CN115679029B - Large-speed-difference stirring spouted fluidized bed for iron ore hydrogen-rich reduction - Google Patents

Large-speed-difference stirring spouted fluidized bed for iron ore hydrogen-rich reduction Download PDF

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CN115679029B
CN115679029B CN202310009638.0A CN202310009638A CN115679029B CN 115679029 B CN115679029 B CN 115679029B CN 202310009638 A CN202310009638 A CN 202310009638A CN 115679029 B CN115679029 B CN 115679029B
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fluidized bed
difference
speed
gas
reduction
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CN115679029A (en
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李雷
陈伟
刘志浩
石新苹
陈小梅
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Tangshan Jingyan Co ltd LLC
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Tangshan Jingyan Co ltd LLC
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Abstract

The invention discloses a large-speed-difference stirring spouted fluidized bed for hydrogen-rich reduction of iron ore, and relates to the technical field of fluidized beds for reduction of iron ore. The device comprises a motion mechanism, a large-speed-difference fluidized bed and a temperature-adjusting belt furnace body, wherein the large-speed-difference fluidized bed is connected in series with one stage or more than two stages; the movement mechanism arranged on the furnace top comprises a pipe shaft group, the lower part of the pipe shaft group is connected with the serial large-speed-difference fluidized bed, and the lower end of the large-speed-difference fluidized bed at the bottom is connected with the furnace body of the temperature adjusting zone; the upper end of the top large-speed-difference fluidized bed is provided with a mineral powder feeding port and a tail gas discharging port, and the side wall of the middle and/or lower large-speed-difference fluidized bed is connected with a heat supplementing gas pipe. The coal gas which is obtained by high-temperature reforming of oxygen-enriched high-air temperature air or a pure oxygen smelting reduction furnace and is added with hydrogen and even pure hydrogen is directly used as reducing gas, and the produced sponge iron granules are directly discharged into the smelting reduction furnace or a sponge iron sealing discharge system from the upper part, so that the intermediate transportation process and heat dissipation loss of the sponge iron granules in other processes are avoided, and the energy utilization rate is improved.

Description

Large-speed-difference stirring spouted fluidized bed for iron ore hydrogen-rich reduction
Technical Field
The invention relates to the technical field of fluidized beds for iron ore reduction, in particular to a large-speed-difference stirring spouted fluidized bed for hydrogen-rich reduction of iron ore.
Background
The iron ore fluidized bed reduction device can directly use fine ore to make iron when in normal operation, avoids the energy consumption and pollution of coking, sintering and pelletizing processes, determines the main production indexes of the smelting reduction and direct reduction processes by the performance of the iron ore fluidized bed reduction device, and has decisive significance for (pure) hydrogen-rich metallurgy, energy conservation and carbon reduction, reduction of the total pollutant production amount, and even success or failure of the smelting reduction process. At present, the research of the iron ore fluidized bed melting reduction and direct reduction process and device mainly solves the significant international problem of mineral powder bonding and defluidization in the reduction process.
Chinese patent publication No. CN103695588A discloses a system and method for reducing powdered iron ore by a fluidized bed, which adopts a three-stage cyclone preheater and a transverse multi-stage bubbling fluidized bed for burning and heating coal gas to 650 to 750 ℃ to dry, preheat and preliminarily reduce the ore powder, thereby improving the heat energy utilization rate and preheating effect of tail gas, and then performing three-stage high-flow-rate 5 to 10m/s circulating fluidized bed reduction at 800 to 900 ℃, wherein the three-stage circulating fluidized bed adopts independently heated high-concentration coal gas to supply gas in parallel, the reduction degree can reach 83.5 to 96.3 percent, and the system and method are suitable for operation under the pressure of 1 atm. The process actually sacrifices partial gas energy utilization rate (including chemical energy and heat energy) to obtain higher reduction speed of the mineral powder, the economy needs to be further researched, and the temperature and the components of the tail gas of the transverse multistage bubbling fluidized bed and the tail gas of the second and third circulating fluidized beds of the process are greatly different, so that the waste heat recovery and the coal gas recycling efficiency are adversely affected.
Patent document CN103725819A discloses a method for oxidizing and roasting exhaust gas at 850-950 ℃ by using completely combusted exhaust gas, and the exhaust gas is treated separately, so the situation is improved, but the whole process system is huge and complex, most of the exhaust gas needs to be subjected to waste heat recovery, the heat dissipation area is too large, the heat loss is increased, and the economical efficiency is also affected.
The Beijing university of science and technology, guohongjie and Li Lin, issued an article named as future of non-coking coal ironmaking process and equipment, analyzed Finex, HIsarna and HIsmelt, and indicated that Finex is the only flow which can stably realize large-scale production, and has the advantages that the gas generated by a final reduction furnace is reformed to remove CO 2 Then enters the fluidized bed, and improves the pre-reduction degree of the fluidized bed. The granularity of the used mineral powder is 0-8 mm, the average grain size is 0.90-3.64 mm, -0.125mm accounts for 4.9-12.68%, the coarse mineral powder plays a great role in reducing the cohesive loss flow in the fluidized bed reduction process, but the cohesive loss flow cannot be completely solved, the cohesive loss flow still has a great threat to the production stability and the popularization of Finex, in addition, the heat of a multistage reduction fluidized bed (belonging to a more conventional bed type) of the Finex process is insufficient, part of reduction gas needs to be combusted for heat supplement, the reduction potential and the reduction speed of the gas are greatly reduced, and the energy consumption of the whole Finex process is increased.
The system introduces the advantages and disadvantages of a gas separation plate, a spouted bed, a spouted fluidized bed, a stirred spouted bed and a three-phase spouted bed of various fluidized beds and design points of a fluidized bed handbook written by the institute of Process engineering of Chinese academy of sciences, guosun, etc.; it is proposed that the collision friction of the particles in the stirring paddle and high-speed spouting prevents the agglomeration and cohesion of the particles and easily maintains and improves the fluidized state, which is very useful for some special particle processing requiring simultaneous drying (including spray granulation with paste-like or suspension slurry, coating, etc.) and pulverization, iron ore reduction, shale pyrolysis, coal coking processes. Although there is a certain cohesive material treatment in the drying and granulating process, it has better industrial application performance, at present there is no further successful case for industrial application in iron ore powder reduction, and the introduced gas distribution plate has larger air flow pressure difference and no blanking capability.
Many researchers use additives such as MgO micro powder, coke powder and the like or deposit graphite carbon or Fe on the surface of the mineral powder 3 C, or temperature-changing, gas-changing component reduction, etc., have conducted intensive research on the reduction or prevention of cohesive defluidization, and although there is a certain effect, it is still unsatisfactory in terms of reliability and economy, and the mineral powder aggregates or original large-particle-size mineral powder generated by cohesion are liable to deposit on the conventional gas distribution plate, and the existing pneumatic discharge dipleg or overflow discharge process is difficult to discharge them all-round, aggravating the hazard of defluidization, thus hindering the development of iron ore fluidized bed reduction.
Disclosure of Invention
It is known to those who have studied thermal state tests of iron ore fluidized beds, for reducing atmosphere mainly containing CO, even if the iron ore fluidized bed is reduced to cause binding defluidization, and the sample is discharged after slow cooling, generally, the particle size of mineral powder agglomerates is more than 2-3 mm and less than 5mm, and the higher the temperature is, the higher the air velocity of the fluidized bed is, the larger the bound agglomerate size is, the more important phenomenon is that the mineral powder agglomerates are actually formed by mutually adhering a plurality of original mineral powder particles, the higher porosity exists inside, the mutual intersection of iron whiskers plays an important role, and the strength of the mineral powder agglomerates is very low, and the mineral powder agglomerates can be broken into small powder particles (mineral powder particles close to the particles before reduction) by light twisting with hands; for H 2 The main reducing atmosphere, even if the adhesive is lost, the sample discharged after cooling does not even have much adhesive mass, and most of the particles after reductionStill dispersed and is not much different from the original mineral powder particles; it can be concluded that the cohesive strength between the ore fines particles in the cohesive mass should not be too strong during the high-temperature reduction process, and the main reason for the loss of flow is that the drag force of the gas flow is weaker than the cohesive force between the ore fines cohesive mass or the ore fines particles, and the cohesive force between the ore fines and the wall, which provides a new solution.
