scrap is large, the solid fuel ratio is increased to lengthen the flame length. Thereby, the scrap can be efficiently heated or melted.
Particularly, in general operation (one charge operation) of the electric furnace, scrap is charged about two to three times. Operation of the electric furnace after the first scrap charging begins when energizing starts or when the use of the auxiliary burner is started. As for the state at the start of operation, there are cases where some of the molten iron in the previous operation is left and molten metal exists in the lower part and where the molten iron in the previous operation is all discharged and the inside of the furnace is empty; however, there is no big difference in the operation method. At the initial stage after scrap charging, the bulk density is high and the whole electric furnace is filled with the scrap. Accordingly, the tip of the auxiliary burner is close to the scrap. The distance between the tip of the auxiliary burner and the scrap at the initial stage after scrap charging is about 0.5 m. This is because, when the tip of the auxiliary burner is too close to the scrap, splashes generated when the scrap melts will weld to the auxiliary burner. The position of the height of the tip of the auxiliary burner depends on the characteristics of the furnace; however, is generally 1 m or more above the height of molten metal surface after burn-through of the scrap.
As the operation proceeds, melting of the scrap proceeds from the lower part in contact with the molten iron, the vicinity of the electrode, and the vicinity of the auxiliary burner. At the initial stage after scrap charging, the top scrap falls with melting, and thus the scrap in the vicinity of the auxiliary burner always has a distance to the auxiliary burner of about 0.5 m; however, the distance increases when the top scrap runs out. Since the heat of the auxiliary burner cannot be efficiently supplied to the scrap when the distance to the scrap increases, conventionally, sometimes operation to stop the auxiliary burner was performed. On the other hand, in the operation using the auxiliary burner of the present embodiment, when the scrap is near, the solid fuel ratio is decreased to melt the scrap with a short flame; and when the distance to the scrap increases as the melting proceeds, the solid fuel ratio is increased to melt the scrap with a long flame. This makes it possible to melt more scrap efficiently and enables reduction of operation time and power consumption unit. The distance between the auxiliary burner and the scrap varies due to two to three times of scrap charging, and by appropriately changing the solid fuel ratio each time, the scrap can be efficiently melted.
In the case of the operation described above, it is necessary to grasp the distance between the auxiliary burner and the scrap; and for example, it is possible to install a laser range finder at the auxiliary burner, and measure the distance to the scrap by the laser range finder. Also, it is possible to observe the situation inside the furnace with a monitoring camera through a window such as a discharge port; and depending on the structure of the electric furnace, is possible to grasp the distance to the scrap through observation on the inside of the furnace by the monitoring camera. In addition, useful information for grasping the distance may be obtained from the operation data.
A steel plate was heated using an auxiliary burner having the structure illustrated in
LNG (gas fuel) and pulverized coal (solid fuel) were used as the fuel, and pure oxygen was used as the combustion-supporting gas. The pulverized coal was injected from the solid fuel injection tube at the center with nitrogen as the carrier gas, the LNG was injected from the gas fuel injection tube outside the solid fuel injection tube, and the pure oxygen was injected from the combustion-supporting gas injection tube outside the gas fuel injection tube (the outermost circumference).
The specifications of the pulverized coal are listed in Table 1. The LNG flow rate was 6.1 Nm3/h, the pulverized coal supply amount was 85 kg/h, the oxygen flow rate was 155 Nm3/h, and the flow rate of nitrogen for carrying the pulverized coal was 6.7 Nm3/h. The discharge area of the combustion-supporting gas discharge port 31 was 2064 mm2, and the oxygen flow speed calculated from the oxygen flow rate was 21 m/s. The solid fuel ratio was set to 90%. The blowing oxygen amount was calculated by the above equation (1) taking the oxygen ratio as 1.1.
The value of the angle θ of the swirl vanes provided in the flow path of the combustion-supporting gas injection tube and the value of Q/P were presented in Table 2 for each level. Note that, the swirl vanes with an angle of 0° are provided as members to coaxially hold the gas fuel injection tube 2 and the combustion-supporting gas injection tube 3, not for the purpose of swirling the combustion-supporting gas. Further, at all levels, the number of the swirl vanes was 8, LB was 40 mm, and P was 30 mm.
