CN111270037A - System and process method for producing sponge iron by directly reducing hydrogen-rich synthesis gas - Google Patents
System and process method for producing sponge iron by directly reducing hydrogen-rich synthesis gas Download PDFInfo
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- CN111270037A CN111270037A CN202010261857.4A CN202010261857A CN111270037A CN 111270037 A CN111270037 A CN 111270037A CN 202010261857 A CN202010261857 A CN 202010261857A CN 111270037 A CN111270037 A CN 111270037A
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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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- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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
- Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
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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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- 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
- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
Abstract
The invention belongs to the technical field of smelting, and discloses a system and a process method for producing sponge iron by directly reducing hydrogen-rich synthesis gas, which take synthesis gas which is a byproduct in the preparation of acetylene from natural gas as a raw material to prepare sponge iron, wherein the raw material gas is sent into a reduction reaction furnace through two paths, one path is heated and directly participates in the reaction, and the other path is used for exchanging heat and reducing the temperature of a reaction product; the tail gas at the top of the reduction reaction furnace is subjected to heat exchange, temperature reduction, dust removal and dehydration, then is compressed and pressurized, enters a decarbonizing device to remove carbon dioxide to obtain circulating synthesis gas, the circulating synthesis gas returns to a raw material gas pipeline to be used as part of the reduction reaction gas to exchange heat with the tail gas at the top of the reduction reaction furnace, one part of the reducing reaction gas is directly introduced into the bottom of the reduction reaction furnace, the heat of sponge iron is recovered while the reduction reaction is carried out, and CO formed in the decarbonizing process2Used for reducing the sealing gas of the reaction furnace. The system and the process fully recover heat, have high energy utilization rate and low device energy consumption, do not need to additionally consume inert sealing gas, and are a green and environment-friendly circulating process.
Description
Technical Field
The invention relates to the technical field of smelting, in particular to a system and a process method for producing sponge iron by directly reducing hydrogen-rich synthesis gas.
Background
The iron and steel industry is the basic industry of national economy and also the key industry of energy resource consumption and pollution emission in China. The method is a future development direction of the steel industry in order to accelerate the structure adjustment and the industry upgrade of the steel industry, change the development mode of the steel industry and promote the conservation, the cleanness and the sustainable development.
The direct reduction process is a typical non-blast furnace ironmaking process, and is an important link for realizing a short steel production process, namely a scrap steel/sponge iron process. More than 90% of the direct reduced iron in the world today is produced by gas-based processes. The representative processes are Midrex shaft furnace method and HYL reaction tank method. The Midrex shaft furnace method takes natural gas as raw material gas and furnace top gas as a transforming agent, and high-quality reducing gas is prepared by reforming. In the reformer, natural gas and a portion of the CO in the top gas2And H2And carrying out reforming reaction on the O under the action of a nickel catalyst to obtain reducing gas, and feeding the reducing gas into the shaft furnace for carrying out iron reduction reaction. The top gas of the shaft furnace is partly used as a reformer and partly as fuel for the reformer.
The iron-making process is a high-temperature reaction, and the obtained product has high temperature in the reaction, so that the product obtained from the bottom of the reaction furnace has high temperature, needs cooling, consumes a large amount of refrigerants and increases energy consumption. In addition, in iron ore iron-making reaction, because the typical reduction reaction needs to seal the furnace body feeding and discharging port to ensure the reaction to be carried out in the reducing atmosphere, at present, the mode of additionally using inert gas is adopted for sealing, and the defect brought by the method is that gas impurities can be introduced and the industrial cost is increased.
Disclosure of Invention
The invention aims to provide a system and a process method for producing sponge iron by directly reducing hydrogen-rich synthetic gas, aiming at solving the technical problems in the prior art, and solving the problems of heat waste and waste gas utilization caused by high temperature of products in the process when the hydrogen-rich synthetic gas byproduct obtained by preparing acetylene from natural gas is used as iron-making reducing gas.
The invention takes the hydrogen-rich synthetic gas which is a byproduct of acetylene preparation from natural gas as a reducing gas source for preparing iron, wherein the hydrogen-rich synthetic gas refers to a reducing gas source with the composition of H2: CO volume ratio greater than 2:1, and H2The sum of the content of the CO and the CO accounts for more than 85 percent of the total volume of the byproducts, namely the system and the method for producing the sponge iron by reducing by using the CO as the raw material are provided in the invention.
In addition, the raw material synthesis gas in the invention refers to gas discharged from a hydrogen-rich synthesis gas source and used for iron making reaction, and the circulating synthesis gas refers to H-containing gas formed by processing reduction reaction furnace top gas2And CO, which is a gas that can be used in the iron making reaction.