In order to solve the technical problems, the invention provides a large-speed-difference stirring spouted fluidized bed for iron ore hydrogen-rich reduction, which utilizes a plurality of large-speed-difference stirring spouted fluidized beds connected in series (called large-speed-difference fluidized beds for short) to directly use oxygen-rich high-air temperature air or coal gas obtained after high-temperature reforming of a pure oxygen smelting reduction furnace or hydrogen-rich coal gas produced by other reduced coal gas preparation systems as reducing gas, wherein the hydrogen-rich refers to that coke oven gas, natural gas, biomass or organic garbage with a large proportion of added fuel and reducing agent used by the smelting reduction furnace, and volatile components in coal blocks and coal powder also enter the smelting reduction furnace, so that the hydrogen content of the produced coal gas is greatly improved compared with blast furnace gas, and the oxygen-rich high-air temperature air refers to that hot air used by the smelting reduction furnace has a temperature of about 1200 ℃ and an oxygen content of more than 30%; the reduced ore powder (sponge iron granules) is directly discharged into the smelting reduction furnace from the upper part or into a sponge iron sealed discharge system, so that the intermediate transportation process and the heat dissipation loss of preheating and reducing the ore powder by other smelting reduction processes are avoided, and the energy utilization rate is improved.
In order to realize the technical purpose, the invention adopts the following scheme: the large-speed-difference stirring spouted fluidized bed for iron ore hydrogen-rich reduction comprises a moving mechanism and a large-speed-difference fluidized bed which is connected in series at one level or more than two levels, the lower part of the moving mechanism arranged on the top of the furnace is connected with the large-speed-difference fluidized bed which is connected in series, the upper end of the large-speed-difference fluidized bed at the top is provided with a mineral powder feeding port and a tail gas discharging port, and the side wall of the large-speed-difference fluidized bed at the middle part and/or the lower part is connected with a heat supplementing gas pipe.
The motion mechanism comprises a lifting cylinder, a lifting frame, a driving mechanism, a transmission gear shaft, a driving gear, a driven gear, a bearing, a pipe shaft group and a seal box; the sealing box is fixed at the top of the furnace body, the lifting cylinder and the driving mechanism are installed outside the sealing box, the lifting frame, the transmission gear shaft, the driving gear, the driven gear and the bearing are installed in the sealing box, and the bearing suspends the tubular shaft group in the sealing box.
The lower part of the tubular shaft group penetrates into the serial large-speed-difference fluidized beds, and is respectively connected with the frame paddle, the scraper, the guide plate, the air inlet mechanism and the material discharging mechanism in each stage of large-speed-difference fluidized bed and drives the frame paddle, the scraper, the guide plate, the air inlet mechanism and the material discharging mechanism to move relatively.
Usually, more than two stages of large-speed-difference fluidized beds (generally, three to six stages, or more than six stages) are connected in series to achieve a better iron ore reduction process effect; other fluidized bed physicochemical treatment purposes for simple cohesive materials or materials with wide particle size distribution may even employ a one-stage large velocity difference fluidized bed. To facilitate the expression of the essential idea of the invention, it is only illustrated here in the context of a three-stage differential velocity fluidized bed cascade.
Compared with the prior art, the invention has the beneficial effects that: the device adopts a plurality of large-speed-difference stirring and spraying fluidized beds which are connected in series, more than one rotatable layer of frame paddles, scrapers and guide plates with different diameters are arranged in each large-speed-difference stirring and spraying fluidized bed, the air speed of the middle and lower parts of each large-speed-difference stirring and spraying fluidized bed is very high, the particle size of ore powder aggregates which are bonded downwards is gradually increased, the increased ore particles are allowed to be adapted to the further improvement of the air speed, the air flow drag force of the area is greatly increased, the mechanical stirring force and the cutting and rubbing crushing force of the rotary motion of various frame paddles, scrapers and guide plates are superposed, so that the ore powder aggregates or the ore powder particles are larger than the ore powder aggregates or the cohesive force between the ore powder and the wall, thereby ensuring the good fluidization state of the area, gradually enriching and depositing the large aggregates and large particles in a moving bed forced stirring and discharging area stored at the bottom of the furnace, discharging the large aggregates and the large particles into the next-stage fluidized bed with higher flow speed under the continuous stirring state according to a certain discharging speed, avoiding the flow loss problem of the fluidized bed, saving the consumption of reducing gas, and maintaining the size of the fluidized aggregates or the normal operation of the fluidized bed, and discharging the ore powder aggregates or the ore powder aggregates beyond the size of the discharging range; the device directly utilizes the high-temperature coal gas reformed by the smelting reduction furnace or hydrogen-rich coal gas produced by other reduced coal gas preparation systems as the reducing gas, thereby reducing the heat energy loss and improving the energy utilization rate; and the inside of the mineral powder aggregate also has a porous loose structure and has excellent reduction kinetic conditions, so that the device improves the effective volume utilization coefficient while improving the operation stability and reliability.
The preferred scheme of the invention is as follows:
the large-speed-difference fluidized bed comprises an upper cylindrical section, a middle conical section and a lower cylindrical section, and the air flow speed at the lower part of the large-speed-difference fluidized bed is 3-20 times of that at the upper part, so that the air flow drag force at the middle lower part of the fluidized bed is greatly enhanced; the tubular shaft group is divided into a lifting tubular shaft and a fixed-height tubular shaft, and more than one layer of frame paddles, scrapers and guide plates with different diameters are arranged in the large-speed-difference fluidized bed and are respectively connected with the corresponding fixed-height tubular shafts and rotate along with the fixed-height tubular shafts.
The large-speed-difference fluidized bed also comprises an air inlet mechanism and a material discharging mechanism, and each lifting pipe shaft is respectively connected with the air inlet mechanism and the material discharging mechanism of each stage of large-speed-difference fluidized bed and drives the same to move. The air inlet mechanism comprises an air inlet cylinder valve and an air inlet fixed conical section, the lower part of the large-speed-difference fluidized bed is connected with a furnace bottom hanging fixing frame, the furnace bottom hanging fixing frame is connected with the air inlet fixed conical section, the air inlet fixed conical section is located on the outer side of the air inlet cylinder valve to form an air inlet channel, and the air inlet cylinder valve is located on the outer side of the lower cylindrical section.
The discharge mechanism comprises a discharge barrel valve, a discharge barrel valve force transmission frame and a lifting plate, the discharge barrel valve is connected with the lifting pipe shaft through the discharge barrel valve force transmission frame, the discharge barrel valve is positioned outside the moving bed section furnace body, and the outer side wall of the discharge barrel valve is connected with the lifting plate.
The discharge mechanism also comprises a discharge groove bottom plate, a sealing disc and a discharge groove side wall, the discharge groove bottom plate is connected with the discharge groove side wall, the upper end of the discharge groove side wall is connected with the furnace bottom hanging fixing frame, and the upper edge of the discharge groove side wall is lower than the upper edge of the material lifting plate; the center of the bottom plate of the discharge tank is provided with a through hole, and the sealing disc is sleeved on the tubular shaft group and is blocked at the through hole of the bottom plate of the discharge tank.
The material discharging mechanism further comprises a moving bed section frame paddle, a material discharging inner scraper, an inner scraper force transmission frame and an inner scraper centering sleeve, the inner scraper centering sleeve is sleeved on the lifting pipe shaft, the material discharging inner scraper and the inner scraper force transmission frame are both fixed on the inner scraper centering sleeve, and the moving bed section frame paddle is fixed at the end part of the material discharging inner scraper and the inner scraper force transmission frame.
The inner scraper centering sleeve is provided with a downward notch and is inserted below the discharging cylinder valve force transmission frame at the position of the discharging cylinder valve force transmission frame corresponding to the inner scraper centering sleeve, and stirring and quantitative discharging rotary motion are realized under the stirring of the discharging cylinder valve force transmission frame; the force transmission frame of the discharging cylinder valve moves downwards along the opening and the lifting pipe shaft at the moment of blowing out, so that the closing of the discharging cylinder valve and the air inlet cylinder valve is realized, and a large amount of furnace burden is prevented from being sprayed outwards.
The large-speed-difference fluidized bed at the bottom extends downwards to form a straight-tube-shaped temperature-adjusting furnace body, and a rotatable temperature-adjusting side frame paddle is arranged in the temperature-adjusting furnace body. The lower end of the heat supplementing gas pipe is connected with a heat supplementing gas outlet pipe, the heat supplementing gas outlet pipe penetrates through the middle part of the furnace body of the temperature adjusting zone, and more than two layers of cold circulating gas distribution pipes are respectively arranged above and below the heat supplementing gas outlet pipe.
Further, the large-speed-difference fluidized bed is divided into a reduction fluidized bed and a cooling fluidized bed, and the reduction fluidized bed is connected above the cooling fluidized bed in series; the reduction fluidized bed is connected with a heat supplementing gas pipe, the gas inlet fixed conical section of the reduction fluidized bed positioned at the bottom extends upwards to the inner wall of the top of the cooling fluidized bed so as to form a heat reduction gas isolation area, the heat reduction gas isolation area is connected with a heat reduction gas supply pipe, and the heat supplementing gas pipe is arranged above the heat reduction gas supply pipe.
The side wall of the upper cylindrical section of the cooling fluidized bed is additionally prolonged, and the side wall of the upper cylindrical section after the extension is connected with a hot cooling coal gas discharge pipe, so that the purposes of sealing hot reduction coal gas and isolating hot cooling coal gas are achieved.
