CN209778917U - High-efficiency full-oxygen iron-smelting furnace - Google Patents
High-efficiency full-oxygen iron-smelting furnace Download PDFInfo
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- CN209778917U CN209778917U CN201920219602.4U CN201920219602U CN209778917U CN 209778917 U CN209778917 U CN 209778917U CN 201920219602 U CN201920219602 U CN 201920219602U CN 209778917 U CN209778917 U CN 209778917U
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Abstract
A high-efficiency total-oxygen iron-smelting furnace comprises a molten pool, a heat exchange reduction cylinder and a speed reduction filter cover which are sequentially connected from bottom to top, the whole furnace is arranged in a dumbbell shape, and the insides of the molten pool, the heat exchange reduction cylinder and the speed reduction filter cover are communicated with each other; the interior of the molten pool is divided into a molten iron layer, a slag layer coke layer and a combustion layer from bottom to top; the top of the heat exchange reduction cylinder is provided with at least two cold air spray guns, the middle upper part of the heat exchange reduction cylinder is provided with at least two first oxygen guns, a filter structure is arranged in the speed reduction filter cover, the filter structure is provided with a plurality of micropores and at least one filter material discharge hole, and the speed reduction filter cover is provided with a tail gas discharge hole and a filter material feed port; the mineral aggregate nozzle is arranged on the deceleration filter cover. The utility model solves the problems that the traditional blast furnace iron making can not use the total oxygen smelting and the reaction period is longer; solves the problems of uncontrollable reaction and longer reaction period of the existing smelting reduction process; the problem of unreasonable heat exchange in the flash iron-making process is solved.
Description
Technical Field
The utility model relates to the technical field of non-blast furnace ironmaking, in particular to a high-efficiency total-oxygen ironmaking furnace.
Background
Blast furnace iron making is a reduction smelting process in which iron ore is reduced into molten iron using coke as a heat generating agent and a reducing agent. The sintered ore and part of the massive iron ore, coke and flux are distributed from the top of the furnace according to a certain rule and then continuously descend, the high-temperature coal gas in the tuyere area moves from bottom to top, the furnace burden which slowly descends is heated in the upward movement process in the furnace, and the coal gas and the furnace burden in the blast furnace move in the reverse direction, so that the energy in the blast furnace is reasonably and fully utilized. However, the serious environmental pollution caused by iron ore powder agglomeration and coking and the global supply shortage of the scarce resource coking coal promote iron-making enterprises to try to get rid of the dependence on metallurgical coke, and further continuously develop the non-blast furnace smelting reduction iron-making technology. Many non-blast furnace smelting reduction iron making schemes have been proposed historically, but most of these schemes are not commercially viable, and some schemes, even if they are commercially viable, are not able to withstand practical inspections and are eliminated during development. The more mature melting reduction process today is the two-stage COREX process, as well as the FINEX process.
The COREX process has strict requirements on raw materials and fuels, has higher energy consumption of working procedures, has higher molten iron production cost and unit capacity investment compared with a blast furnace, and more or less COREX devices which are put into operation have the problems of high coal/coke consumption, high-quality sintered blocks and the like.
The pre-reduced fine ore of the smelting reduction gas making furnace of the FINEX process needs to be pressed into blocks and then enters the smelting reduction gas making furnace, so that the process links are multiple, the maintenance amount is large, the connection difficulty of the subsequent process is large, and the process energy consumption is higher than that of the traditional blast furnace iron making process.
The existing flash iron-making process in the test stage has the problems of over-small mineral powder particle size (average 0.074 mm), unreasonable heat exchange, high tail gas dust content, high tail gas temperature (higher than 600 degrees), high coal consumption and the like, so that the process energy consumption is higher than that of the COREX method and FINEX method.
Therefore, the existing iron-making means still needs to be improved.
