CN115261542A - Circulating fluidized bed direct reduction method and process for short-process smelting of coal powder and mineral powder - Google Patents
Circulating fluidized bed direct reduction method and process for short-process smelting of coal powder and mineral powder Download PDFInfo
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- 239000000843 powder Substances 0.000 title claims abstract description 62
- 230000009467 reduction Effects 0.000 title claims abstract description 39
- 239000003245 coal Substances 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000003723 Smelting Methods 0.000 title claims abstract description 18
- 229910052500 inorganic mineral Inorganic materials 0.000 title claims abstract description 17
- 239000011707 mineral Substances 0.000 title claims abstract description 17
- 230000008569 process Effects 0.000 title description 5
- 238000002309 gasification Methods 0.000 claims abstract description 58
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 55
- 238000006722 reduction reaction Methods 0.000 claims abstract description 48
- 238000000197 pyrolysis Methods 0.000 claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 24
- 229910052742 iron Inorganic materials 0.000 claims abstract description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000011946 reduction process Methods 0.000 claims abstract description 13
- 239000007790 solid phase Substances 0.000 claims abstract description 13
- 239000012071 phase Substances 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 85
- 238000002407 reforming Methods 0.000 claims description 41
- 239000000428 dust Substances 0.000 claims description 27
- 238000007885 magnetic separation Methods 0.000 claims description 18
- 230000001172 regenerating effect Effects 0.000 claims description 17
- 239000003034 coal gas Substances 0.000 claims description 12
- 239000002817 coal dust Substances 0.000 claims description 11
- 239000002912 waste gas Substances 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 7
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 5
- 238000006057 reforming reaction Methods 0.000 claims description 5
- 239000006148 magnetic separator Substances 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000002485 combustion reaction Methods 0.000 claims description 3
- 230000001276 controlling effect Effects 0.000 claims description 3
- 239000002994 raw material Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 239000008247 solid mixture Substances 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 239000000956 alloy Substances 0.000 description 2
- 229910045601 alloy Inorganic materials 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000002699 waste material Chemical group 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0066—Preliminary conditioning of the solid carbonaceous reductant
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0073—Selection or treatment of the reducing gases
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/22—Increasing the gas reduction potential of recycled exhaust gases by reforming
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
- C21B2100/66—Heat exchange
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
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- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Manufacture Of Iron (AREA)
Abstract
The invention relates to a circulating fluidized bed direct reduction method and a circulating fluidized bed direct reduction process for short-process smelting of coal powder and mineral powder. All equipment is effectively and reasonably arranged, a direct reduction system based on a circulating fluidized bed is formed, the technology for preparing the reducing gas by coal gasification and the gas-based direct reduction technology are effectively combined, and the problem of the reducing gas which is required by the gas-based direct reduction and is economical and high in quality is solved. Meanwhile, the coal powder pyrolysis and the iron ore powder reduction are performed in a circulating fluidized bed reaction tower in a coordinated manner, the coal powder pyrolysis gas-phase product can effectively increase the reduction potential of the reduction gas, and the pyrolysis solid-phase product (coke powder) can effectively prevent adhesion in the iron ore powder reduction reaction. In addition, the system flow constructed by the invention basically realizes closed circulation, and the energy consumption is obviously reduced.
Description
Technical Field
The invention belongs to the field of direct reduction, and particularly relates to a circulating fluidized bed direct reduction method and process for short-process smelting of coal powder and mineral powder.
Background
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
By means of H2Or is rich in H2Compared with the traditional long-flow ironmaking process, the gas-based direct reduction process using gas as a reducing agent can reduce the emission of carbon dioxide by 40-65% and reduce SO2About 30 percent of emission is the preferable scheme for realizing 'carbon peak reaching and carbon neutralization' in the current metallurgical industry. The short-term gas-based direct reduction process is a mainstream metallurgical technical means in China, and the quality and the economy of the reducing gas for direct reduction are one of the keys of popularization and application of the gas-based direct reduction technology. In the prior artThe tube is a gas-based shaft furnace method or a gas-based fluidized bed method, and natural gas is not required to be used as energy. However, the application and popularization of the direct iron-making technology taking natural gas as energy are strongly restricted by natural resources in China due to shortage of natural gas resources in China.