The lower end of the cooling fluidized bed is provided with a cold circulating coal gas distribution pipe, and the cold circulating coal gas is used as a cooling medium.
Further, the large-speed-difference fluidized bed is divided into an oxidizing roasting fluidized bed and a reducing fluidized bed, and the oxidizing roasting fluidized bed is connected above the reducing fluidized bed in series; the gas inlet fixing conical section of the oxidizing roasting fluidized bed extends obliquely upwards, the upper end of the extended gas inlet fixing conical section is connected with the outer wall of the oxidizing roasting fluidized bed in a sealing mode through a sealing plate, the extended gas inlet fixing conical section is connected with a burner, the burner is connected with a gas branch pipe valve and a combustion-supporting air branch pipe valve, and the end portion of the gas branch pipe is communicated with the upper portion of the reducing fluidized bed.
The side wall below the connecting position of the reduction fluidized bed and the gas branch pipe is connected with a furnace top gas discharge pipe so as to discharge the redundant furnace top gas out of the furnace.
The reduction fluidized bed is connected with a heat supplementing gas pipe, the lower end of the heat supplementing gas pipe is connected with a heat supplementing gas outlet pipe, the heat supplementing gas outlet pipe traverses the middle part of the furnace body of the temperature adjusting zone, and more than two layers of cold circulating gas distribution pipes are respectively arranged above and below the heat supplementing gas outlet pipe.
Drawings
FIG. 1 is a schematic cross-sectional view of a large-speed-difference stirring spouted fluidized bed for hydrogen-rich reduction of iron ore, which is provided by the embodiment of the invention;
FIG. 2 is a schematic cross-sectional structural view of a large velocity difference fluidized bed provided in an embodiment of the present invention;
FIG. 3 is a schematic diagram of the structure inside the seal box according to the embodiment of the present invention;
FIG. 4 is a partial cross-sectional view of a cone-ring baffle provided in accordance with an embodiment of the present invention;
FIG. 5 is a schematic connection diagram of a gas inlet mechanism and a material outlet mechanism in a large velocity difference fluidized bed according to an embodiment of the present invention;
FIG. 6 is a schematic cross-sectional view of a multi-stage reduction-cooling apparatus provided in accordance with an embodiment of the present invention;
FIG. 7 is a schematic cross-sectional view of a pre-oxidizing roasting-multi-stage reduction apparatus according to an embodiment of the present invention;
FIG. 8 is an enlarged view of the structure at I in FIG. 3;
FIG. 9 is an enlarged view of a portion of the structure of FIG. 5;
FIG. 10 is an enlarged view of a lower portion of the structure of FIG. 5;
labeled as: 1. lifting the cylinder; 2. a lifting frame; 3. sealing the box; 301. a furnace top cold cycle gas inlet valve; 4. a first drive mechanism; 401. a first drive gear shaft; 5. a second drive mechanism; 501. a second drive gear shaft; 6. a furnace body fixing bracket; 7. fixing a support frame; 701. a second bearing; 8. a family of pipe axes; 801. class A tubular shaft; 802. a class B tubular shaft; 803. lifting the tubular shaft; 804. a driven gear; 805. a first bearing; 806. a driving gear; 807. fixing a high pipe shaft; 808. a slider; 9. a furnace roof flange; 91. a furnace top expansion joint; 10. a large differential velocity fluidized bed; 101. an upper cylindrical section; 1011. the upper cylindrical section is provided with a frame paddle; 1012. a connecting frame; 102. a middle cone section; 1021. the upper frame paddle of the furnace body; 1022. a frame paddle in the middle of the furnace body; 1023. a lower frame paddle of the furnace body; 103. a conical ring-shaped guide plate; 1031. the guide plate section furnace body frame paddle; 1032. a discharge hole; 1033. a first vent hole; 1034. a second vent hole; 1035. reinforcing ribs; 104. a scraper; 1041. a scraper force transmission frame; 105. a lower cylindrical section; 1051. high-speed section frame paddles; 106. a mineral powder feeding port; 107. a tail gas discharge port; 11. an air inlet cylinder valve; 1101. a force transmission frame of the air inlet cylinder valve; 12. the air inlet is fixed with a conical section; 13. an air inlet scraper; 14. a fixed frame is hung at the bottom of the furnace; 15. a moving bed section furnace body; 16. moving bed section frame paddles; 17. a discharge cylinder valve; 18. a force transmission frame of the discharge cylinder valve; 19. a material raising plate; 20. a discharge chute base plate; 21. a side wall of the discharge groove; 22. sealing the disc; 23. an inner scraper centering sleeve; 24. an inner scraper force transmission frame; 25. discharging an inner scraper; 31. sealing the furnace wall; 32. a temperature-regulating zone furnace body; 33. a temperature-adjusting side frame paddle; 34. a heat supplementing gas pipe; 35. a heat supplementing gas valve; 36. a heat supplementing gas delivery pipe; 37. a cold cycle gas distribution pipe; 38. cooling the fluidized bed; 40. A hot reducing gas supply pipe; 42. A hot cooling gas discharge pipe; 43. a sponge iron sealed discharge system; 44. oxidizing and roasting the fluidized bed; 45. burning the nozzle; 46. a gas branch valve; 47. a combustion-supporting air branch pipe valve; 48. a furnace top gas discharge pipe; 49. and a smelting reduction furnace.
Detailed Description
The present invention will be described in detail with reference to the following embodiments in order to fully understand the objects, features and effects of the invention, but the present invention is not limited thereto. The high-temperature high-reduction potential coal gas which is enriched with hydrogen and even pure hydrogen and is directly used as a reducing agent in the oxygen-enriched high-air temperature air or pure oxygen melting reduction furnace; the produced high-temperature sponge iron particle groups are also directly discharged into a smelting reduction furnace or a sponge iron sealed discharge system below. Especially, the series connection of more than two stages of large speed difference fluidized beds (generally four to six stages) can achieve better process effect, and the physical and chemical treatment of other fluidized beds for simply binding materials or materials with wide particle size distribution can even adopt one stage of large speed difference fluidized bed. To facilitate the expression of the essential idea of the invention, it is only illustrated here in the context of a three-stage differential velocity fluidized bed cascade.
As shown in fig. 1, the large-speed-difference stirring and spouted fluidized bed for hydrogen-rich reduction of iron ore provided by the invention comprises a furnace body fixing support 6, a movement mechanism, a large-speed-difference fluidized bed 10 and a temperature-adjusting zone furnace body 32, wherein the large-speed-difference fluidized bed is connected in series with one or more stages; the motion mechanism comprises a lifting cylinder 1, a lifting frame 2, a driving mechanism, a transmission gear shaft, a driving gear 806, a driven gear 804, a bearing, a pipe shaft group 8 and a seal box 3; the furnace top sealing box 3 is fixed on the furnace body fixing support 6, the lifting cylinder 1 and the driving mechanism are installed on the top plate of the sealing box 3, the lifting frame 2, the transmission gear shaft, the driving gear 806, the driven gear 804 and the bearing are installed in the sealing box 3, the tubular shaft group 8 is hung in the sealing box 3 by the bearing, the lower part of the tubular shaft group 8 is connected with the serial large-speed-difference fluidized bed, and the lower end of the large-speed-difference fluidized bed at the bottom is connected with the temperature-adjusting belt furnace body 32.
As shown in fig. 2, 3 and 8, the motion mechanism comprises a pulling cylinder 1, a pulling frame 2, a driving mechanism, a transmission gear shaft, a driving gear 806, a driven gear 804, a bearing, a tube shaft group 8, a seal box 3 and the like, wherein the tube shaft group 8 is further divided into a pulling tube shaft 803 and a fixed-height tube shaft 807, and the fixed-height tube shaft 807 is connected with more than one layer of frame paddles, scrapers and guide plates with different diameters in the large-speed-difference fluidized bed and drives the frame paddles, the scrapers and the guide plates to rotate; the lifting pipe shaft 803 is connected with the gas inlet mechanism and the material discharge mechanism of each stage of large-speed-difference fluidized bed and drives the same to move; be fixed with furnace body fixed bolster 6 on the building basis, be fixed with seal box 3 on the furnace body fixed bolster 6, carry and draw jar 1 dress at the outer top center of seal box 3, carry the telescopic link of drawing jar 1 and pass the seal box 3 top surface and be connected with carrying the drawing frame 2, carry the central axis of drawing frame 2 and carry the telescopic link collineation of drawing jar 1.