SUMMERY OF THE UTILITY MODEL
The utility model provides a high-efficiency total oxygen ironmaking furnace, which can solve the problems that the traditional blast furnace can not use total oxygen smelting and the flow time is longer; the problem of low efficiency caused by uncontrollable reaction of COREX and FINEX in the existing melting reduction process can be solved; the method can solve the problem that the tail gas temperature is too high, about 1500 ℃, the mineral powder granularity is too small, and the tail gas dust is too high, which is more than 10 percent because the average particle size is 0.074mm, which is caused by unreasonable heat exchange in the flash iron-making process in the test stage.
The technical scheme of the utility model is that: the high-efficiency total-oxygen iron-smelting furnace comprises a molten pool, a heat exchange reduction cylinder and a speed reduction filter cover which are sequentially connected from bottom to top, the whole furnace is arranged in a dumbbell shape, and the interiors of the molten pool, the heat exchange reduction cylinder and the speed reduction filter cover are communicated with one another; at least one oxygen coal spray gun which is inclined downwards is arranged at the upper part of the molten pool, and at least one tapping hole and at least one slag discharging hole are arranged on the side surface of the lower part of the molten pool; the interior of the molten pool is divided into a molten iron layer, a slag layer coke layer and a combustion layer from bottom to top; the top of the heat exchange reduction cylinder is provided with at least two cold air spray guns, the middle upper part of the heat exchange reduction cylinder is provided with at least two first oxygen guns, and/or the bottom of the heat exchange reduction cylinder is provided with at least two second oxygen guns; the lower part of the speed reduction filter cover is in a funnel shape, the upper part of the speed reduction filter cover is in a segment shape or an inverted funnel shape, a filter structure for bearing filter materials is arranged in the speed reduction filter cover, a plurality of micropores for gas to pass through and at least one controllable filter material discharge hole are arranged on the filter structure, and a tail gas discharge port and a filter material feed port are arranged on the speed reduction filter cover above the filter structure; and a mineral aggregate nozzle is arranged on the speed reduction filter cover below the filter structure.
As an improvement to the utility model, the oxygen coal spray gun sprays the pulverized coal and oxygen in the melting pool 1500 generated by combustion of the combustion layer0a reducing gas of C or more, formed along the horizontal plane at 45 to 60 DEG0the coke layer and the slag layer are sprayed into the molten pool at a speed of 50 ~ 200m/s in an angle and obliquely downward, the reducing gas stirs the coke layer and the slag layer to provide melting heat for the interior of the molten pool, and the residual FeO in the slag layer is reduced.
As an improvement, the heat exchange reduction cylinder is of a cylindrical structure with a uniform cross section.
As an improvement to the utility model, the lower part of the molten pool is cylindrical or polygonal tube-shape, and the upper part of the molten pool is in a spherical segment shape, a conical shape or a polygonal cone shape.
As an improvement of the utility model, the oxygen coal spray guns are 1 to 32.
As an improvement of the utility model, the number of the tapholes is 1-4, and the number of the slag discharge holes is 1-4.
As the improvement of the utility model, the internal diameter of the molten pool is selected between 6 ~ 20 meters, and the height of the molten pool is selected between 4 ~ 6 meters.
As an improvement of the utility model, the number of the cold air spray guns 21 is 2-8.
As an improvement of the utility model, the number of the first oxygen lances is 2 to 8.
As an improvement of the utility model, the number of the second oxygen lances is 2 to 4.
As an improvement, the inner diameter of the heat exchange reduction cylinder is 0.5 ~ 0.9 times of the inner diameter of the molten pool.
As right the utility model discloses an improvement, the internal diameter of a heat transfer reduction section of thick bamboo selects between 2 ~ 16 meters, the height of a heat transfer reduction section of thick bamboo selects between 5 ~ 30 meters.
As an improvement of the utility model, a plurality of fin-shaped guide plates are arranged in the heat exchange reduction cylinder along the radial direction, a plurality of layers of fin-shaped guide plates are arranged in the heat exchange reduction cylinder along the axial direction, and the fin-shaped guide plates between adjacent layers are distributed in a staggered way; the airflow generates airflow with specific flow speed and direction under the disturbance of the fin-shaped guide plate.
As an improvement of the utility model, the number of the fin-shaped guide plates arranged in the radial direction is selected from 10 ~ 100.
