CN114941046A - System and method for directly reducing iron ore by hydrogen based on circulating fluidized bed - Google Patents
System and method for directly reducing iron ore by hydrogen based on circulating fluidized bed Download PDFInfo
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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
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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
- C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
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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
- C21B13/0073—Selection or treatment of the reducing gases
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
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- 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
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- 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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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
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Abstract
The invention provides a system and a method for directly reducing iron ore by hydrogen based on a circulating fluidized bed, wherein the system comprises: a hydrogen production subsystem for providing hydrogen; the gas circulation subsystem is used for collecting high-temperature flue gas of the circulating fluidized bed and preheating fluidized air through the high-temperature flue gas; the raw material feeding subsystem is used for providing iron ore powder raw materials; and the circulating fluidized bed performs reduction reaction on the iron ore powder raw material provided by the raw material feeding subsystem through hydrogen provided by the hydrogen production subsystem and fluidized air provided by the gas circulating subsystem to generate high-temperature flue gas, iron and slag. The invention solves the problem that the existing gas-based direct reduced iron technology can not completely solve the problem of carbon dioxide emission, and realizes zero emission of carbon dioxide.
Description
[ technical field ] A method for producing a semiconductor device
The invention relates to the technical field of ferrous metallurgy, in particular to a system and a method for directly reducing iron ore by hydrogen based on a circulating fluidized bed.
[ background of the invention ]
The steel industry is one of the main emission sources of carbon dioxide, the carbon emission of the steel industry accounts for 5% -6% of the total emission in the world, and 15% of the carbon dioxide emission in China is generated by the steel industry. At present, 1 ton of molten iron is smelted, and 1.58 tons of carbon dioxide are discharged. Therefore, in order to realize the carbon peak reaching and carbon neutralization targets in the steel industry, the process of directly reducing the iron ore by using the hydrogen is an effective method for thoroughly solving the problem of high carbon dioxide emission in the pig iron smelting process represented by a blast furnace.
The prior art related to the invention comprises a blast furnace hydrogen-rich smelting technology, and realizes carbon emission reduction by blowing hydrogen-rich reducing gas; the technology of a full hydrogen reduction shaft furnace.
The reducing agent of the existing gas-based direct reduced iron technology is mainly reducing gas generated by catalytic cracking of natural gas abroad, and the reducing gas is CO and H 2 In which H is 2 Up to a volume fraction of 55%; in China, coal gas is mainly used, for example, a coal gas + reduction shaft furnace process (B-L method of Bao steel), although the above technologies are all gas-based direct reduced iron, the technology is still in the category of carbon metallurgy, and a large amount of carbon dioxide is still discharged.
The invention obtains electric energy through solar photovoltaic power generation and wind energy power generation, then utilizes electrolyzed water to prepare hydrogen, and the prepared hydrogen is sent into a circulating fluidized bed reactor to directly reduce iron ore, and finally pure iron or molten iron is obtained. The invention does not need the coking process and the sintering process in the traditional blast furnace ironmaking process, thoroughly realizes the carbon-free metallurgy, and has no carbon dioxide emission in the whole process flow. The invention can adopt iron ore powder with the granularity range of 0-8mm, and saves the procedure of sintering iron ore compared with the traditional blast furnace. The circulating fluidized bed has high-efficiency heat and mass transfer, long residence time and high gas-solid reaction rate, so that the reduction efficiency of the hydrogen to the iron ore powder is far higher than that of a shaft furnace.
The circulating fluidized bed is the best reactor for gas-solid reaction, and has the advantages of high heat and mass transfer efficiency, high chemical reaction rate, long reaction residence time and the like due to the gas-solid two-phase fluidized state in the reactor, and is widely applied to chemical processes, coal combustion, coal gasification and the like. The direct reduction reaction of the hydrogen and the iron ore is realized in the circulating fluidized bed, which belongs to the field of hydrogen metallurgy, thoroughly realizes zero emission of carbon dioxide, and has important significance for realizing carbon neutralization in the steel industry.
Accordingly, there is a need to develop a system and method for direct reduction of iron ore based on hydrogen of a circulating fluidized bed to address the shortcomings of the prior art to solve or mitigate one or more of the problems set forth above.