The steel plate used for the temperature measurement is SS400, having a size of 500 mm in length, 500 mm in width, and 4 mm in thickness. In order to measure the temperature of the steel plate, K type thermocouples were installed at five positions on the side opposite to the surface irradiated by the burner flame, with one at the center of the plate, one each at the positions 100 mm left and right from the center, and one each at the positions 200 mm left and right from the center. Further, a heat insulator (a fireproof board) having a thickness of 25 mm was installed on the steel plate surface side where the K type thermocouples were installed. The steel plate with this heat insulator was placed in a furnace (furnace temperature: room temperature) provided with an opening for introducing a burner flame on the front surface facing the auxiliary burner. The distance from the tip of the burner to the steel plate was set to be 1.0 m, assuming electric furnace operation. Burner ignition was taken as the start of the experiment, the outputs of the thermocouples installed on the steel plate were incorporated into a data logger, and the steel plate temperature was measured over time. The temperatures of the five thermocouples became constant about 10 minutes after the start of the experiment. These temperatures were taken as the maximum heating temperatures.
The maximum heating temperatures at the five points and the average temperature thereof are presented in Table 2 for each level. Also, as an index of the temperature variation of the five points, the values of (maximum temperature among the five points)−average temperature, and average temperature−(minimum temperature among the five points) are presented. Each value was judged to be defective when it exceeds 50° C.
As can be seen from Table 2, as for Sample No. 10 where the angle θ is 0°, although the average temperature of the five points was high, the variation thereof was extremely large due to poor and unstable combustibility of the pulverized coal. Therefore, the scrap cannot be homogeneously heated, and inhomogeneous melting of the scrap occurs.
On the other hand, as for Samples No. 1 to 5 where the angle θ is within the scope of the present disclosure, the average temperature of the five points was high, and the variation thereof was small. That is, it can be known that high combustibility was obtained by suitably and efficiently burning the pulverized coal. Therefore, the scrap within the furnace can be heated homogeneously in the electric furnace operation. Among Samples No. 1 to 5, as for Samples No. 2 to 4 where the angle θ of the swirl vanes was set to 10° or more and 30° or less, the average temperature of the five points was particularly high, and the variation thereof was particularly small. That is, it can be said that these are auxiliary burners having better performance.
On the other hand, as for Sample No. 11 where the angle θ of the swirl vanes is 60°, since the combustion-supporting gas diffused too much in the steel plate width direction, the average temperature of the five points was low, and similarly to Sample No. 10, the variation thereof was large. That is, it can be said that its capability as an auxiliary burner is low.
Further, comparing Samples No. 5 to 9 where the angle θ of the swirl vanes was fixed to 45° and the value of Q/P was variously changed, it can be seen that in Samples No. 5, 7 and 8 where the value of Q/P was set to 1.0 or more and 1.2 or less, the variation of the five points was particularly small.
The burner output of 590 Mcal/h in this test is the scale installed in an electric furnace of 60 t/ch, and the test was carried out on the actual machine scale. Therefore, it is obvious that the same effect can be expected also in an actual electric furnace.
According to the auxiliary burner of the present disclosure, it is possible to increase and homogenize the heating effect of iron scrap by suitably and efficiently burning the solid fuel along with the gas fuel.