The side wall of the sealing box 3 is connected with a gas pipeline, and a furnace top cold circulation gas inlet valve 301 is arranged on the gas pipeline. The number of the driving mechanisms is more than 2, the pipe shafts in the pipe shaft group 8 are classified according to the number of the driving mechanisms, and the number of the driving mechanisms is the same as that of the pipe shafts. The driving mechanism can be electric, hydraulic or pneumatic, in order to express the essential idea of the invention conveniently, the embodiment is only explained by two sets, the outer top of the sealing box 3 is also fixed with two sets of driving mechanisms, the output shaft of the driving mechanism penetrates through the sealing box and extends into the sealing box 3, and the two driving mechanisms are symmetrically arranged about the lifting cylinder 1 and are respectively a first driving mechanism 4 and a second driving mechanism 5. The first drive mechanism 4 has a first drive gear shaft 401 connected to an output shaft end thereof, and the second drive mechanism 5 has a second drive gear shaft 501 connected to an output shaft end thereof. The first transmission gear shaft 401 and the second transmission gear shaft 501 are respectively linked with a plurality of driving gears 806 through keys.
The tubular shaft group 8 is formed by sleeving a plurality of tubular shafts together, the tubular shafts in the tubular shaft group 8 are classified according to the number of sets of driving mechanisms, the number of the classes is the same as the number of the sets of the driving mechanisms, and two sets are taken as an example for explanation. The tube shafts in the tube shaft group 8 are divided into an A-type tube shaft 801 and a B-type tube shaft 802 from outside to inside, a driven gear 804 is fixedly sleeved at the top end of each of the A-type tube shaft 801 and the B-type tube shaft 802, the driven gear 804 of the A-type tube shaft 801 is meshed with a driving gear 806 on the first transmission gear shaft 401, and the driven gear 804 of the B-type tube shaft 802 is meshed with a driving gear 806 on the second transmission gear shaft 501. For better alignment of the driven gear 804, the height of the upper end of the spool (from outside to inside) is gradually increased. The first A-type tubular shaft 801 positioned at the lowest side is sleeved with a bearing, the lower end of the bearing is fixed on the bottom plate of the sealing box 3 on the furnace body fixing support 6 through a sizing block, and the first A-type tubular shaft 801 rotates through bearing support. A first class B tubular shaft 802 sleeved on the inner side of the first class A tubular shaft 801 is also sleeved with a bearing, the lower end face of the bearing is fixed on a driven gear 804 of the first class A tubular shaft 801 by a sizing block, and other tubular shafts are connected by adopting the structure; a slider 808 or other bearing is also provided in the lower portion of each spool, in the gap between adjacent spools, to control its oscillation and reduce friction.
The tube shaft group 8 is further divided into a fixed height tube shaft 807 and a lifting tube shaft 803, the upper end of the lifting tube shaft 803 is sleeved with a first bearing 805, and the lower end face of the first bearing 805 is fixedly connected with the lifting frame 2 through a sizing block; the upper end of the fixed height pipe shaft 807 is sleeved with a second bearing 701, the lower end face of the second bearing 701 is fixed on a driven gear 804 or a fixed support frame 7 of other fixed height pipe shafts by using a sizing block, the fixed support frame 7 is a rectangular frame fixed on the furnace body fixed support 6, a transverse support arm is fixed on the fixed support frame 7 and positioned above each lifting pipe shaft 803, and the lifting pipe shafts 803 are guaranteed to sink without affecting the rotation of the fixed height pipe shafts 807.
The tubular shaft group 8 penetrates through the bottom plate of the seal box 3 and the furnace body fixing support 6 and is connected with the top of the furnace body of the serial large-speed-difference stirring spout fluidized bed through a furnace top flange 9 and a furnace top expansion joint 91.
The number of the large differential fluidized beds 10 in series is determined according to the actual production situation, and 3 are taken as examples to be explained here: the main structures of the three large-speed difference fluidized beds are basically the same, and the detailed structure is described by taking the large-speed difference fluidized bed positioned at the top as an example.
As shown in fig. 2, the differential fluidized bed 10 includes a furnace body and a rotatable baffle plate with a blanking function and a gas distribution function. The upper end of the furnace body is provided with a mineral powder feeding port 106 and a tail gas discharging port 107, the furnace body is of an upper expanding structure, the air flow speed at the lower part of the fluidized bed is 7.5-12.9 times of that at the upper part, and a sub-fast fluidized state, a turbulent fluidized state and a bubbling fluidized state coexist. The upper expansion type furnace body comprises an upper cylindrical section 101, a middle cone section 102, a lower cylindrical section 105 and the like, the lower end of the upper cylindrical section 101 is fixedly connected with the upper end of the middle cone section 102, and the lower end of the middle cone section 102 is fixedly connected with the lower cylindrical section 105.
Go up and be provided with cylinder section frame oar 1011 in the cylinder section 101, go up cylinder section frame oar 1011 and comprise paddle, link 1012, and link 1012 connects on A class hollow shaft, rotates along with A class hollow shaft's rotation.
Middle part cone section 102 is for the cone structure more than 2 sections of gradual section undergauge, all be provided with the frame oar in every section cone, specifically be furnace body upper portion frame oar 1021 from top to bottom, water conservancy diversion board section furnace body frame oar 1031, furnace body middle part frame oar 1022, furnace body lower part frame oar 1023, wherein furnace body upper portion frame oar 1021 and last cylinder section frame oar 1011 are connected on same link 1012, it is located the link 1012 upside to go up cylinder section frame oar 1011, furnace body upper portion frame oar 1021 is located link 1012 downside. Also provided within the middle-cone section 102 is a rotatable multi-layer baffle, only two layers of which are illustrated herein. The shape of each layer of guide plate is provided with a scraper 104 matched with the upper surface of the guide plate, the shape of the scraper 104 is plow-shaped or single-knife-edge-shaped, the knife surface of the scraper and the tangent plane of each corresponding conical surface form an included angle of 8 to 90 degrees, and one or more than two scrapers 104 above each layer of guide plate can be arranged.
The blades 104 rotate in the opposite direction to the baffles, and thus the baffles are connected to different classes of a and B of pipe shafts with their upper and lower adjacent baffles or attachment brackets 1012. For example: the lower surface of the connecting frame 1012 is fixed with the scraper 104, the connecting frame 1012 is connected on a class A tubular shaft, the upper guide plate adjacent to the connecting frame 1012 is connected on a class B tubular shaft, when the connecting frame 1012 rotates forwards, the scraper 104 is driven to rotate forwards, the upper guide plate rotates backwards, and the two form relative motion.
The outer edge of the guide plate is provided with guide plate section furnace body frame paddles 1031, the lower side of the upper guide plate is provided with a scraper 104 of the next guide plate layer, and the outer edge of the scraper 104 is fixed with furnace body middle frame paddles 1022; the lower side of the guide plate at the lowest layer is not provided with a scraper and only connected with the edge frame paddle 1023 at the lower part of the furnace body.
As shown in fig. 4, the baffle may be any one of a conical ring-shaped baffle, a flat plate-shaped baffle, a conical baffle, and a curved baffle; the conical annular deflector 103 is taken as an example for introduction, the conical annular deflector 103 comprises a conical plate, an annular ridge and the like, a plurality of rings of annular ridges with gradually expanded diameters are sequentially arranged on the upper surface of the conical plate from inside to outside, a plurality of discharge holes 1032 are formed in the conical plate at the bottom of the annular ridge, and the aperture of each discharge hole 1032 is 2 to 4 times of the maximum particle size of a cohesive mass designed in a large-velocity-difference fluidized bed, so that furnace burden (including large-particle mineral powder and the cohesive mass) can fall below the conical annular deflector 103 through the discharge holes 1032 under the pushing of the scraper 104 or can be crushed on the conical annular deflector 103, and the secondary distribution of material flow is completed. The conical ring-shaped guide plate 103 is fixedly connected with the pipe shaft through a reinforcing rib 1035, and the scraper 104 is connected with the side wall of the pipe shaft through a scraper force transmission frame 1041.
The section of each annular ridge is of a triangular structure with an upward tip, a first vent 1033 with a smaller size is formed in the side wall of each annular ridge and a conical plate between adjacent annular ridges, the aperture of each first vent 1033 is 1.5-2.5 times of the maximum particle size of a furnace charge, the first vent is still larger than the pore size of a common distribution plate, and the first vent also has a smaller material passing capacity; the conical plate corresponding to the lower part of the annular ridge is also provided with a second vent 1034 with a larger size, and secondary distribution of the airflow (instead of uniform distribution on the section) is completed through the change of the opening size, the opening direction and the opening rate. The movement of the air flow and the material flow in each vent hole and each discharge hole 1032 is performed alternately along with the regular fluctuation of the bed pressure difference, and the secondary distribution effect of the material flow and the air flow is further improved along with the continuous rotation of the guide plates. The overall opening size and the opening rate of the conical ring-shaped guide plate 103 are far larger than those of a conventional gas distribution plate, the pressure difference is small, and the conical ring-shaped guide plate has the functions of blanking (including large-particle mineral powder and caking clusters) and preventing blockage.