As the improvement of the utility model, the number of piles of the fin-shaped guide plate that sets up along the axial is selected between 2 ~ 20 layers.
As an improvement to the present invention, the first oxygen gun horizontally deflects 30-60% along the radial direction of the plane where the first oxygen gun is located0。
As an improvement of the utility model, the second oxygen gun horizontally deflects 30 ~ 60 degrees along the radial direction of the plane where the second oxygen gun is located0。
As an improvement of the utility model, the cooling medium sprayed by the cold air spray gun is normal temperature nitrogen or coal gas.
as right the utility model discloses an improvement, the filter media dog-house is 2 ~ 8, is cyclic annular setting.
As an improvement of the utility model, the number of the mineral aggregate nozzles is 2-8, and the mineral aggregate nozzles are arranged in a ring shape;
As the improvement of the utility model, the internal diameter of the deceleration filter mantle is selected between 6 ~ 20 meters, and the height of the deceleration filter mantle is selected between 6 ~ 10 meters.
As a pair of the improvement of the utility model, the maximum inner diameter of the speed reduction filter cover is 1.2 ~ 2 times of the inner diameter of the heat exchange reduction cylinder, and the gas flowing into the speed reduction filter cover from the heat exchange reduction cylinder is discharged from a tail gas discharge port after being subjected to speed reduction filtration in the speed reduction filter cover.
As the improvement of the utility model, the controllable filter material discharge holes are 2 ~ 8.
As an improvement, the thickness of the filter material is selected between 1 ~ 3 meters.
As an improvement of the utility model, the filter material is coke or porous ceramic.
As an improvement ~ the present invention, the average particle size of the mineral aggregate is selected between 0.1 ~ 1 mm.
As an improvement of the utility model, the device also comprises a furnace pressure and flow rate control system, wherein the furnace pressure and flow rate control system comprises a control unit, a gas pressure sensor, a gas flow rate sensor, a tail gas discharge outlet regulating valve, a first actuating mechanism, a second actuating mechanism and a third actuating mechanism; the gas pressure sensor and the gas flow velocity sensor are arranged in the heat exchange reduction cylinder and are electrically connected with the control unit; and after receiving the real-time pressure value and the real-time flow velocity value respectively transmitted by the gas pressure sensor and the gas flow velocity sensor, the control unit compares the real-time pressure value and the real-time flow velocity value with a standard pressure value and a standard flow velocity value which are prestored in the control unit, and controls the tail gas discharge port regulating valve, the first executing mechanism, the second executing mechanism and the third executing mechanism to work respectively or simultaneously according to a comparison result so as to keep the pressure and the flow velocity in the heat exchange reduction cylinder in a normal working state.
as right the utility model discloses an improvement, the normal operating pressure in the heat transfer reduction section of thick bamboo is 0 ~ 5 atmospheric pressure.
The utility model solves the problems that the traditional blast furnace iron making can not use the total oxygen smelting and the flow time is long (several hours); solves the problems of low efficiency (the pressure, the flow rate and the reaction process in the furnace can not be quickly regulated and controlled) caused by uncontrollable reaction of the existing melting reduction process (COREX and FINEX); the utility model adopts the cold air spray gun to spray cooling medium to the upper part in the heat exchange reduction cylinder according to the requirement, so that the temperature of the upper part in the heat exchange reduction cylinder is in the specified requirement, such as 300 ℃, thereby solving the problem that the tail gas temperature is too high (about 1500 ℃) caused by unreasonable heat exchange in the flash iron-making process in the test stage; by adopting the filter layer and controlling the granularity of the mineral aggregate within the range of 0.1-1mm, the engineering problems of overhigh tail gas dust (more than about 10 percent) and the like caused by the undersize (average 0.074 mm) of the mineral powder in the flash iron-making process can be solved.
Drawings
Fig. 1 is a schematic sectional structure diagram of an embodiment of the present invention.
Fig. 2 is a schematic front view of the embodiment shown in fig. 1.
Fig. 3 is a schematic perspective view of the embodiment shown in fig. 1.
FIG. 4 is a schematic top view of the molten bath in the embodiment of FIG. 1.