Disclosure of Invention
The invention provides a circulating fluidized bed direct reduction method and a circulating fluidized bed direct reduction process for short-process smelting of coal powder and mineral powder, which aims to solve the problem of source of reducing gas required by gas-based direct reduction and effectively combine a coal gasification technology for preparing the reducing gas and a gas-based direct reduction technology.
In order to achieve the purpose, the invention is realized by the following technical scheme:
the invention provides a circulating fluidized bed direct reduction system for short-process smelting of coal powder and mineral powder, which mainly comprises a coal powder bin, an iron ore powder bin, a circulating fluidized bed reaction tower, a high-temperature cyclone separator, a feed back pipe, a discharge pipe, a magnetic separation device, a gasification reforming furnace, an exhaust gas regenerative heat exchanger, a bag-type dust remover and a hot blast stove; wherein, the coal dust bin and the iron ore dust bin are respectively connected with the circulating fluidized bed reaction tower; the outlet of the circulating fluidized bed reaction tower is connected with a high-temperature cyclone separator, the solid phase outlet end of the high-temperature cyclone separator is divided into two paths, and one path returns to the bottom of the fluidized bed reaction tower through a material return pipe to continue reduction reaction; one path enters a magnetic separation device through a discharge pipe; the gas-phase outlet end of the high-temperature cyclone separator is connected with a waste gas backheating heat exchanger; the magnetic separation device is connected with the gasification reforming furnace; the outlet of the exhaust gas backheating heat exchanger is divided into two paths, one path is connected with the gasification reforming furnace, and the other path is connected with the hot blast stove; the hot end outlet of the exhaust gas heat regenerative heat exchanger is connected with the hot end inlet of the water-cooling heat exchanger; the hot end outlet of the water-cooling heat exchanger is connected with a bag-type dust collector.
Each device effectively builds a system, realizes the basic closed circulation of the material and the energy of the system, and greatly reduces the energy consumption of the system.
Furthermore, the exhaust gas heat recovery heat exchanger is a gas-gas heat exchanger, and circulating coal gas is heated, so that the temperature after pyrolysis and reduction reaction is reduced, and the sensible heat of the coal gas is fully utilized; and secondly, the circulating coal gas is heated, the temperature of the circulating coal gas is increased, the energy consumption of the gasification reforming furnace is reduced, and the efficiency of the hot blast stove is improved.
Furthermore, the system also comprises a water-cooling heat exchanger which is arranged between the exhaust gas heat regenerative heat exchanger and the bag-type dust remover and has the function of regulating and controlling the air temperature to meet the requirement that the outlet temperature (namely the inlet temperature of the bag-type dust remover) is in the range of 150-200 ℃ so as to ensure the normal operation of the bag-type dust remover.
In a second aspect, the invention provides a circulating fluidized bed direct reduction process of pulverized coal and iron ore powder, comprising the following steps:
respectively feeding coal powder and iron ore powder at the bottom of the circulating fluidized bed, and finishing the quick pyrolysis of the coal powder and the direct reduction of the iron ore powder in the circulating fluidized bed along with the high-temperature reducing gas for 3-10 s; after reaction, the gas-solid mixture enters a high-temperature cyclone separator for separation, part of the separated solid phase product is circularly returned to the bottom of the fluidized bed for repeated reduction, and the other part of the solid phase product enters a magnetic separator; the separated gas phase enters a waste gas regenerative heat exchanger for heat exchange to heat the circulating cold gas; one part of the heated circulating cold coal gas is sent to a gasification reforming furnace, and the sensible heat of the high-temperature gasification gas is utilized to carry out reforming reaction with excessive carbon, so that CO in the circulating coal gas is converted into CO2And H2Reforming of O to CO and H2(ii) a One strand is sent to hot air for combustion, and the air is heated to provide high-temperature air for the gasification reforming furnace; the reducing gas generated by the gasification reforming furnace enters a circulating fluidized bed after the temperature of the circulating cold gas is adjusted, and a heat source and a medium (simultaneously serving as a fluidizing medium and a reducing medium) are provided for coal dust pyrolysis and iron ore powder reduction; and the main gas after pyrolysis and reduction flows through the exhaust gas backheating heat exchanger and then enters the water-cooled heat exchanger, and the main gas after temperature adjustment enters the bag-type dust remover.