Because the diameters of the upper furnace body and the lower furnace body of the conical annular guide plate 103 are different, the flow velocity in the air holes on the conical annular guide plate 103 is suddenly increased, so that an air flow redirection space exists below the conical annular guide plate 103, the quantity of materials which flow downwards through each layer of conical annular guide plate 103 is far larger than that of materials (entrainment) which flow upwards,
most materials are limited in the space between the two conical annular guide plates 103, the mixing of the upper and lower materials is reduced, the number of stages (sub-stages) of the fluidized bed is increased, the counter-flow heat transfer and reaction are closer to the reaction engineering, the conical annular guide plates 103 are provided with a plurality of layers, and only two or three layers are illustrated.
The bed layer between two adjacent layers of conical ring-shaped guide plates 103 belongs to the fluidization form of an upper expansion type large-speed-difference stirring spouted fluidized bed, each discharge hole 1032 and vent hole on each conical ring-shaped guide plate 103 are equivalent to the spout of the spouted bed, the jet flow of the spouts all moves along with the rotation of a tubular shaft, the dynamic jet flow action is stronger than the bubble action of a common fluidized bed, the coal gas replacement speed and the reduction speed in an emulsion phase are enhanced, the material dragging force of air flow is greatly enhanced, and the mechanical stirring force and the rubbing crushing force of the rotary motion of various frame paddles, scrapers and conical ring-shaped guide plates are superposed to ensure that the mechanical stirring force and the rubbing crushing force are greater than the viscous force among mineral powder aggregates and between the mineral powder aggregates and the wall of the spouted bed, so that the occurrence of fluid loss is prevented. Meanwhile, the bonding phenomenon in the mineral powder reduction process enables mineral powder aggregates to grow gradually, further improvement of the air velocity is allowed and adapted, and the interior of the mineral powder aggregates is still in a porous loose structure and has excellent reduction kinetic conditions, so that the device improves the operation stability and reliability and simultaneously improves the air velocity and the effective volume utilization coefficient by using the bonding effect.
The device and the structure enhance the airflow velocity and the airflow drag force of the middle lower part of the large-speed-difference fluidized bed 10, and the mechanical stirring force and the rubbing crushing force of the rotary motion of various frame paddles, scrapers and conical ring-shaped guide plates are superposed to ensure that the mechanical stirring force and the rubbing crushing force are greater than the cohesive force between mineral powder cohesive masses or mineral powder particles and between the mineral powder and the wall of the fluidized bed, so that the good fluidization state of the cohesive masses and large-particle mineral powder at the middle lower part of the large-speed-difference fluidized bed is ensured, and the cohesive defluidization is avoided, which is one of the core innovation points of the invention.
As shown in fig. 2, 5, 9 and 10, a high-speed rim paddle 1051 is provided in the lower cylindrical section 105, the high-speed rim paddle 1051 is connected to a pulling pipe shaft 803 via a connecting rod and an intake pipe valve transmission rack 1101, and an intake mechanism is further connected to the pulling pipe shaft 803 below the connecting rod. The air inlet mechanism comprises an air inlet cylinder valve 11, an air inlet cylinder valve transmission frame 1101, an air inlet fixing conical section 12 and the like, wherein the air inlet cylinder valve 11 is fixed on a lifting pipe shaft 803 through the air inlet cylinder valve transmission frame 1101, the air inlet cylinder valve 11 is of a cylindrical structure and is sleeved outside a lower port of the lower cylindrical section 105, so that the inner diameter of the air inlet cylinder valve 11 is slightly larger than the outer diameter (optimally 0 to 2mm) of the lower cylindrical section 105, and the outer diameter of the air inlet cylinder valve 11 is larger than the minimum inner diameter of the air inlet fixing conical section 12. An air inlet scraper 13 is fixed on the outer side wall of the air inlet cylinder valve 11, the air inlet scraper 13 is of an inverted right-angled triangle structure, and an included angle of 8-90 degrees is formed between the air inlet scraper 13 and the tangent plane of the inner wall of the air inlet fixing conical section 12.
A furnace bottom hanging fixing frame 14 is fixed outside the fluidized bed furnace body, the furnace bottom hanging fixing frame 14 is connected with an air inlet fixing conical section 12, and the air inlet fixing conical section 12 is positioned outside the air inlet cylinder valve 11. The air inlet fixing conical section 12 is of a conical structure with a wide upper part and a narrow lower part, an included angle between a bus of the air inlet fixing conical section 12 and a horizontal plane is 40-83 degrees, an included angle between a knife face of the air inlet scraper 13 and a tangent plane of the corresponding air inlet fixing conical section 12 is 8-90 degrees, and when the air inlet cylinder valve 11 sinks, the air inlet scraper 13 is tightly attached to the inner side wall of the air inlet fixing conical section 12.
The lower port of the air inlet fixed cone section 12 is connected with a moving bed section furnace body 15, and the moving bed section furnace body 15 is of a cylindrical barrel structure. The lower side of the moving bed section furnace body 15 is provided with a discharging mechanism.
As shown in fig. 5, the discharging mechanism includes a discharging cylinder valve 17, a discharging cylinder valve force transmission frame 18, a lifting blade 19, and the like, the discharging cylinder valve 17 is connected with the lifting pipe shaft 803 through the discharging cylinder valve force transmission frame 18, the discharging cylinder valve 17 is of a cylindrical structure and is located outside the moving bed section furnace body 15 (the optimal gap is 0 to 2mm), the lifting blade 19 is connected to the outer side wall of the discharging cylinder valve 17, and the lower end of the lifting blade 19 is connected with the discharging cylinder valve force transmission frame 18. The sealing disc 22 is sleeved on the lifting pipe shaft 803 below the discharging mechanism, and the discharging groove is arranged below the sealing disc 22.
The discharge groove comprises a discharge groove bottom plate 20 and a discharge groove side wall 21, the discharge groove bottom plate 20 is sleeved on the lifting pipe shaft 803, the upper end of the discharge groove side wall 21 is connected with the furnace bottom hanging and fixing frame 14, and the upper edge of the discharge groove side wall 21 is lower than the upper edge of the material lifting plate 19; the lower end of the side wall 21 of the discharge groove is fixedly connected with the outer edge of the bottom plate 20 of the discharge groove, a through hole is arranged at the center of the bottom plate 20 of the discharge groove, and the sealing disc 22 is blocked at the through hole of the bottom plate 20 of the discharge groove in a suspension way.
The discharging mechanism further comprises a moving bed section frame paddle 16, a discharging inner scraper 25, an inner scraper force transmission frame 24 and an inner scraper centering sleeve 23, the inner scraper centering sleeve 23 is sleeved on the lifting pipe shaft 803, the discharging inner scraper 25 and the inner scraper force transmission frame 24 are both fixed on the inner scraper centering sleeve 23, and the moving bed section frame paddle 16 is fixed at the end parts of the discharging inner scraper 25 and the inner scraper force transmission frame 24. The discharging inner scraper 25 and the moving bed section frame paddle 16 form an included angle of 8-90 degrees with the tangent plane of the corresponding cleaning surface.
At the position corresponding to the discharging cylinder valve force transmission frame 18, the inner scraper centering sleeve 23 is provided with a downward notch and is inserted below the discharging cylinder valve force transmission frame 18, and the rotary motion of continuous stirring and quantitative discharging is realized under the stirring of the discharging cylinder valve force transmission frame 18. The force transmission frame 18 of the discharging cylinder valve moves downwards along the opening and the lifting pipe shaft 803 at the moment of blowing-out, so that the closing of the discharging cylinder valve 17 and the air inlet cylinder valve 11 is realized, and a large amount of furnace burden is prevented from being sprayed outwards.
Under the conditions of the device and the structure, the large-particle mineral powder and the cohesive masses which are deposited and stored in the forced stirring discharge area of the moving bed at the bottom of the furnace are quantitatively discharged into the next stage of large-speed-difference fluidized bed with higher flow speed by the discharge mechanism in a continuously stirring state, keep good fluidization and reduction, and finally are discharged into the melting reduction furnace 49 or the sponge iron sealed discharge system 43.
The furnace bottom hanging fixed frame 14 and the top plate of the next stage of large speed differential fluidized bed are both connected at the lower part of the middle cone section 102, so as to realize the series connection process of the multistage fluidized bed.
The outer side wall of the tubular shaft group 8 between the furnace body fixing support 6 and the top of the fluidized bed furnace body is connected with a furnace top flange 9 and a furnace top expansion joint 91.