3 fig. 35 3 is 3 a 3 schematic 3 sectional 3 structure 3 view 3 a 3- 3 a 3 of 3 fig. 34 3. 3
Fig. 6 is a schematic perspective view of fig. 4.
Fig. 7 is a schematic top view of the heat exchange reduction drum in the embodiment shown in fig. 1.
Fig. 8 is a schematic sectional structure view of B-B of fig. 7.
Fig. 9 is a schematic perspective view of fig. 7.
FIG. 10 is a schematic top view of the speed reducing filter housing in the embodiment of FIG. 1.
Fig. 11 is a schematic cross-sectional structure view of fig. 10C-C.
Fig. 12 is a schematic perspective view of fig. 10.
FIG. 13 is a schematic top view of the filter arrangement in the speed reduction filter cage of FIG. 10.
Fig. 14 is a schematic sectional view of D-D in fig. 13.
Fig. 15 is a schematic front view of the structure of fig. 13.
FIG. 16 is a schematic view of an oxygen lance layout of the present invention.
Fig. 17 is a block diagram of the furnace pressure and flow rate control system of the present invention.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present invention, and should not be construed as limiting the present invention.
In the description of the present invention, it is to be understood that the terms "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships illustrated in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, unless otherwise specified and limited, it is to be noted that the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, mechanically or electrically connected, or may be connected between two elements through an intermediate medium, or may be directly connected or indirectly connected, and specific meanings of the terms may be understood by those skilled in the art according to specific situations.
Referring to fig. 1-12, fig. 1-12 disclose a high-efficiency total oxygen ironmaking furnace, which comprises a molten pool 1, a heat exchange reduction cylinder 2 and a speed reduction filter housing 3 which are sequentially connected from bottom to top, and the whole furnace is arranged in a dumbbell shape, wherein the molten pool 1, the heat exchange reduction cylinder 2 and the speed reduction filter housing 3 are communicated with each other; 8 downward-inclined oxygen coal lances 111 are arranged at the upper part 11 of the molten pool 1 (of course, the number of the oxygen coal lances 111 can be selected from positive integers of more than 1 according to requirements), and 4 tapholes 121 (more than one taphole 121 can be arranged according to requirements) and 4 deslagging ports 122 (more than one deslagging port 122 can be arranged according to requirements) are arranged at the side surface of the lower part 12 of the molten pool 1; the interior 13 of the molten pool 1 is divided into a molten iron layer 131, a slag layer 132, a coke layer 133 and a combustion layer 134 from bottom to top; 4 cold air lances 21 are arranged at the top of the heat exchange reduction cylinder 2 (the cold air lances 21 can be selected from positive integers of more than 2 as required), 8 first oxygen lances 22 are arranged at the middle upper part of the heat exchange reduction cylinder 2 (the first oxygen lances 22 can be selected from positive integers of more than 2 as required), and/or 4 second oxygen lances 23 are arranged at the bottom of the heat exchange reduction cylinder 2 (the second oxygen lances 23 can be selected from positive integers of more than 2 as required); the lower part 31 of the deceleration filter cover 3 is in a funnel shape, the upper part 32 of the deceleration filter cover 3 is in a segment shape or an inverted funnel shape, a filter structure 34 (see fig. 10-15) for carrying filter materials 33 is arranged in the deceleration filter cover 3, a plurality of micropores 341 and 5 controllable filter material discharge holes 342 (see fig. 13-15) for allowing gas (gas refers to high-temperature gas from a molten pool) to pass through are arranged on the filter structure 34, in the embodiment, the filter structure 34 is in a pot shape, the micropores 341 and the controllable filter material discharge holes 342 are arranged on a pot bottom (fig. 13 is convenient for view, only part of the micropores 341 are drawn, actually, the micropores 341 are fully distributed on the whole pot bottom), filter materials 33 are arranged in the pot, and 1 tail gas discharge port 35 and 4 filter material feed ports 36 are arranged on the deceleration filter cover 3 above the filter structure 34 (the filter material feed ports 36 can be set to be more than one as required); the decelerating filter casing 3 below the filter structure 34 is provided with 4 mineral aggregate nozzles 37 (the number of mineral aggregate nozzles 37 may be set to one or more as required).