In the circulating fluidized bed, the coal powder pyrolysis gas-phase product is mainly cracked into H2And CO, increasing the reduction potential of the reducing gas; the pulverized coal pyrolysis solid-phase product coke powder plays a role in preventing reduced iron from being adhered.
Furthermore, in the magnetic separator, the magnetically separated part is directly reduced iron, and the coke powder which is not magnetically separated is directly sent to a gasification reforming furnace to be gasified to prepare reducing gas.
Furthermore, coal powder pyrolysis and iron ore powder reduction are cooperatively generated in the circulating fluidized bed reaction tower, the reaction atmosphere is obtained by adjusting the temperature of the reducing gas generated by the gasification reforming furnace through circulating cold gas, the temperature range after temperature adjustment is 1000-1200 ℃, and the temperature range after pyrolysis and reduction reaction is 800-1000 ℃.
As a further implementation mode, the gasification raw material of the gasification reforming furnace is high-temperature coke powder separated by a magnetic separation device, the gasification agent is hot air from a hot blast stove, and the temperature range of the hot air is 600-1000 ℃. The reforming reaction is to return exhaust gas for the circulation heated by the regenerative heat exchanger, and use the high temperature of coke powder gasification to convert CO in the exhaust gas into CO under the premise of excessive carbon2、H2Reforming of O to CO and H2So that the alloy has reducibility again.
As a further implementation mode, the bag dust collected by the bag-type dust remover is pneumatically conveyed to the gasification reforming furnace to participate in gasification, exhaust gas at the outlet of the bag-type dust remover is divided into three paths, one path of exhaust gas is circulated to the exhaust gas regenerative heat exchanger, the other path of exhaust gas is circulated to the outlet of the gasification reforming furnace, and the other path of exhaust gas is externally supplied.
The invention has the following beneficial effects:
(1) According to the invention, coal powder pyrolysis and iron ore powder reduction are performed in a circulating fluidized bed reaction tower in a coordinated manner, the coal powder pyrolysis gas-phase product can effectively increase the reduction potential of the reduction gas, and the pyrolysis solid-phase product (coke powder) can effectively prevent adhesion in the iron ore powder reduction reaction. Through the magnetic separation device, the directly reduced iron is further collected, and resources are effectively utilized. The exhaust gas is reasonably and plurally utilized by the bag-type dust collector.
(2) The system flow constructed by the invention basically realizes closed circulation and has the advantage of low energy consumption.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, are included to provide a further understanding of the application, and the description of the exemplary embodiments and illustrations of the application are intended to explain the application and are not intended to limit the application.