[ summary of the invention ]
In view of the above, the invention provides a system and a method for directly reducing iron ore by using hydrogen based on a circulating fluidized bed, which solve the problem that the existing gas-based direct iron reduction technology cannot completely solve the emission of carbon dioxide and realize zero emission of carbon dioxide.
In one aspect, the present invention provides a system for direct reduction of iron ore with hydrogen based on a circulating fluidized bed, the system comprising:
a hydrogen production subsystem for providing hydrogen;
the gas circulation subsystem is used for collecting high-temperature flue gas of the circulating fluidized bed and preheating fluidized air externally added into the circulating fluidized bed through the high-temperature flue gas;
the raw material feeding subsystem is used for providing iron ore powder raw materials;
and the circulating fluidized bed performs reduction reaction on the iron ore powder raw material provided by the raw material feeding subsystem through hydrogen provided by the hydrogen production subsystem and fluidized air provided by the gas circulating subsystem to generate high-temperature flue gas, iron and slag.
The above aspects and any possible implementation manners further provide an implementation manner, the circulating fluidized bed includes a heating zone, a reduction zone, a gas-solid separation device and a material returning device, the heating zone is communicated below the reduction zone, the reduction zone is communicated with the gas-solid separation device, the upper end of the gas-solid separation device is communicated with the gas circulation subsystem, the lower end of the gas-solid separation device is communicated with the material returning device, and the heating zone is simultaneously communicated with the material returning device and the raw material feeding subsystem.
The above aspects and any possible implementation manners further provide an implementation manner, the gas circulation subsystem includes a fluidized air preheater, a condenser and a dust remover, one end of the fluidized air preheater is communicated with the upper end of the gas-solid separation device, the other end of the fluidized air preheater is communicated with the fluidized air, the fluidized air is preheated and then sent to the heating zone, and the bottom of the fluidized air preheater is communicated with the dust remover through the condenser.
The above aspects and any possible implementation manners further provide an implementation manner, wherein the gas circulation subsystem further comprises a water heater, the water heater is arranged between the condenser and the fluidized air preheater, the water heater is communicated with the hydrogen production subsystem and provides hydrogen production raw materials for the hydrogen production subsystem, and the water heater is communicated with the condenser in a bidirectional manner.
The above aspect and any possible implementation further provide an implementation in which the dust remover is open to the atmosphere.
The above aspects and any possible implementations further provide an implementation in which the system further includes a molten pool communicating with a bottom of the heating zone, the molten pool forming iron into an iron billet by slag iron separation.
The above aspects and any possible implementations further provide an implementation in which the hydrogen generation subsystem is an apparatus for generating hydrogen by electrolysis of water from a renewable energy source.
The above aspects and any possible implementations further provide a method for direct reduction of iron ore with hydrogen based on a circulating fluidized bed, the method comprising the steps of:
s1: hydrogen prepared by the hydrogen production subsystem is sent into a circulating fluidized bed, and iron ore powder is sent into a heating zone;
s2: the circulating fluidized bed is in a gas-solid two-phase circulating flow state, and preheated fluidized air is sent into a heating zone through an air distribution plate;
s3: the iron ore powder entering the heating zone is heated to the same temperature as the existing solid of the circulating fluidized bed, and then is subjected to reduction reaction with hydrogen in the reduction zone to generate iron and slag, and the reacted and unreacted iron ore powder enters a gas-solid separation device along with air flow;
s4: separating iron ore powder in a gas-solid separation device, and returning the iron ore powder to a heating zone through a material returning device to form circulation of the iron ore powder;
s5: discharging iron and slag into a melting tank at the bottom of a heating area in a continuous or intermittent iron discharging mode, and finally forming an iron blank through slag-iron separation;
s6: the high-temperature gas separated from the gas-solid separation device enters a fluidized air preheater to preheat normal-temperature fluidized air, then enters a condenser to condense and separate water, and finally is discharged into the atmosphere through a dust remover.
The above aspect and any possible implementation further provides an implementation, wherein the grain size of the iron ore powder in S1 is in the range of 0 to 8 mm.