The utility model adopts the structure that the whole body of the molten pool 1, the heat exchange reduction cylinder 2 and the deceleration filter cover 3 which are connected in sequence from bottom to top are arranged in a dumbbell shape, and oxygen lances are arranged at the middle upper part or/and the bottom of the heat exchange reduction cylinder 2, thereby solving the problem of longer smelting period (4-6 hours) of the traditional blast furnace ironmaking; the utility model can adjust the gas pressure and gas flow velocity in the furnace by increasing the structure of the furnace pressure and flow velocity control system 4, is used for controlling the falling speed of mineral aggregate and controlling the reaction time, and solves the problem of low efficiency (the pressure, flow velocity and reaction process in the furnace can not be quickly controlled) caused by uncontrollable reaction of the existing melting reduction process (COREX and FINEX); the utility model adopts the cold air spray gun to spray cooling medium to the upper part in the heat exchange reduction cylinder according to the requirement, so that the temperature of the upper part in the heat exchange reduction cylinder is in the specified requirement, such as 300 ℃, thereby solving the problem that the tail gas temperature is too high (about 1500 ℃) caused by unreasonable heat exchange in the flash iron-making process in the test stage; by adopting the filter layer and controlling the granularity of the mineral aggregate within the range of 0.1-1mm, the engineering problems of overhigh tail gas dust (more than about 10 percent) and the like caused by the undersize (average 0.074 mm) of the mineral powder in the flash iron-making process can be solved.
preferably, the oxygen coal spray gun 21 sprays pulverized coal and oxygen in the molten pool 1, and reducing gas with the temperature of more than 1500 ℃ generated by combustion of the combustion layer 134 forms 45-60 degrees along the horizontal plane0the coke layer 133 and the slag layer 132 are sprayed into the molten pool 1 at a speed of 50 ~ 200m/s in an inclined downward mode, the reducing gas stirs the coke layer 133 and the slag layer 132 to provide melting heat for the interior of the molten pool 1 and reduce residual FeO in the slag layer 132, and therefore dust generation can be reduced, and the yield of iron can be improved.
Preferably, the heat exchange reduction cylinder 2 is a cylindrical structure with an equal cross section, and is designed to be a cylindrical structure with an equal cross section, so that the rising of high-temperature reducing gas is facilitated, the heat exchange of the filter material and the mineral aggregate from top to bottom is accelerated, and the reduction reaction of the mineral aggregate is accelerated.
Preferably, the lower portion 12 of the molten bath 1 is cylindrical or polygonal, and the upper portion 11 of the molten bath 1 is spherical, conical or polygonal.
Preferably, the number of the oxygen coal spray guns is 1-32.
preferably, the number of the tapholes 121 is 1 to 4, and the number of the slag discharge holes 122 is 1 to 4.
preferably, the inner diameter of the molten pool 1 is selected from 6 ~ 20 meters, and the height of the molten pool 1 is selected from 4 ~ 6 meters.
Preferably, the number of the cold air spray guns 21 is 2-8.
Preferably, the number of the first oxygen guns 22 is 2 to 8.
Preferably, the number of the second oxygen lances 23 is 2-4.
preferably, the inner diameter of the heat exchange reduction cylinder 2 is 0.5 ~ 0.9 times of the inner diameter of the molten pool 1, so that the reduction gas can rise.
preferably, the inner diameter of the heat exchange reduction cylinder 2 is selected from 2 ~ 16 meters, and the height of the heat exchange reduction cylinder 2 is selected from 5 ~ 30 meters, which can be selected according to actual conditions.