FIG. 1 is a process system flow diagram of the present invention;
the system comprises a circulating fluidized bed reaction tower 1, a high-temperature cyclone separator 2, a material return pipe 3, a material discharge pipe 4, a material discharge pipe 5, a magnetic separation device 6, direct reduced iron 7, a gasification burner 8, a gasification reformer 9, gasification reforming reducing gas 10, ash, 11, an exhaust gas regenerative heat exchanger 12, a water-cooled heat exchanger 13, a bag-type dust remover 14, an exhaust gas burner 15, cold air 16, a hot blast stove 17, cold air 18, flue gas 19, a coal dust bin 20 and an iron ore dust bin.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
The embodiment provides a direct reduction system for short-flow smelting of pulverized coal and mineral powder based on a circulating fluidized bed, which mainly comprises a pulverized coal bin 19, an iron ore powder bin 20, a circulating fluidized bed reaction tower 1, a high-temperature cyclone separator 2, a material return pipe 3, a material discharge pipe 4, a magnetic separation device 5, a gasification reforming furnace 8, an exhaust gas regenerative heat exchanger 11, a water-cooled heat exchanger 12, a bag-type dust remover 13 and a hot blast stove 16, as shown in fig. 1; wherein the coal powder bin and the iron ore powder bin are respectively connected with the circulating fluidized bed reaction tower; the outlet of the circulating fluidized bed reaction tower 1 is connected with a high-temperature cyclone separator 2, the solid phase outlet end of the high-temperature cyclone separator 2 is divided into two paths, and one path returns to the bottom of the fluidized bed reaction tower 1 through a material return pipe 3 to continue the reduction reaction; one path enters a magnetic separation device 5 through a discharge pipe; the gas-phase outlet end of the high-temperature cyclone separator 2 is connected with a waste gas backheating heat exchanger 11; the magnetic separation device 5 is connected with the gasification reforming furnace 8, the outlet of the exhaust gas regenerative heat exchanger 11 is divided into two paths, one path is connected with the gasification reforming furnace 8, and the other path is connected with the hot blast stove 16; the hot end outlet of the lower part of the exhaust gas heat recovery heat exchanger 11 is connected with the hot end inlet of the water cooling heat exchanger 12; the outlet of the hot end of the water-cooled heat exchanger 12 is connected with a bag-type dust collector 13. The inlet of the gasification reforming furnace 8 is composed of coke breeze from the magnetic separation device 5 and hot air from the hot-blast stove 16 by the gasification burner 7, so that the coke breeze and the hot air are fully mixed and gasified to generate reducing gas, and the gasified ash 10 is discharged from the bottom of the furnace. The upper part of the hot blast stove 16 is provided with a waste gas burner 14 which organizes the waste gas and the cold air 15 from the waste gas backheating heat exchanger 11 to ensure that the waste gas and the cold air are fully combusted to generate heat, and the cold air 17 is heated by a heat exchange surface arranged in the stove body to provide hot air for the gasification reforming of the gasification reforming stove 8.
Each device effectively builds a system, realizes the basic closed circulation of the material and the energy of the system, and greatly reduces the energy consumption of the system.
Furthermore, the exhaust gas heat recovery heat exchanger is a gas-gas heat exchanger, and circulating coal gas is heated, so that the temperature after pyrolysis and reduction reaction is reduced, and the sensible heat of the coal gas is fully utilized; and secondly, the circulating coal gas is heated, the temperature of the circulating coal gas is increased, the energy consumption of the gasification reforming furnace is reduced, and the efficiency of the hot blast stove is improved.
Furthermore, the hot blast stove adopts an indirect heat exchange mode, the exhaust burner is used for burning and backheating the exhaust to generate high-temperature flue gas, and cold air is heated through a heat exchange surface arranged in the stove to obtain high-temperature hot air.
Furthermore, the system also comprises a water-cooling heat exchanger which is arranged between the exhaust gas heat regenerative heat exchanger and the bag-type dust remover and has the function of regulating and controlling the air temperature to meet the requirement that the outlet temperature (namely the inlet temperature of the bag-type dust remover) is in the range of 150-200 ℃ so as to ensure the normal operation of the bag-type dust remover.
A circulating fluidized bed direct reduction process for short-process smelting of coal dust and mineral powder comprises the following steps:
respectively feeding coal powder and iron ore powder at the bottom of the circulating fluidized bed, and finishing the quick pyrolysis of the coal powder and the direct reduction of the iron ore powder in the circulating fluidized bed along with the high-temperature reducing gas for 3-10 s; after the reaction, the gas-solid mixture enters a high-temperature cyclone separator for separation, part of the separated solid phase product is circularly returned to the bottom of the fluidized bed for repeated reduction, and part of the separated solid phase product enters a magnetic separator; the separated gas phase enters a waste gas regenerative heat exchanger for heat exchange to heat the circulating cold gas; one part of the heated circulating cold gas is sent to a gasification reforming furnace, and the sensible heat of the high-temperature gasification gas is utilized to carry out reforming reaction with excessive carbon, so that CO in the circulating gas is converted into CO2And H2Reforming of O to CO and H2(ii) a One strand is sent to hot air for combustion, and the air is heated to provide high-temperature air for the gasification reforming furnace; the reducing gas 9 generated by the gasification reforming furnace enters a circulating fluidized bed after the temperature of the circulating cold coal gas is adjusted, and is coal powder pyrolysis and iron ore powderReduction provides a heat source and a medium (both as fluidizing medium and reducing medium); and (3) allowing the pyrolyzed and reduced main gas to flow through a waste gas heat recovery heat exchanger and then enter a water-cooled heat exchanger, and adjusting the temperature and then enter a bag-type dust collector.