The multi-stage high speed difference fluidized bed has the lifting pipe shaft 803 and the fixed pipe shaft 807 connected in series below, and is arranged inside the lifting pipe shaft 803 and the fixed pipe shaft 807 of the high speed difference fluidized bed positioned at the top, all the lifting pipe shafts 803 and the fixed pipe shafts 807 are coaxially arranged, the rotating directions of the adjacent pipe shafts are opposite, in the gap between the adjacent pipe shafts, and the lower part of each pipe shaft is also provided with a slide block 808 or other bearings to control the swinging of the pipe shaft and reduce the friction. The connection and working principle of other parts of the multi-stage large-speed-difference fluidized bed connected in series below are the same as those of the large-speed-difference fluidized bed positioned at the top, and the small difference is that the inner diameter of the furnace body corresponding to each part of the furnace body is gradually reduced downwards so as to adapt to the rule that the diameter of the mineral powder granules gradually increases and the fluidization speed is suitable for gradually increasing.
The top of the top large-speed-difference fluidized bed is provided with a mineral powder feeding port 106 and a tail gas discharging port 107, the upper end of the middle large-speed-difference fluidized bed is fixed on the outer side wall below the middle cone section 102 of the top large-speed-difference fluidized bed, so that the upper cylindrical section 101 of the middle large-speed-difference fluidized bed is wrapped outside the air inlet mechanism and the material discharging mechanism of the top large-speed-difference fluidized bed, and the air inlet and material discharging structure and the furnace bottom hanging and fixing frame 14 of the top large-speed-difference fluidized bed 10 are sealed. Similarly, the upper end of the large-speed-difference fluidized bed 10 at the bottom is connected with the middle lower part of the middle large-speed-difference fluidized bed.
As shown in FIG. 1, a sealed furnace wall 31 is arranged outside the gas inlet mechanism and the material outlet mechanism at the lower part of the bottom differential fluidized bed 10, the sealed furnace wall 31 is connected to the outer side wall of the middle cone section 102 of the bottom differential fluidized bed 10, and the materials and the gas are ensured to flow in the furnace.
The sealed furnace wall 31 extends downwards to the bottom of the large-speed-difference fluidized bed to form a straight cylindrical temperature-regulating zone furnace body 32. A rotatable temperature-adjusting side frame paddle 33 is arranged in the temperature-adjusting furnace body 32.
Meanwhile, the side wall of the middle cone section 102 of the large-velocity-difference fluidized bed 10 positioned at the middle part and the bottom part is connected with more than one heat-supplementing gas pipe 34, at the upper part of the middle cone section 102 of the furnace body of each stage of large-velocity-difference fluidized bed 10, the heat-supplementing gas pipe 34 is provided with a heat-supplementing gas valve 35 for increasing the temperature of the fluidized gas so as to replace the combustion temperature increase of the Finex process, the lower end of the heat-supplementing gas pipe 34 is connected with a heat-supplementing gas outlet pipe 36, the heat-supplementing gas outlet pipe 36 penetrates through the middle part of the furnace body 32 in the temperature adjusting zone, and the upper part and the lower part of the heat-supplementing gas outlet pipe 36 are respectively provided with more than two layers of cold-cycle gas distribution pipes 37 (only two layers are explained herein).
The working principle or process is as follows:
during normal operation, the lifting cylinder 1 is in a contracted state, the driven gear 804 of the lifting pipe shaft 803 is meshed with the driving gear 806, the lifting pipe shaft 803 and the fixed pipe shaft 807 are rotated under the driving of the first driving mechanism 4 and the second driving mechanism 5, and the class a pipe shaft 801 and the class B pipe shaft 802 rotate in opposite directions to drive the components connected thereto to move relatively.
Mineral powder A (including lime, light burned dolomite and other fluxes) with the thickness of 0-8 mm enters the top large-speed-difference fluidized bed 10 from a mineral powder feeding port 106, and is called a first-stage large-speed-difference fluidized bed 10 according to the convention, and the specific steps are as follows: the mineral powder A is gradually reduced in the upper expanding furnace body, wherein the fine mineral powder with higher reduction degree is gradually bonded into a lump shape, and the ore powder lumps and the large-particle mineral powder fall on the conical annular deflector 103 together and then fall into the next sub-level fluidized bed with higher flow velocity through the discharge hole 1032 of the conical annular deflector 103 to be continuously reduced in a fluidized state; while the fine ore powder which is not bonded into lumps is difficult to pass through the discharge hole 1032 of the conical ring-shaped guide plate 103 (the gas velocity is higher than the terminal settling velocity of the fine ore powder), and most of the fine ore powder which is remained in the lower flow velocity area at the upper part of the furnace body is continuously reduced in a fluidized state. The multi-layer rotating conical ring-shaped guide plates 103 have the triple functions of a material flow distribution plate, a spouted bed air flow distribution plate and a stirring paddle; the inner surfaces of all the sections of the furnace body are correspondingly provided with frame paddles, the upper surfaces of all the layers of the conical annular guide plates 103 are also provided with scrapers 104, the frame paddles and the scrapers are driven by respective pipe shafts to continuously rotate to scrape and clean the walls of the corresponding furnace, and large-size bonding blocks are crushed, so that the agglomeration of the walls of the furnace and the blockage of each discharge hole 1032 and each first vent 1033 are avoided, and the pushing function is also realized on the blanking of common mineral powder bonding blocks. The airflow velocity of each sub-level up-expansion type stirring and spraying fluidized bed is gradually increased from top to bottom, so that the rule that fine mineral powder aggregates are gradually bonded and grow is adapted, fine mineral powder (above), mineral powder agglomerates and large mineral powder (below) can be continuously reduced under the condition of keeping a good fluidized state, the reduction degree of the mineral powder is improved by using a bonding effect, the mineral powder finally falls into a discharge tank, the mineral powder agglomerates and the large mineral powder are gradually pushed to the outer side of the discharge tank under the continuous rotating stirring of a discharge inner scraper 25 and a moving bed section frame paddle 16, the mineral powder in the discharge tank is circularly stirred by the rotation of a lifting blade 19, flows upwards through a side wall 21 of the discharge tank and enters a next-level large velocity difference fluidized bed 10 commonly called as a second-level.
The movement and mass and heat transfer reactions of the mineral powder in the second stage, the third stage and the ith stage (i is a positive integer more than or equal to 4) until the last stage of the fluidized bed with large speed difference 10 at the bottom are consistent with the movement and heat transfer reactions, only the air velocity of the corresponding part is gradually increased, and finally the sponge iron granules M are directly discharged into the melting reduction furnace 49 or the sponge iron sealed discharge system 43.
Hot coal gas H which is from oxygen-enriched high-air-temperature air (the temperature is about 1200 ℃, the oxygen content is about 30 percent) or a pure oxygen melting reduction furnace 49 or other hot reduction coal gas supply systems and is added with hydrogen-enriched even reformed high-temperature high reduction potential of pure hydrogen enters from a temperature adjusting zone furnace body 32 at the lowest part, part of cold circulation coal gas C is added through a cold circulation coal gas distribution pipe 37 at the lower part for primary temperature adjustment, part of hotter complementary coal gas B is led out through a complementary coal gas leading-out pipe 36, and then each stage of fluidized bed at the upper part is supplemented with heat through a complementary coal gas pipe 34 and a complementary coal gas valve 35 so as to maintain the proper working temperature of each stage of fluidized bed; then part of the cold circulating coal gas C is added through the cold circulating coal gas distribution pipe 37 at the upper part to carry out accurate temperature adjustment so as to ensure that the requirement of the lowest large-speed-difference fluidized bed 10 on the temperature of the reducing coal gas is met.
The reducing coal gas enters the lowest large-speed-difference fluidized bed 10 from a gas inlet mechanism at the lower part, and the method specifically comprises the following steps: the reducing coal gas flows upwards through a gap between the side wall 21 of the discharge groove and the sealed furnace wall 31, passes through the furnace bottom hanging fixing frame 14, passes through a gap between the air inlet fixing conical section 12 and the air inlet cylinder valve 11, then passes through the air inlet cylinder valve force transmission frame 1101, flows into the furnace body of the lower cylindrical section 105 of the large-speed-difference fluidized bed 10, passes through the discharge hole 1032, the second vent hole 1034 and the first vent hole 1033 of each layer of conical ring-shaped guide plate 103, rises all the way, is used as a spouted fluidized medium, keeps good spouted fluidized state of each part, particularly a high flow velocity area at the lower part, and prevents the loss flow of larger mineral powder particles or mineral powder caking groups; during the ascending process, the reducing coal gas and the mineral powder have mass transfer and heat transfer and reduction reactions, the reacted coal gas is added with part of hotter supplementing coal gas B through the supplementing heat coal gas pipe 34 and the supplementing heat coal gas valve 35, and then enters the upper stage large velocity difference fluidized bed 10 according to the same path until the tail gas G is discharged out of the furnace from the tail gas outlet 107 of the top large velocity difference fluidized bed 10 and enters the furnace top coal gas treatment system. Therefore, the air velocity and the air flow drag force on the materials at the middle lower part of the large-velocity-difference fluidized bed 10 are greatly improved, and the mechanical stirring force and the scraping and crushing force of the rotary motion of various frame paddles, scrapers and conical ring-shaped guide plates are superposed to be larger than the viscous force among mineral powder aggregates and between the mineral powder aggregates and the wall of the fluidized bed, so that the occurrence of fluid loss is prevented.