In the aspect and any possible implementation manner described above, there is further provided an implementation manner, the preheated fluidizing air in S3 is air or a mixed gas of air and nitrogen, the temperature after preheating is 200-.
Compared with the prior art, the invention can obtain the following technical effects:
1): the invention relates to a method for directly reducing iron ore by hydrogen in a circulating fluidized bed, which belongs to the total hydrogen metallurgy technology, wherein hydrogen is used for replacing carbon, and gas is used for replacing coke, which is an important technical direction for realizing carbon neutralization in the steel industry;
2): the invention solves the problem that the existing gas-based direct reduced iron technology still cannot completely solve the problem of carbon dioxide emission, and realizes zero emission of carbon dioxide.
Of course, it is not necessary for any one product in which the invention is practiced to achieve all of the above-described technical effects simultaneously.
[ description of the drawings ]
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
FIG. 1 is a flow chart of the method provided in example 1 of the present invention;
fig. 2 is a flow chart of the method provided in embodiment 2 of the present invention.
[ detailed description ] embodiments
In order to better understand the technical scheme of the invention, the following detailed description of the embodiments of the invention is made with reference to the accompanying drawings.
It should be understood that the described embodiments are only some embodiments of the invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The terminology used in the embodiments of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used in the examples of the present invention and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.
The invention provides a system for directly reducing iron ore by hydrogen based on a circulating fluidized bed, which comprises:
a hydrogen production subsystem for providing hydrogen;
the gas circulation subsystem collects the high-temperature flue gas of the circulating fluidized bed and preheats fluidized air through the high-temperature flue gas;
the raw material feeding subsystem is used for providing iron ore powder raw materials;
and the circulating fluidized bed performs reduction reaction on the iron ore powder raw material provided by the raw material feeding subsystem through hydrogen provided by the hydrogen production subsystem and fluidized air provided by the gas circulating subsystem to generate high-temperature flue gas, iron and slag.
The circulating fluidized bed comprises a heating zone, a reduction zone, a gas-solid separation device and a material returning device, wherein the heating zone is communicated with the lower part of the reduction zone, the reduction zone is communicated with the gas-solid separation device, the upper end of the gas-solid separation device is communicated with a gas circulation subsystem, the lower end of the gas-solid separation device is communicated with the material returning device, and the heating zone is simultaneously communicated with the material returning device and a raw material feeding subsystem.
The gas circulation subsystem comprises a fluidized air preheater, a condenser and a dust remover, one end of the fluidized air preheater is communicated with the upper end of the gas-solid separation device, the other end of the fluidized air preheater is communicated with fluidized air, the fluidized air is preheated and then sent to a heating zone, and the bottom of the fluidized air preheater is communicated with the dust remover through the condenser.
In another embodiment, the gas circulation subsystem further comprises a water heater, the water heater is arranged between the condenser and the fluidized air preheater, the water heater is communicated with the hydrogen production subsystem and provides hydrogen production raw materials for the hydrogen production subsystem, and the water heater is communicated with the condenser in a bidirectional mode. The dust remover is communicated with the atmosphere.
The system also comprises a melting tank, wherein the melting tank is communicated with the bottom of the heating area, and iron is formed into an iron billet through slag-iron separation in the melting tank. The hydrogen production subsystem is a device for preparing hydrogen by using renewable energy sources through water electrolysis.
The invention also provides a method for directly reducing iron ore by hydrogen based on the circulating fluidized bed, which comprises the following steps:
s1: hydrogen prepared by the hydrogen production subsystem is sent into a circulating fluidized bed, and iron ore powder is sent into a heating zone;
s2: the circulating fluidized bed is in a gas-solid two-phase circulating flow state, and preheated fluidized air is sent into a heating zone through an air distribution plate;
s3: the iron ore powder entering the heating zone is heated to the same temperature as the existing solid of the circulating fluidized bed, and then is subjected to reduction reaction with hydrogen in the reduction zone to generate iron and slag, and the reacted and unreacted iron ore powder enters a gas-solid separation device along with air flow;
s4: separating iron ore powder in a gas-solid separation device, and returning the iron ore powder to a heating zone through a material returning device to form circulation of the iron ore powder;
s5: discharging iron and slag into a melting tank at the bottom of a heating area in a continuous or intermittent iron discharging mode, and finally forming an iron blank through slag-iron separation;
s6: the high-temperature gas separated from the gas-solid separation device enters a fluidized air preheater to preheat normal-temperature fluidized air, then enters a condenser to condense and separate water, and finally is discharged into the atmosphere through a dust remover.