In the circulating fluidized bed, the coal powder pyrolysis gas-phase product is mainly cracked into H2And CO, increasing the reduction potential of the reducing gas; the pulverized coal pyrolysis solid-phase product coke powder plays a role in preventing reduced iron from being adhered.
As a further implementation mode, in the magnetic separation separator, the magnetically separated part is directly reduced iron 6, and the coke powder which is not magnetically separated is directly sent to a gasification reforming furnace to be gasified to prepare reducing gas.
As a further implementation mode, coal powder pyrolysis and iron ore powder reduction are cooperatively generated in the circulating fluidized bed reaction tower, the reaction atmosphere is obtained by adjusting the temperature of the reducing gas generated by the gasification reforming furnace through circulating cold gas, the temperature range after temperature adjustment is 1000-1200 ℃, and the temperature range after pyrolysis and reduction reaction is 800-1000 ℃.
As a further implementation mode, the gasification raw material of the gasification reforming furnace is a product separated by a magnetic separation device, mainly comprises high-temperature coke powder and waste residue which is not subjected to magnetic separation, the gasification agent is hot air from a hot blast stove, and the temperature range of the hot air is 600-1000 ℃. The reforming reaction is to return exhaust gas for the circulation heated by the regenerative heat exchanger, and use the high temperature of coke powder gasification to convert CO in the exhaust gas into CO under the premise of excessive carbon2、H2Reforming of O to CO and H2So that the alloy has reducibility again.
As a further realisation, the hot air of the stove is heated by cold air 17. The flue gas 18 of the stove may be discharged from the bottom.
As a further implementation mode, bag-type ash collected by the bag-type dust remover is conveyed to the gasification reforming furnace by air force to participate in gasification, exhaust gas at the outlet of the bag-type dust remover is divided into three paths for use, one path is circulated to the exhaust gas backheating heat exchanger, the other path is circulated to the outlet of the gasification reforming furnace, and the other path is supplied externally.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made to the present application by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (10)
1. A circulating fluidized bed direct reduction system for short-process smelting of coal powder and mineral powder is characterized by mainly comprising a coal powder bin, an iron ore powder bin, a circulating fluidized bed reaction tower, a high-temperature cyclone separator, a feed back pipe, a discharge pipe, a magnetic separation device, a gasification reforming furnace, an exhaust gas regenerative heat exchanger, a bag-type dust remover and a hot blast furnace; wherein, the coal dust bin and the iron ore dust bin are respectively connected with the circulating fluidized bed reaction tower; the outlet of the circulating fluidized bed reaction tower is connected with a high-temperature cyclone separator, the solid phase outlet end of the high-temperature cyclone separator is divided into two paths, and one path returns to the bottom of the fluidized bed reaction tower through a material return pipe to continue reduction reaction; one path enters a magnetic separation device through a discharge pipe; the gas-phase outlet end of the high-temperature cyclone separator is connected with a waste gas regenerative heat exchanger; the magnetic separation device is connected with the gasification reforming furnace; the outlet of the exhaust gas heat regenerative heat exchanger is divided into two paths, one path is connected with the gasification reforming furnace, and the other path is connected with the hot blast stove; the hot end outlet of the exhaust gas backheating heat exchanger is connected with the hot end inlet of the water cooling heat exchanger; the hot end outlet of the water-cooling heat exchanger is connected with a bag-type dust collector.
2. The circulating fluidized bed direct reduction system for short-process smelting of pulverized coal and mineral powder according to claim 1, wherein the exhaust gas regenerative heat exchanger is a gas-gas heat exchanger.