| Number | Date | Country | Kind |
|---|---|---|---|
| JP2016-146540 | Jul 2016 | JP | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/JP2017/026716 | 7/24/2017 | WO | 00 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2018/021249 | 2/1/2018 | WO | A |
| Number | Name | Date | Kind |
|---|---|---|---|
| 3236280 | Greinke | Feb 1966 | A |
| 4367686 | Adrian | Jan 1983 | A |
| 4428727 | Deussner | Jan 1984 | A |
| 4464108 | Korenyi | Aug 1984 | A |
| 4523530 | Kaminaka | Jun 1985 | A |
| 4561841 | Korenyi | Dec 1985 | A |
| 4836772 | Larue | Jun 1989 | A |
| 4949655 | Greer | Aug 1990 | A |
| 5203692 | Wexoe | Apr 1993 | A |
| 5249535 | Chung | Oct 1993 | A |
| 5599375 | Gitman | Feb 1997 | A |
| 6116171 | Oota | Sep 2000 | A |
| 6684796 | Feldermann | Feb 2004 | B1 |
| 7289514 | Robotham et al. | Oct 2007 | B2 |
| 9671107 | Yamamoto et al. | Jun 2017 | B2 |
| 20070231761 | Rosen et al. | Oct 2007 | A1 |
| 20080044782 | Kostlin | Feb 2008 | A1 |
| 20090068601 | Londerville | Mar 2009 | A1 |
| 20090208889 | Pillard | Aug 2009 | A1 |
| 20100227284 | Daneri | Sep 2010 | A1 |
| 20120129111 | Robertson et al. | May 2012 | A1 |
| 20140157790 | Forsberg | Jun 2014 | A1 |
| 20140245742 | Chew | Sep 2014 | A1 |
| 20140311150 | Pinson | Oct 2014 | A1 |
| 20150010871 | Starcke | Jan 2015 | A1 |
| 20150047305 | Altorf | Feb 2015 | A1 |
| 20150176900 | Ka | Jun 2015 | A1 |
| 20160010856 | Biagioli | Jan 2016 | A1 |
| 20160195266 | Kim | Jul 2016 | A1 |
| 20160252246 | Arakawa et al. | Sep 2016 | A1 |
| 20180209639 | Mahe | Jul 2018 | A1 |
| 20180216814 | Londerville | Aug 2018 | A1 |
| Number | Date | Country |
|---|---|---|
| 204786421 | Nov 2015 | CN |
| 52090818 | Jul 1977 | JP |
| 55082211 | Jun 1980 | JP |
| S5719506 | Feb 1982 | JP |
| S5751204 | Mar 1982 | JP |
| 57150719 | Sep 1982 | JP |
| S5825098 | Feb 1983 | JP |
| S59134728 | Sep 1984 | JP |
| 60129518 | Jul 1985 | JP |
| S62225816 | Oct 1987 | JP |
| S6312923 | Mar 1988 | JP |
| H0712314 | Jan 1995 | JP |
| H109524 | Jan 1998 | JP |
| 2003004382 | Jan 2003 | JP |
| 2004100967 | Apr 2004 | JP |
| 2005283029 | Oct 2005 | JP |
| 2009532661 | Sep 2009 | JP |
| 2014185784 | Oct 2014 | JP |
| 2015136609 | Sep 2015 | WO |
| Entry |
|---|
| JP_07012314_A_M—Machine Translation.pdf, machine translation, J-PLAT—JPO.org, Jun. 22, 2020. |
| Aug. 21, 2018, Notification of Reasons for Refusal issued by the Japan Patent Office in the corresponding Japanese Patent Application No. 2017-559626 with English language Concise Statement of Relevance. |
| Oct. 3, 2017, International Search Report issued in the International Patent Application No. PCT/JP2017/026716. |
| Aug. 26, 2019, Office Action issued by the China National Intellectual Property Administration in the corresponding Chinese Patent Application No. 201780046453.X with English language concise statement of relevance. |
| Feb. 19, 2020, Office Action issued by the China National Intellectual Property Administration in the corresponding Chinese Patent Application No. 201780046453.X with English language concise statement of relevance. |
| A. H. Lefebvre et al., Gas Turbine Combustion (Third Edition), Dec. 31, 2016, pp. 114-120. |
| Feb. 19, 2019, Notification of Reasons for Refusal issued by the Japan Patent Office in the corresponding Japanese Patent Application No. 2017-559626 with English language concise statement of relevance. |
| Jun. 25, 2020, Office Action issued by the Korean Intellectual Property Office in the corresponding Korean Patent Application No. 10-2019-7004582 with English language concise statement of relevance. |
| Number | Date | Country | |
|---|---|---|---|
| 20190271465 A1 | Sep 2019 | US |