The particle size of the iron ore powder in the S1 is in the range of 0-8 mm. The preheated fluidizing air in the S3 is air or a mixed gas of air and nitrogen, the temperature after preheating is 200-500 ℃, the temperature of the heating area and the reduction area is controlled at 700-1100 ℃, and the temperature difference between the heating area and the reduction area is controlled at 0-80 ℃.
The invention sends hydrogen prepared by renewable energy into a circulating fluidized bed device, and the circulating fluidized bed device mainly comprises a heating zone 1, a reduction zone 2, a gas-solid separation device 3 and a material returning device 4. The iron ore powder (the particle size range is 0-8mm) is sent into the heating zone 1, the circulating fluidized bed is in a gas-solid two-phase circulating flow state, preheated fluidized air (air or mixed gas of air and nitrogen, the temperature after preheating is about 200 plus 500 ℃) is also sent into the heating zone 1 through an air distribution plate, the temperature of the heating zone 1 and the temperature of the reduction zone 2 are controlled within 700 plus 1100 ℃, the temperature in the whole circulating fluidized bed is more uniform due to the fluidizing circulation of a large amount of iron ore powder, and the temperature difference of each part is controlled within 0-80 ℃.
The iron ore entering the heating zone 1 can be rapidly heated to the same temperature as the existing solids of the circulating fluidized bed, and then the hydrogen and the iron ore powder are subjected to a reduction reaction in the reduction zone 2, wherein the total package reaction equation of the reduction reaction is as follows:
Fe 2 O 3 +3H 2 →2Fe+3H 2 O(1)
the hydrogen and iron ore powder are subjected to iron ore reduction reaction in a reduction zone, the reacted and unreacted iron ore powder enters a gas-solid separation device 3 along with air flow, the iron ore powder is separated in the gas-solid separation device and enters a material returning device 4, and then the iron ore powder enters a heating zone 1 to form circulation of the iron ore powder.
Because the specific gravity of iron is larger than that of iron ore powder, iron and slag generated by the reduction reaction gradually sink to the bottom of the heating area 1, the iron and the slag are discharged into a melting tank in a continuous or intermittent iron discharge mode, and finally, iron and slag are separated to form an iron billet.
The high-temperature gas separated from the gas-solid separation device 3 firstly enters a fluidized air preheater to preheat normal-temperature fluidized air, then enters a condenser to condense and separate water, and finally is discharged into the atmosphere through a dust remover.
Example 1:
as shown in fig. 1, hydrogen prepared by renewable energy sources such as solar energy or wind energy is fed into a circulating fluidized bed device, and the circulating fluidized bed device mainly comprises a heating zone 1, a reduction zone 2, a gas-solid separation device 3 and a material returning device 4. The iron ore powder (the particle size range is 0-8mm) is sent into the heating zone 1, the preheated fluidized air is also sent into the heating zone 1 through the air distribution plate, the fluidized air is air or mixed gas of air and nitrogen, the iron ore powder is rapidly heated after entering the heating zone, only hydrogen and the iron ore powder generate iron ore reduction reaction in the reduction zone along with the gas-solid fluidization movement of the heating zone and the reduction zone, so the problem that the existing gas-based direct reduced iron technology cannot completely solve the emission of carbon dioxide is solved, and the zero emission of carbon dioxide is realized. The reacted and unreacted iron ore powder enters a gas-solid separation device 3 along with the air flow, and in the gas-solid separation device, the iron ore powder is separated and enters a material returning device 4 and then enters a heating zone 1 to form the circulation of the iron ore powder. The high-temperature gas separated from the gas-solid separation device 3 firstly enters a fluidized air preheater to preheat normal-temperature fluidized air, then enters a condenser to condense and separate water, and finally is discharged into the atmosphere through a dust remover. Iron and slag generated by reduction reaction in the circulating fluidized bed are discharged into a melting tank 5, and finally, iron and slag are separated to form an iron billet.