Preferably, a plurality of fin-shaped guide plates 24 are arranged in the heat exchange reduction cylinder 2 along the radial direction, a plurality of layers of fin-shaped guide plates 24 are arranged in the heat exchange reduction cylinder 2 along the axial direction, and the fin-shaped guide plates 24 between the adjacent layers are distributed in a staggered manner; the airflow is disturbed by the fin-shaped guide plate 24 to generate airflow with a specific flow speed and direction, such as an S-shaped ascending airflow or a circular ascending rotating ascending airflow. The structure of the fin-shaped guide plate 24 is added, so that the detention time of the reducing gas rising at high temperature in the heat exchange reduction cylinder 2 can be prolonged, and the purposes of increasing the heat exchange time and the reaction time are achieved.
preferably, the number of the radially arranged fin-shaped deflectors 24 is selected from 10 to 100.
preferably, the number of layers of the fin-shaped guide plate 24 arranged along the axial direction is selected from 2 to 20.
preferably, the horizontal deflection included angle alpha of the first oxygen gun 22 along the radial direction of the plane on which the first oxygen gun is arranged is 30-60 DEG0the second oxygen gun 23 horizontally deflects along the radial direction of the plane where the second oxygen gun is located by an included angle alpha of 30-60 degrees0. By adopting the design, after oxygen enters the heat exchange reduction cylinder 2, the oxygen can quickly form a ring flow state so as to increase the reaction time of mineral aggregate (see fig. 16).
Preferably, the cooling medium injected by the cold air spray gun 21 is normal-temperature nitrogen or coal gas.
preferably, the number of the filter material feeding ports 36 is 2 ~ 8, and the filter material feeding ports are annularly arranged.
Preferably, the number of the mineral aggregate nozzles 37 is 2-8, and the mineral aggregate nozzles are arranged annularly;
preferably, the inner diameter of the deceleration filter housing 3 is selected from 6 ~ 20 meters, and the height of the deceleration filter housing 3 is selected from 6 ~ 10 meters.
preferably, the maximum inner diameter of the speed reduction filter housing 3 is 1.2 ~ 2 times of the inner diameter of the heat exchange reduction cylinder, and gas flowing into the speed reduction filter housing from the heat exchange reduction cylinder is subjected to speed reduction filtration in the speed reduction filter housing and then is discharged from a tail gas discharge port 35.
preferably, the number of the controllable filter material discharge holes 342 is 2 ~ 8.
preferably, the thickness of the filter medium 33 is selected from 1 to 3 meters, and the filter medium 33 is coke or porous ceramic, when the filter medium 33 is coke, on one hand, the coke can be used for adsorbing dust in high-temperature gas, and on the other hand, the coke can be used as a carburization and reduction material for supplementing a coke layer of the smelting furnace 1.
the average particle size of the mineral aggregate is preferably selected from 0.1 ~ 1mm, and the average particle size of the mineral aggregate is determined to be 0.1 ~ 1mm, because a large number of tests show that the mineral aggregate particle size in the range can realize rapid reaction (reaction time is about more than ten seconds) and can smoothly fall, so that the industrial process can be realized, and in addition, when the particle size is less than 0.1mm, the mineral aggregate can become floating dust and can not fall, so that the realization of the industrial process is influenced.
Referring to fig. 17, the present invention further includes a furnace internal pressure and flow rate control system 4, wherein the furnace internal pressure and flow rate control system 4 includes a control unit 41, a gas pressure sensor 42, a gas flow rate sensor 43, a tail gas discharge port regulating valve 44, a first actuator 45, a second actuator 45 and a third actuator 45; the gas pressure sensor 42 and the gas flow velocity sensor 43 are arranged in the heat exchange reduction cylinder 2 and are electrically connected with the control unit 41; after receiving the real-time pressure value and the real-time flow rate value respectively transmitted by the gas pressure sensor 42 and the gas flow rate sensor 43, the control unit 41 compares the real-time pressure value and the real-time flow rate value with a standard pressure value and a standard flow rate value prestored in the control unit 41, and controls the tail gas discharge port regulating valve 44, the first executing mechanism 45, the second executing mechanism 45 and the third executing mechanism 45 to work respectively or simultaneously according to the comparison result, wherein the first executing mechanism 45, the second executing mechanism 45 and the third executing mechanism 45 respectively control the cold gas spray gun 21, the oxygen coal spray gun 111 and the first oxygen gun 22/the second oxygen gun 23 to work, and the pressure and the flow rate in the heat exchange reduction cylinder 2 are kept in a normal working state.