3. The circulating fluidized bed direct reduction system for short-process smelting of pulverized coal and mineral powder according to claim 1, wherein the water-cooled heat exchanger is used for regulating and controlling air temperature, and the outlet temperature range is 150-200 ℃.
4. A circulating fluidized bed direct reduction process for short-process smelting of coal powder and mineral powder is characterized by comprising the following steps:
circulating flow of coal powder and iron ore powderThe bottom parts of the fluidized beds are respectively fed, and the pulverized coal fast pyrolysis and the direct reduction of the iron ore powder are completed in the circulating fluidized bed along with the upward movement of high-temperature reducing gas for 3 to 10 seconds; after reaction, the gas-solid mixture enters a high-temperature cyclone separator for separation, part of the separated solid phase product is circularly returned to the bottom of the fluidized bed for repeated reduction, and the other part of the solid phase product enters a magnetic separator; the separated gas phase enters a waste gas heat recovery heat exchanger for heat exchange, and the circulating cold gas is heated; one part of the heated circulating cold gas is sent to a gasification reforming furnace, and the sensible heat of the high-temperature gasification gas is utilized to carry out reforming reaction with excessive carbon, so that CO in the circulating gas is converted into CO2And H2Reforming of O to CO and H2(ii) a One strand is sent to hot air for combustion, and the air is heated to provide high-temperature air for the gasification reforming furnace; the reducing gas generated by the gasification reforming furnace enters a circulating fluidized bed after the temperature of the circulating cold gas is adjusted, and a heat source and a medium are provided for coal dust pyrolysis and iron ore powder reduction; and the main gas after pyrolysis and reduction flows through the exhaust gas backheating heat exchanger and then enters the water-cooled heat exchanger, and the main gas after temperature adjustment enters the bag-type dust remover.
5. The circulating fluidized bed direct reduction process for short-process smelting of pulverized coal and mineral powder according to claim 4, characterized in that in the magnetic separation separator, the magnetically separated part is directly reduced iron, and the coke powder which is not magnetically separated is directly sent to the gasification reforming furnace for gasification to prepare reducing gas.
6. The circulating fluidized bed direct reduction process for short-process smelting of coal dust and ore powder according to claim 4, characterized in that coal dust pyrolysis and iron ore powder reduction are cooperatively generated in the circulating fluidized bed reaction tower, and the reaction atmosphere is obtained by adjusting the temperature of circulating cold coal gas of reducing gas generated by the gasification reforming furnace.
7. The direct reduction process of the circulating fluidized bed for the short-process smelting of the coal dust and the mineral powder according to claim 6, wherein the temperature range after the temperature adjustment is 1000-1200 ℃, and the temperature range after the pyrolysis and reduction reaction is 800-1000 ℃.
8. The circulating fluidized bed direct reduction process for short-process smelting of coal dust and mineral powder according to claim 4, wherein the gasification raw material of the gasification reformer is high-temperature coke powder separated by a magnetic separation device, the gasifying agent is hot air from a hot blast stove, and the temperature range of the hot air is 600-1000 ℃.
9. The circulating fluidized bed direct reduction process for short-process smelting of coal dust and mineral powder according to claim 4, characterized in that bag-type ash collected by the bag-type dust remover is pneumatically conveyed to a gasification reformer to participate in gasification.
10. The circulating fluidized bed direct reduction process for short-process smelting of pulverized coal and mineral powder according to claim 9, wherein exhaust gas at an outlet of the bag-type dust remover is used in three ways, one way is circulated to the exhaust gas regenerative heat exchanger, the other way is circulated to an outlet of the gasification reformer, and the other way is supplied externally.