Example 2:
as shown in fig. 2, hydrogen prepared by renewable energy sources such as solar energy or wind energy is fed into a circulating fluidized bed device, and the circulating fluidized bed device mainly comprises a heating zone 1, a reduction zone 2, a gas-solid separation device 3 and a material returning device 4. The iron ore powder (the particle size range is 0-8mm) is sent into the heating zone 1, the preheated fluidized air is also sent into the heating zone 1 through the air distribution plate, the fluidized air is air or mixed gas of air and nitrogen, the iron ore powder is rapidly heated after entering the heating zone, only hydrogen and the iron ore powder generate iron ore reduction reaction in the reduction zone along with the gas-solid fluidization movement of the heating zone and the reduction zone, so the problem that the existing gas-based direct reduced iron technology cannot completely solve the emission of carbon dioxide is solved, and the zero emission of carbon dioxide is realized. The reacted and unreacted iron ore powder enters a gas-solid separation device 3 along with the air flow, and in the gas-solid separation device, the iron ore powder is separated and enters a material returning device 4 and then enters a heating zone 1 to form the circulation of the iron ore powder. The high-temperature gas separated from the gas-solid separation device 3 firstly enters a fluidized air preheater to preheat normal-temperature fluidized air, then enters a water heater to heat water to 80-90 ℃, and then enters a condenser to condense and separate the water in the condenser, the separated water enters the water heater after passing through a purification system, and the heated water is used as a raw material for hydrogen production by water electrolysis. The gas from the condenser is finally discharged to the atmosphere through a dust remover. Iron and slag generated by reduction reaction in the circulating fluidized bed are discharged into a melting tank 5, and finally, iron and slag are separated to form an iron billet.
The system and the method for directly reducing iron ore by using hydrogen based on the circulating fluidized bed provided by the embodiments of the present application are described in detail above. The above description of the embodiments is only for the purpose of helping to understand the method of the present application and its core ideas; meanwhile, for a person skilled in the art, according to the idea of the present application, there may be variations in the specific embodiments and the application scope, and in summary, the content of the present specification should not be construed as a limitation to the present application.
As used in the specification and claims, certain terms are used to refer to particular components. As one skilled in the art will appreciate, manufacturers may refer to a component by different names. This specification and claims do not intend to distinguish between components that differ in name but not function. In the following description and in the claims, the terms "include" and "comprise" are used in an open-ended fashion, and thus should be interpreted to mean "include, but not limited to. "substantially" means within an acceptable error range, that a person skilled in the art can solve the technical problem within a certain error range to substantially achieve the technical effect. The description which follows is a preferred embodiment of the present application, but is made for the purpose of illustrating the general principles of the application and not for the purpose of limiting the scope of the application. The protection scope of the present application shall be subject to the definitions of the appended claims.
It should also be noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a good or system that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such good or system. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of additional like elements in the article of commerce or system in which the element is comprised.
It should be understood that the term "and/or" as used herein is merely one type of association that describes an associated object, meaning that three relationships may exist, e.g., a and/or B may mean:
a exists alone, A and B exist simultaneously, and B exists alone. In addition, the character "/" herein generally indicates that the former and latter related objects are in an "or" relationship.
The foregoing description shows and describes several preferred embodiments of the present application, but as aforementioned, it is to be understood that the application is not limited to the forms disclosed herein, but is not to be construed as excluding other embodiments and is capable of use in various other combinations, modifications, and environments and is capable of changes within the scope of the application as described herein, commensurate with the above teachings, or the skill or knowledge of the relevant art. And that modifications and variations may be effected by those skilled in the art without departing from the spirit and scope of the application, which is to be protected by the claims appended hereto.
Claims (10)
1. A system for direct reduction of iron ore by hydrogen based on a circulating fluidized bed, comprising:
a hydrogen production subsystem for providing hydrogen;
the gas circulation subsystem is used for collecting high-temperature flue gas of the circulating fluidized bed and preheating fluidized air externally added into the circulating fluidized bed through the high-temperature flue gas;
the raw material feeding subsystem is used for providing iron ore powder raw materials;
and the circulating fluidized bed performs reduction reaction on the iron ore powder raw material provided by the raw material feeding subsystem through hydrogen provided by the hydrogen production subsystem and fluidized air provided by the gas circulating subsystem to generate high-temperature flue gas, iron and slag.