As shown in fig. 17, when the control unit 41 detects a pressure decrease, it gives a command to decrease the flow rate to the exhaust gas discharge port regulating valve 44, and increases the pressure by a smaller flow rate; otherwise, an instruction for increasing the flow is sent. When the control unit 41 detects that the flow velocity of the gas flow in the heat exchange reduction cylinder 2 is too high, an instruction for reducing the injection amount of the oxygen coal is sent to the oxygen coal gun, the flow velocity of the gas is reduced, and the pressure is synchronously reduced; the pressure drop will trigger the regulator valve action to reduce the flow boost pressure. On the contrary, the oxygen coal injection amount is increased, so that the flow rate and the pressure are increased. Similarly, the disturbance of the cold air and the oxygen lance on the flow and the pressure can be controlled by the regulating valve.
preferably, the normal operating pressure in the heat exchange reduction cylinder 2 is 0 ~ 5 atmospheric pressures, the operating pressure is determined according to the production efficiency, and the production efficiency is in direct proportion to the pressure.
Claims (16)
1. The utility model provides a high-efficient total oxygen ironmaking stove which characterized in that: the device comprises a molten pool (1), a heat exchange reduction cylinder (2) and a speed reduction filter cover (3) which are sequentially connected from bottom to top, the whole device is arranged in a dumbbell shape, and the molten pool (1), the heat exchange reduction cylinder (2) and the speed reduction filter cover (3) are communicated with each other; at least one oxygen coal spray gun (111) which is inclined downwards is arranged at the upper part (11) of the molten pool (1), and at least one tapping hole (121) and at least one slag discharging hole (122) are arranged on the side surface of the lower part (12) of the molten pool (1); the interior (13) of the molten pool (1) is divided into a molten iron layer (131), a slag layer (132), a coke layer (133) and a combustion layer (134) from bottom to top; at least two cold air spray guns (21) are arranged at the top of the heat exchange reduction cylinder (2), at least two first oxygen guns (22) are arranged at the middle upper part of the heat exchange reduction cylinder (2), and/or at least two second oxygen guns (23) are arranged at the bottom of the heat exchange reduction cylinder (2); the lower part (31) of the speed reduction filter cover (3) is in a funnel shape, the upper part (32) of the speed reduction filter cover (3) is in a segment shape or an inverted funnel shape, a filter structure (34) for bearing filter materials (33) is arranged in the speed reduction filter cover (3), a plurality of micropores (341) for allowing gas to pass and at least one controllable filter material discharge hole (342) are formed in the filter structure (34), and a tail gas discharge port (35) and a filter material feeding port (36) are formed in the speed reduction filter cover (3) above the filter structure (34); and a mineral aggregate nozzle (37) is arranged on the deceleration filter cover (3) below the filter structure (34).
2. The high efficiency total oxygen ironmaking furnace of claim 1, characterized in that: the pulverized coal and the oxygen which are injected into the molten pool (1) by the oxygen-coal injection gun (111) are burnt in the burning layer (134) to generate 15000a reducing gas of C or more, formed along the horizontal plane at 45 to 60 DEG0the coke layer (133) and the slag layer (132) in the molten pool (1) are sprayed into the molten pool (1) at a speed of 50 ~ 200m/s in an inclined downward mode, the reducing gas stirs the coke layer (133) and the slag layer (132) to provide melting heat for the interior of the molten pool (1), and residual FeO in the slag layer (132) is reduced.
3. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: the heat exchange reduction cylinder (2) is of a cylindrical structure with an equal section.
4. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: the lower part (12) of the molten pool (1) is cylindrical or polygonal cylindrical, and the upper part (11) of the molten pool (1) is in a spherical segment shape, a conical shape or a polygonal cone shape.
5. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: the number of the oxygen coal spray guns is 1-32.
6. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: the number of the iron outlets is 1-4, and the number of the slag outlets is 1-4.
7. the high-efficiency total oxygen ironmaking furnace according ~ claim 1 or 2, characterized in that the inner diameter of the molten pool (1) is selected from 6 ~ 20 meters, and the height of the molten pool (1) is selected from 4 ~ 6 meters.