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Citations (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3844766A (en) * | 1973-12-26 | 1974-10-29 | Midland Ross Corp | Process for reducing iron oxide to metallic sponge iron with liquid or solid fuels |
| CN1961084A (en) * | 2004-05-31 | 2007-05-09 | 奥托昆普技术公开有限公司 | Direct reduction device and method |
| CN101397597A (en) * | 2007-09-26 | 2009-04-01 | 宝山钢铁股份有限公司 | Method for producing spongy iron by direct reduction of dry coal powder gasification and hot coal gas fine ore fluidized bed |
| CN203333697U (en) * | 2013-05-23 | 2013-12-11 | 北京神雾环境能源科技集团股份有限公司 | Cold-feeding fluidized-bed smelting system for preparing reducing gas through medium-level and low-level coal gasification |
| CN203333696U (en) * | 2013-05-23 | 2013-12-11 | 北京神雾环境能源科技集团股份有限公司 | Fluidized-bed smelting system for preparing reducing gas through medium-level and low-level coal gasification |
| CN104152165A (en) * | 2014-08-19 | 2014-11-19 | 合肥乾海洁净煤技术有限公司 | Gas cycle coal full-particle diameter grading, pyrolyzing and coupling metallurgy reduction technology and system thereof |
| CN204039332U (en) * | 2014-08-19 | 2014-12-24 | 合肥乾海洁净煤技术有限公司 | The metallurgical restoring system of coal gas circulation coal wholegrain radial sector pyrolysis coupling |
| CN104673954A (en) * | 2015-02-13 | 2015-06-03 | 湖南长拓高科冶金有限公司 | Direct-reduction ironmaking method and system for iron-containing mineral powder |
| KR20150062249A (en) * | 2013-11-28 | 2015-06-08 | 주식회사 포스코 | Apparatus for manufacturing molten iron |
| CA2938641A1 (en) * | 2013-12-31 | 2015-07-09 | Institute Of Process Engineering, Chinese Academy Of Sciences | System and method for fluidized reduction of iron ore powder |
| CN105408500A (en) * | 2013-07-31 | 2016-03-16 | 米德雷克斯技术公司 | Reducing iron oxide to metallic iron using natural gas |
| CN105543437A (en) * | 2012-10-24 | 2016-05-04 | 沈阳东方钢铁有限公司 | Two-stage type entrained flow bed iron ore powder reduction process |
| CN109321703A (en) * | 2018-11-02 | 2019-02-12 | 山东大学 | A kind of short route fused reduction iron-smelting system and method |
| CN109680114A (en) * | 2019-01-29 | 2019-04-26 | 山东大学 | A kind of system and method for coal gasification collaboration reduction of iron ore |
| CN209243092U (en) * | 2018-11-02 | 2019-08-13 | 山东大学 | A kind of short route fused reduction iron-smelting system |
| CN110218831A (en) * | 2019-06-27 | 2019-09-10 | 山东大学 | A kind of be fully warmed-up cooperates with molten iron reduction apparatus and method with the coal gasification of gas phase prereduction |
| CN110438278A (en) * | 2019-09-11 | 2019-11-12 | 武汉科思瑞迪科技有限公司 | A kind of Shaft Furnace Direct Reduction Process of gas base and the combination of coal base phase |
| CN111961784A (en) * | 2020-08-31 | 2020-11-20 | 山东大学 | Method and system for reduction reaction of iron ore powder in bubbling bed |
| CN213507040U (en) * | 2020-10-21 | 2021-06-22 | 山东大学 | Device for producing direct reduced iron by circularly reducing iron ore powder |
| CN113025771A (en) * | 2021-03-05 | 2021-06-25 | 山东大学 | Grate type direct reduced iron production system and method for sintering machine |
| CN113583719A (en) * | 2021-07-29 | 2021-11-02 | 山东大学 | Synthesis gas production method and system for synergetic hydrogen-rich gasification and reforming pyrolysis |
| CN114574651A (en) * | 2022-01-24 | 2022-06-03 | 山东大学 | Rotational flow iron wall melting smelting device and method |
-
2022
- 2022-07-11 CN CN202210810095.8A patent/CN115261542B/en active Active