When the furnace is shut down in plan or sudden accident, the telescopic cylinder of the lifting cylinder 1 extends out, the lifting frame 2 is driven to sink, the lifting pipe shaft 803 of each stage of large-speed-difference fluidized bed 10 moves downwards, the parts (the air inlet cylinder valve 11, the discharge cylinder valve 17 and the like) fixedly connected to the lifting pipe shaft 803 move downwards along with the lifting pipe shaft 803, the lower edge of the air inlet cylinder valve 11 is tightly attached to the air inlet fixing conical section 12, the upper edge of the air inlet cylinder valve 11 is attached to the outer wall of the lower edge of the lower cylindrical section 105, and the phenomenon that materials in the large-speed-difference fluidized bed are instantly sprayed out to cause the furnace to be cold is avoided; at the same time, the discharge cylinder valve 17 is also closed together in the same way; thus, the fluidized materials in each stage of the large-speed-difference fluidized bed 10 are kept in the respective furnace bodies, and after the furnace is stopped, all the tube shafts 803 and the fixed-height tube shafts are lifted and rotated at a slow speed to prevent the mineral powder bonded lumps from excessively growing and hardening, so that good conditions are created for the next operation.
At the top of the furnace, the cold circulating gas C is filled into the seal box 3 through a furnace top cold circulating gas inlet valve 301 to play a role in cooling and pressure maintaining, and meanwhile, the cold circulating gas C passes through gaps of sizing blocks below the bottoms of the bearings, then descends along gaps among the tubular shafts of the tubular shaft group 8 and enters material layers of the large-speed-difference fluidized beds 10, so that the tubular shafts are cooled, and friction and abrasion caused by the fact that materials flow backwards into the gaps among the tubular shafts are prevented.
Another embodiment
As shown in fig. 6, the main structure is the same as that of the large velocity difference stirring spouted fluidized bed for hydrogen-rich reduction of iron ore of the above embodiment, except that: the embodiment is a device used in the iron ore fluidized bed direct reduction process, the large speed difference fluidized bed is divided into a reduction large speed difference fluidized bed 10 and a cooling fluidized bed 38, the reduction fluidized bed is connected in series above the cooling fluidized bed, that is, the number of the large speed difference fluidized bed in series is still 3 (or more n), the large speed difference fluidized beds positioned at the top and the middle part are the reduction large speed difference fluidized bed 10, the reduction fluidized bed contains (2 + 1) × 2 sub-stages, and all the multi-stage reduction large speed difference fluidized beds 10 have the same structure, working principle and process as those of the first embodiment, and are not described repeatedly; the large-speed-difference fluidized bed at the bottom is a cooling fluidized bed 38, three layers (or m layers) of conical annular guide plates 103 are arranged in the cooling fluidized bed 38, and the number of scrapers and frame paddles is correspondingly increased to increase one (or m + 1) sub-level to reach (3 + 1) } 1 sub-level. The upper cylindrical section of the cooling fluidized bed 38 is additionally extended compared with the upper cylindrical section of the reduction fluidized bed, so that the side wall of the extended upper cylindrical section of the closed thermal reduction coal gas D (the temperature is about 700-850 ℃) and the isolation thermal cooling coal gas E (the temperature is about 550-700 ℃) is connected with a thermal cooling coal gas discharge pipe 42, and the thermal cooling coal gas E is led out of the furnace.
The side wall of the middle part of the reduction fluidized bed at the middle position is connected with an auxiliary heating gas pipe 34, the air inlet fixing conical section 12 of the reduction fluidized bed extends upwards to the inner wall of the top of the cooling fluidized bed 38 so as to form a thermal reduction gas D isolation area, the thermal reduction gas isolation area is connected with a thermal reduction gas supply pipe 40, and the thermal reduction gas supply pipe 40 is positioned below the auxiliary heating gas pipe 34. The hot reducing gas D with high reducing potential and proper temperature from the outside is fed into the device through a hot reducing gas supply pipe 40; the make-up gas B with slightly higher temperature from the outside is fed into the device through the make-up gas pipe 34 and the make-up gas valve 35.
Similarly, the furnace walls 31 are provided outside the gas inlet means and the gas outlet means connected to the lower part of the cooled fluidized bed 38, and are connected to the outer side walls of the middle cone section 102 of the cooled fluidized bed 38, ensuring the flow of the material and gas inside the furnace. The sealed furnace wall 31 extends downward below the cooling fluidized bed 38 to form a straight cylindrical temperature-adjusting zone furnace body 32. More than two layers of cold circulating gas distribution pipes 37 penetrate through the furnace body 32 of the temperature adjusting zone, cold circulating gas C is injected to serve as a cooling medium, a sponge iron sealing discharge system 43 is arranged below the cold circulating gas distribution pipes 37, and sponge iron granules M discharged out of the furnace are distributed to a subsequent process according to use requirements.
Another embodiment
As shown in fig. 7, the main structure is the same as that of the large-speed-difference stirring spout-fluidized bed for hydrogen-rich reduction of iron ore of the first example, except that: the embodiment is a device suitable for a fluidized bed pre-oxidation roasting-multistage reduction process of iron ore (for treating materials with larger endothermic reaction in a medium-low temperature region or excessively compact internal structure of ore particles and excessively low reduction speed, such as laterite-nickel ore, limonite, goethite, siderite, red mud, magnetite and the like with excessively low reduction speed, or materials containing more physical water, crystal water, hydroxide, carbonate and the like). The specific differences are as follows:
the large speed difference fluidized bed is divided into an oxidizing roasting fluidized bed 44 and a reducing large speed difference fluidized bed 10, the oxidizing roasting fluidized bed 44 is connected above the reducing fluidized bed in series, namely the number of the large speed difference fluidized beds in series is three (or n), the large speed difference fluidized bed positioned at the top is the oxidizing roasting fluidized bed 44, and the partially reduced coal gas is directly and completely combusted so as to increase the physical heat supply; three layers of conical ring-shaped guide plates 103 (or more layers) are arranged in the pre-oxidation roasting fluidized bed 44, four sub-stages are connected in series, and the number of corresponding scrapers and frame paddles is increased; the differential fluidized beds located at the middle and bottom are reducing fluidized beds, and have the same structure as the differential fluidized bed described in the first embodiment, and comprise six sub-stages (or more) connected in series. The air inlet fixing conical section 12 of the oxidizing and roasting fluidized bed 44 extends obliquely upwards, and the upper end of the extended air inlet fixing conical section 12 is hermetically connected with the outer wall of the oxidizing and roasting fluidized bed 44 through a sealing plate so as to seal combustion waste gas at the temperature of about 850-950 ℃ and isolate and reduce furnace top gas G at the temperature of 600-700 ℃. The extended air inlet fixed conical section 12 is connected with a burner 45, the burner 45 is connected with a coal gas branch pipe valve 46 and a combustion-supporting air branch pipe valve 47, and one end of the coal gas branch pipe valve 46 is communicated with the upper part of the reduction fluidized bed positioned in the middle. The sidewall of the reducing large velocity difference fluidized bed 10 below the connection position of the gas branch pipe valve 46 is connected with a top gas discharge pipe 48 so as to discharge the excess top gas G out of the furnace. The combustion-supporting air F with the air excess coefficient larger than 1 enters the burner 45 through the combustion-supporting air branch pipe valve 47 and is completely combusted with part of the top gas introduced by the gas branch pipe valve 46, and the top gas is completely combusted in the burnerHigh heat supply capacity and simultaneously, the iron oxide is completely converted into the Fe easy to reduce 2 O 3 And directly discharged into the reduction large-speed-difference fluidized bed 10 connected therebelow, including other multi-stage reduction large-speed-difference fluidized beds 10, until the sponge iron granules M are finally discharged into the smelting reduction furnace 49, which is the same as the structure, working principle and process of the first embodiment and is not described repeatedly; the exhaust gas L from the oxidizing/calcining fluidized bed 44 is discharged to the outside of the furnace through the exhaust gas outlet 107.
Finally, it is noted that: the above lists only illustrate preferred embodiments of the invention, and it is of course possible for those skilled in the art to make changes and modifications to the invention, and such changes and modifications are considered to be within the scope of the invention as defined by the claims and their equivalents.