8. the high ~ efficiency total ~ oxygen ironmaking furnace according to claim 1 or 2, characterized in that the inner diameter of the heat exchange reduction cylinder (2) is 0.5 ~ 0.9 times of the inner diameter of the molten pool (1).
9. the high-efficiency total-oxygen ironmaking furnace according ~ claim 1 or 2, characterized in that the inner diameter of the heat exchange reduction cylinder (2) is selected from 2 ~ 16 meters, and the height of the heat exchange reduction cylinder (2) is selected from 5 ~ 30 meters.
10. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: a plurality of fin-shaped guide plates (24) are arranged in the heat exchange reduction cylinder (2) along the radial direction, a plurality of layers of fin-shaped guide plates (24) are arranged in the heat exchange reduction cylinder (2) along the axial direction, and the fin-shaped guide plates (24) between the adjacent layers are distributed in a staggered manner; the airflow generates airflow with specific flow speed and direction under the disturbance of the fin-shaped guide plate (24).
11. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: the cooling medium sprayed by the cold air spray gun (21) is normal-temperature nitrogen or coal gas.
12. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: the number of the mineral aggregate nozzles (37) is 2-8, and the mineral aggregate nozzles are arranged annularly.
13. the high-efficiency total-oxygen ironmaking furnace according ~ claim 1 or 2, characterized in that the inner diameter of the speed-reducing filter hood (3) is selected from 6 ~ 20 meters, and the height of the speed-reducing filter hood (3) is selected from 6 ~ 10 meters.
14. the high ~ efficiency total ~ oxygen ironmaking furnace according to claim 1 or 2, characterized in that the maximum inner diameter of the speed ~ reducing filter cover (3) is 1.2 ~ 2 times of the inner diameter of the heat exchange reduction cylinder, and gas flowing into the speed ~ reducing filter cover from the heat exchange reduction cylinder is subjected to speed reduction filtration in the speed ~ reducing filter cover and then discharged from an exhaust port.
15. the high ~ efficiency total ~ oxygen ironmaking furnace according to claim 1 or 2, characterized in that the average particle size of the ore material is selected from 0.1 ~ 1 mm.
16. The high efficiency total oxygen ironmaking furnace of claim 1 or 2, characterized in that: the system is characterized by further comprising a furnace pressure and flow rate control system (4), wherein the furnace pressure and flow rate control system (4) comprises a control unit (41), a gas pressure sensor (42), a gas flow rate sensor (43), a tail gas discharge port regulating valve (44), a first actuator (45), a second actuator (46) and a third actuator (47); the gas pressure sensor (42) and the gas flow velocity sensor (43) are arranged in the heat exchange reduction cylinder (2) and are electrically connected with the control unit (41); after receiving the real-time pressure value and the real-time flow velocity value respectively transmitted by the gas pressure sensor (42) and the gas flow velocity sensor (43), the control unit (41) compares the real-time pressure value and the real-time flow velocity value with a standard pressure value and a standard flow velocity value prestored in the control unit (41), and controls the tail gas discharge port regulating valve (44), the first executing mechanism (45), the second executing mechanism (46) and the third executing mechanism (47) to work respectively or simultaneously according to a comparison result, so that the pressure and the flow velocity in the heat exchange reduction cylinder (2) are kept in a normal working state.
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| CN109666771A (en) * | 2019-02-21 | 2019-04-23 | 前海红波(深圳)科技有限公司 | Efficient total oxygen iron-smelting furnace |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109666771A (en) * | 2019-02-21 | 2019-04-23 | 前海红波(深圳)科技有限公司 | Efficient total oxygen iron-smelting furnace |
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Address after: 100800 1106, floor 11, NO.67 Fucheng Road, Haidian District, Beijing Patentee after: Beijing Shantie Technology Co., Ltd. Address before: Room 01 and 15, 14th floor, Block B, Tiangong Building, 30 College Road, Haidian District, Beijing, 100800 Patentee before: Beijing Sparkling Iron Technology Co., Ltd. |
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