Patent Citations (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3844766A (en) * | 1973-12-26 | 1974-10-29 | Midland Ross Corp | Process for reducing iron oxide to metallic sponge iron with liquid or solid fuels |
| CN1961084A (en) * | 2004-05-31 | 2007-05-09 | 奥托昆普技术公开有限公司 | Direct reduction device and method |
| CN101397597A (en) * | 2007-09-26 | 2009-04-01 | 宝山钢铁股份有限公司 | Method for producing spongy iron by direct reduction of dry coal powder gasification and hot coal gas fine ore fluidized bed |
| CN105543437A (en) * | 2012-10-24 | 2016-05-04 | 沈阳东方钢铁有限公司 | Two-stage type entrained flow bed iron ore powder reduction process |
| CN203333697U (en) * | 2013-05-23 | 2013-12-11 | 北京神雾环境能源科技集团股份有限公司 | Cold-feeding fluidized-bed smelting system for preparing reducing gas through medium-level and low-level coal gasification |
| CN203333696U (en) * | 2013-05-23 | 2013-12-11 | 北京神雾环境能源科技集团股份有限公司 | Fluidized-bed smelting system for preparing reducing gas through medium-level and low-level coal gasification |
| CN105408500A (en) * | 2013-07-31 | 2016-03-16 | 米德雷克斯技术公司 | Reducing iron oxide to metallic iron using natural gas |
| KR20150062249A (en) * | 2013-11-28 | 2015-06-08 | 주식회사 포스코 | Apparatus for manufacturing molten iron |
| CA2938641A1 (en) * | 2013-12-31 | 2015-07-09 | Institute Of Process Engineering, Chinese Academy Of Sciences | System and method for fluidized reduction of iron ore powder |
| CN104152165A (en) * | 2014-08-19 | 2014-11-19 | 合肥乾海洁净煤技术有限公司 | Gas cycle coal full-particle diameter grading, pyrolyzing and coupling metallurgy reduction technology and system thereof |
| CN204039332U (en) * | 2014-08-19 | 2014-12-24 | 合肥乾海洁净煤技术有限公司 | The metallurgical restoring system of coal gas circulation coal wholegrain radial sector pyrolysis coupling |
| CN104673954A (en) * | 2015-02-13 | 2015-06-03 | 湖南长拓高科冶金有限公司 | Direct-reduction ironmaking method and system for iron-containing mineral powder |
| CN109321703A (en) * | 2018-11-02 | 2019-02-12 | 山东大学 | A kind of short route fused reduction iron-smelting system and method |
| CN209243092U (en) * | 2018-11-02 | 2019-08-13 | 山东大学 | A kind of short route fused reduction iron-smelting system |
| CN109680114A (en) * | 2019-01-29 | 2019-04-26 | 山东大学 | A kind of system and method for coal gasification collaboration reduction of iron ore |
| CN110218831A (en) * | 2019-06-27 | 2019-09-10 | 山东大学 | A kind of be fully warmed-up cooperates with molten iron reduction apparatus and method with the coal gasification of gas phase prereduction |
| CN110438278A (en) * | 2019-09-11 | 2019-11-12 | 武汉科思瑞迪科技有限公司 | A kind of Shaft Furnace Direct Reduction Process of gas base and the combination of coal base phase |
| CN111961784A (en) * | 2020-08-31 | 2020-11-20 | 山东大学 | Method and system for reduction reaction of iron ore powder in bubbling bed |
| CN213507040U (en) * | 2020-10-21 | 2021-06-22 | 山东大学 | Device for producing direct reduced iron by circularly reducing iron ore powder |
| CN113025771A (en) * | 2021-03-05 | 2021-06-25 | 山东大学 | Grate type direct reduced iron production system and method for sintering machine |
| CN113583719A (en) * | 2021-07-29 | 2021-11-02 | 山东大学 | Synthesis gas production method and system for synergetic hydrogen-rich gasification and reforming pyrolysis |
| CN114574651A (en) * | 2022-01-24 | 2022-06-03 | 山东大学 | Rotational flow iron wall melting smelting device and method |
Non-Patent Citations (1)
| Title |
|---|
| 于鲁: "铁矿粉对铁焦炭化过程体积演变的影响", 《钢铁研究学报》, vol. 31, no. 6, 15 June 2019 (2019-06-15), pages 515 - 521 * |
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