2. The system of claim 1, wherein the circulating fluidized bed comprises a heating zone, a reduction zone, a gas-solid separation device and a material returning device, the heating zone is communicated with the reduction zone, the reduction zone is communicated with the gas-solid separation device, the upper end of the gas-solid separation device is communicated with the gas circulation subsystem, the lower end of the gas-solid separation device is communicated with the material returning device, and the heating zone is simultaneously communicated with the material returning device and the raw material feeding subsystem.
3. The system of claim 2, wherein the gas circulation subsystem comprises a fluidizing air preheater, a condenser and a dust remover, the fluidizing air preheater is communicated with the upper end of the gas-solid separation device, and the bottom of the fluidizing air preheater is communicated with the dust remover through the condenser.
4. The system of claim 3, wherein the gas circulation subsystem further comprises a water heater disposed between the condenser and the fluidized air preheater, the water heater being in communication with the hydrogen production subsystem and providing a hydrogen production feedstock for the hydrogen production subsystem, the water heater being in bidirectional communication with the condenser.
5. The system of claim 3, wherein the dust separator is open to the atmosphere.
6. The system of claim 1, further comprising a molten pool communicating with the bottom of the heating zone, wherein the molten pool forms iron into an iron billet by slag iron separation.
7. The system of claim 1, wherein the hydrogen generation subsystem is a device that generates hydrogen from renewable energy sources by electrolyzing water.
8. A method for direct reduction of iron ore by hydrogen based on a circulating fluidized bed comprising the system according to any one of claims 1 to 7, characterized in that it comprises the steps of:
s1: hydrogen prepared by the hydrogen production subsystem is sent into a circulating fluidized bed, and iron ore powder is sent into a heating zone;
s2: sending the preheated fluidized air in the circulating fluidized bed into a heating zone;
s3: the iron ore powder entering the heating zone is heated to the same temperature as the existing solid of the circulating fluidized bed, and then is subjected to reduction reaction with hydrogen in the reduction zone to generate iron and slag, and the reacted and unreacted iron ore powder enters a gas-solid separation device along with air flow;
s4: separating iron ore powder in a gas-solid separation device, and returning the iron ore powder to a heating zone through a material returning device to form circulation of the iron ore powder;
s5: discharging iron and slag into a melting tank at the bottom of a heating area in a continuous or intermittent iron discharging mode, and finally forming an iron blank through slag-iron separation;
s6: the high-temperature gas separated from the gas-solid separation device enters a fluidized air preheater to preheat normal-temperature fluidized air, then enters a condenser to condense and separate water, and finally is discharged into the atmosphere through a dust remover.
9. The method according to claim 8, wherein the particle size of the iron ore powder in S1 is in the range of 0-8 mm.
10. The method as claimed in claim 8, wherein the preheated fluidizing air in S3 is air or a mixture of air and nitrogen, the temperature after preheating is 200-500 ℃, the temperature of the heating zone and the reduction zone is controlled at 700-1100 ℃, and the temperature difference between the heating zone and the reduction zone is controlled at 0-80 ℃.
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| AU3430695A (en) * | 1994-10-20 | 1996-05-02 | Outotec Oyj | Process for the heat treatment of fine-grained iron ore and for the conversion of the heat-treated iron ore to mettalic iron |
| CN203159661U (en) * | 2013-04-09 | 2013-08-28 | 莱芜钢铁集团有限公司 | Solar power generating hydrogen-production steelmaking device and reductant supply system thereof |
| RU2590029C1 (en) * | 2015-01-12 | 2016-07-10 | Общество с ограниченной ответственностью "Научно-производственное внедренческое предприятие ТОРЭКС" | Method for production of sponge iron and shaft furnace therefor |
| CN213835553U (en) * | 2020-11-09 | 2021-07-30 | 中国石油大学(北京) | Metallurgical system is united to electrolytic water hydrogen manufacturing |
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