Claims (11)

1. A large-speed-difference stirring spouted fluidized bed for iron ore hydrogen-rich reduction is characterized by comprising a motion mechanism and a large-speed-difference fluidized bed which is connected in series at one stage or more than two stages, wherein the lower part of the motion mechanism arranged at the top of a furnace is connected with the large-speed-difference fluidized bed which is connected in series;
the upper end of the top large-speed-difference fluidized bed is provided with a mineral powder feeding port and a tail gas discharging port, and the side wall of the middle and/or lower large-speed-difference fluidized bed is connected with a heat supplementing gas pipe;
the moving mechanism comprises a pipe shaft group, the pipe shaft group is divided into a lifting pipe shaft and a fixed-height pipe shaft, each stage of large-speed-difference fluidized bed comprises an upper cylindrical section, a middle conical section and a lower cylindrical section, frame paddles, scrapers and guide plates with different diameters are arranged in the large-speed-difference fluidized bed, the frame paddles, the scrapers and the guide plates are respectively connected with the fixed-height pipe shafts at corresponding positions and rotate along with the fixed-height pipe shafts, and the rotating directions of the scrapers and the guide plates are opposite;
the guide plate has the blanking function and the gas distribution function, and is any one of a conical ring-shaped guide plate, a flat plate-shaped guide plate, a conical guide plate and a curved guide plate;
the conical annular guide plate comprises a conical plate and an annular ridge, the annular ridge with the diameter gradually expanded is sequentially arranged on the upper surface of the conical plate from inside to outside, a discharge hole is formed in the conical plate at the bottom of the annular ridge, and the aperture of the discharge hole is 2-4 times of the maximum aperture of a large-speed-difference fluidized bed designed adhesive mass; the section of each annular ridge is of a triangular structure with the tip portion upward, a first vent hole is formed in the side wall of each annular ridge and a conical plate between every two adjacent annular ridges, the aperture of each first vent hole is 1.5 to 2.5 times of the maximum aperture of furnace charge, and a second vent hole is formed in the corresponding conical plate below each annular ridge.
2. The iron ore hydrogen-rich reduction large-speed-difference stirring spouted fluidized bed according to claim 1, wherein the moving mechanism further comprises a pulling cylinder, a pulling frame, a driving mechanism, a transmission gear shaft, a driving gear, a driven gear, a bearing and a seal box; the sealing box is fixed at the top of the furnace body, the lifting cylinder and the driving mechanism are installed outside the sealing box, the lifting frame, the transmission gear shaft, the driving gear, the driven gear and the bearing are installed in the sealing box, and the bearing suspends the tubular shaft group in the sealing box.
3. The iron ore hydrogen-rich reduction large-speed-difference stirring spouted fluidized bed according to claim 2, wherein the large-speed-difference fluidized bed further comprises an air inlet mechanism and a material discharge mechanism, and each lifting pipe shaft is respectively connected with the air inlet mechanism and the material discharge mechanism of each stage of large-speed-difference fluidized bed and drives the air inlet mechanism and the material discharge mechanism to move;
the discharging mechanism comprises a discharging cylinder valve, a discharging cylinder valve force transmission frame and a lifting plate, the discharging cylinder valve is connected with the lifting pipe shaft through the discharging cylinder valve force transmission frame, the discharging cylinder valve is positioned on the outer side of the moving bed section furnace body, and the outer side wall of the discharging cylinder valve is connected with the lifting plate;
the discharge mechanism also comprises a discharge groove bottom plate, a sealing disc and a discharge groove side wall, the discharge groove bottom plate is connected with the discharge groove side wall, the upper end of the discharge groove side wall is connected with the furnace bottom hanging fixing frame, and the upper edge of the discharge groove side wall is lower than the upper edge of the material lifting plate;
the discharging mechanism also comprises a moving bed section frame paddle, a discharging inner scraper, an inner scraper force transmission frame and an inner scraper centering sleeve, the inner scraper centering sleeve is sleeved on the lifting pipe shaft, the discharging inner scraper and the inner scraper force transmission frame are both fixed on the inner scraper centering sleeve, and the moving bed section frame paddle is fixed at the end parts of the discharging inner scraper and the inner scraper force transmission frame;
at the position of the discharging cylinder valve force transmission frame corresponding to the inner scraper centering sleeve, the inner scraper centering sleeve is provided with a downward notch and is inserted below the discharging cylinder valve force transmission frame, and the rotary motion of continuous forced stirring and quantitative discharging of moving bed materials is realized under the stirring of the discharging cylinder valve force transmission frame.
4. The iron ore hydrogen-rich reduction large-speed-difference stirring spouted fluidized bed according to claim 3, wherein the air inlet mechanism comprises an air inlet cylinder valve and an air inlet fixing conical section, the lower part of the large-speed-difference fluidized bed is connected with a furnace bottom hanging and fixing frame, the furnace bottom hanging and fixing frame is connected with the air inlet fixing conical section, the air inlet fixing conical section is positioned on the outer side of the air inlet cylinder valve to form an air inlet channel, and the air inlet cylinder valve is positioned on the outer side of the lower cylindrical section; the air inlet cylinder valve is connected with the lifting pipe shaft;
the air flow velocity at the lower part of each stage of the large-velocity-difference fluidized bed is 3-20 times of that at the upper part, the air flow drag force at the middle and lower parts of the fluidized bed is greatly enhanced, and the mechanical stirring force and the rubbing crushing force of the rotary motion of various frame paddles, scrapers and guide plates are superposed to ensure that the air flow drag force is greater than the cohesive force of mineral powder cohesive masses or mineral powder particles and the cohesive force between the mineral powder and the wall of the fluidized bed, so that the good fluidization state of the cohesive masses and large-particle mineral powder at the middle and lower parts of the large-velocity-difference fluidized bed is ensured, and the fluid loss is avoided.
5. The iron ore hydrogen-rich reduction large-speed-difference stirring spouted fluidized bed according to claim 1, wherein the bottom large-speed-difference fluidized bed extends downwards to form a straight-tube-shaped temperature-adjusting zone furnace body, and a rotatable temperature-adjusting zone frame paddle is arranged in the temperature-adjusting zone furnace body;
the lower end of the heat supplementing gas pipe is connected with a heat supplementing gas outlet pipe, the heat supplementing gas outlet pipe penetrates through the middle part of the temperature adjusting zone furnace body, and more than two layers of cold circulating gas distribution pipes are respectively arranged above and below the heat supplementing gas outlet pipe; the high-temperature high-reduction potential coal gas which is rich in hydrogen and is added in the oxygen-enriched high-air temperature air or pure oxygen melting reduction furnace is directly used as a reducing agent; the produced high-temperature sponge iron particle clusters are also directly discharged into a lower smelting reduction furnace or a sponge iron sealing discharge system.
6. The iron ore hydrogen-rich reduction spout-fluidized bed for large-speed-difference agitation according to any one of claims 1 to 4, wherein the large-speed-difference fluidized bed is divided into a reducing fluidized bed and a cooling fluidized bed, and the reducing fluidized bed is connected in series above the cooling fluidized bed;
the reduction fluidized bed is connected with a concurrent heating gas pipe, the gas inlet fixing cone section of the reduction fluidized bed positioned at the bottom extends upwards to the inner wall of the top of the cooling fluidized bed so as to form a thermal reduction gas isolation zone, the thermal reduction gas isolation zone is connected with a thermal reduction gas supply pipe, and the concurrent heating gas pipe is arranged above the thermal reduction gas supply pipe.
7. The large velocity differential stirred spouted fluidized bed for hydrogen-rich reduction of iron ore of claim 6, wherein the upper side wall of the cooling fluidized bed is additionally extended, and a hot cooling gas discharge pipe is connected to the extended upper side wall.
8. The large velocity differential agitated spouted fluidized bed for hydrogen-rich reduction of iron ore according to claim 6, wherein a cold circulating gas distribution pipe is provided at a lower end of the cooling fluidized bed.
9. The iron ore hydrogen-rich reduction spout-fluidized bed for stirring with large speed difference according to any one of claims 1 to 5, wherein the large speed difference fluidized bed is divided into an oxidizing roasting fluidized bed and a reducing fluidized bed, and the oxidizing roasting fluidized bed is connected in series above the reducing fluidized bed; the gas inlet fixing conical section of the oxidizing roasting fluidized bed extends obliquely upwards, the upper end of the extended gas inlet fixing conical section is connected with the outer wall of the oxidizing roasting fluidized bed in a sealing mode through a sealing plate, the extended gas inlet fixing conical section is connected with a burner, the burner is connected with a gas branch pipe valve and a combustion-supporting air branch pipe valve, and the end portion of the gas branch pipe is communicated with the upper portion of the reducing fluidized bed.
10. The iron ore hydrogen-rich reduction large-speed-difference stirring spouted fluidized bed according to claim 9, wherein a top gas discharge pipe is connected to a side wall below a connection position of the reduction fluidized bed and the gas branch pipe.
11. The large velocity difference stirring spouted fluidized bed for hydrogen-rich reduction of iron ore of claim 9, wherein an additional heating gas pipe is connected to the reduction fluidized bed, an additional heating gas outlet pipe is connected to the lower end of the additional heating gas pipe, and more than two layers of cold circulation gas distribution pipes are respectively arranged above and below the additional heating gas outlet pipe.
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