The invention provides a system for producing sponge iron by directly reducing hydrogen-rich synthesis gas, which comprises the following components: a hydrogen-rich synthesis gas source, a heating furnace, a reduction reaction furnace, a heat exchanger, a dust remover and a decarburization device; two gas communication passages are arranged between the hydrogen-rich synthesis gas source and the reduction reaction furnace and are used for sending gas in the hydrogen-rich synthesis gas source into the reduction reaction furnace through a pipeline, wherein the first gas passage is communicated with the middle part of the reduction reaction furnace, a heating furnace is arranged on the gas passage, and the first gas passage at the front end of the heating furnace passes through the inside of the heat exchanger; the second gas passage is communicated with the bottom of the reduction reaction furnace; the reduction reaction furnace is a reactor for carrying out sealed reaction on iron ore and hydrogen-rich synthesis gas, and comprises a bottom discharge hole and a top exhaust port; the top exhaust port is connected with an inlet of a dust remover, the connecting passage passes through the inside of the heat exchanger, and an outlet of the dust remover is connected with an inlet of a decarburization device; a first outlet of the decarburization device is connected to an outlet of a hydrogen-rich synthesis gas source, and a second outlet of the decarburization device is respectively connected with a top exhaust port and a bottom discharge port of the reduction reaction furnace; the heat exchanger is used for exchanging heat between the tail gas at the top of the reduction reaction furnace and the gas in the first gas passage at the front end of the heating furnace.
Further, the present invention includes a compressor; the number of the compressors is 1 or more than 1, and the compressors are used for compressing and boosting the pressure of the gas in the pipeline.
A compressor is arranged at the outlet of the dust remover, and the gas after dust removal is compressed and then sent to a decarburization device; and a compressor is arranged at a second outlet of the decarburization device or at a proper position before the decarburization device enters a top exhaust port and a bottom discharge port of the reduction reaction furnace, so that the gas entering the sealing part is compressed for use.
Furthermore, the outlet of the hydrogen-rich synthesis gas source is communicated with the outlet of the dust remover and then is connected to the inlet of the decarburization device together, so that the reduction reaction furnace top tail gas subjected to dust removal and dehydration treatment and the gas in the hydrogen-rich synthesis gas source are mixed and then enter the decarburization device through the same pipeline. .
The purpose of designing the pipeline connection mode is to firstly consider the decarburization treatment aiming at the condition that carbon dioxide exists in the gas of the hydrogen-rich synthesis gas source, and also can design a gas pipeline which is communicated with the inlet of the decarburization device and is independently controlled so as to filter CO in the hydrogen-rich synthesis gas source before use2Namely: the hydrogen-rich synthesis gas source and the dust remover are connected with the decarburization device through respective independent connecting pipelines, or the hydrogen-rich synthesis gas source and the dust remover are combined and then sent into the decarburization device.
Compared with the prior art, the system of the invention has the following effects:
1) two-way conveying of raw material gas is designed: one path of the synthesis gas enters the reduction reaction furnace from the upper part for reduction reaction after being preheated and heated, the other path of the synthesis gas directly enters the reduction reaction furnace from the bottom of the reduction reaction furnace, the part of the synthesis gas directly exchanges heat with the sponge iron product, the temperature of the synthesis gas is raised, the temperature of the sponge iron product is lowered, the heat is fully recovered, and the energy consumption of the process is reduced.
2) The device for treating and recycling the top gas is designed, the top gas comprises reaction tail gas and unreacted raw gas, after dust removal and decarburization treatment, the unreacted raw gas is returned to the hydrogen-rich synthesis gas to be used as raw gas, carbon dioxide is continuously used for reducing the gas seal and industrial raw material of the reaction furnace, the top gas can be fully utilized and recycled, and the process is pollution-free.
The invention provides a process method for producing sponge iron by directly reducing hydrogen-rich synthesis gas, which uses a system for producing sponge iron by directly reducing the hydrogen-rich synthesis gas, and comprises the following steps:
s1, sending the gas raw material in the hydrogen-rich synthesis gas source out through two paths, wherein the first path enters the middle part of the reduction reaction furnace through the heating furnace and performs reduction reaction with iron ore to generate sponge iron; the second passage is directly fed into the reduction reaction furnace from the bottom of the reduction reaction furnace, and exchanges heat with the sponge iron product falling from the middle part of the reduction reaction furnace in the ascending process;
s2, firstly, heat exchanging and cooling the tail gas at the top of the reduction reaction furnace with the gas in the first passage of the hydrogen-rich synthesis gas source before heating through a heat exchanger, then removing dust and moisture through a dust remover, then removing carbon dioxide in a decarbonizing device to obtain a circulating synthesis gas, and sending the circulating synthesis gas into the exhaust passage of the hydrogen-rich synthesis gas source through the first outlet of the decarbonizing device to be used as a raw material for circulation;
s3, when the carbon dioxide removed by the decarbonization device reaches saturation, carrying out desorption treatment to obtain CO2The mixture is sent to a top feeding hole and a bottom discharging hole of the reduction reaction furnace through a second outlet of the decarburization device to be used as sealing gas;
wherein, the hydrogen-rich synthetic gas in the hydrogen-rich synthetic gas source is a byproduct mixed gas of a process for preparing acetylene from natural gas, and comprises H with a volume ratio of more than 2:12: the sum of the contents of the CO and the CO accounts for more than 85 percent of the total volume of the byproducts.
Further, in step S2, the tail gas at the top of the reduction reactor and the first path gas of the hydrogen-rich synthesis gas source before heating are subjected to heat exchange, cooled, and then heated in the heating furnace, and then enter the dust remover.
Further, when the hydrogen-rich syngas source contains carbon dioxide gas, the gas in the hydrogen-rich syngas source in step S1 enters the decarbonization device through the pipeline between the outlet of the hydrogen-rich syngas source and the inlet of the decarbonization device to remove CO2And then sent out through two paths.
Further, the reduction reaction temperature at the middle part of the reduction reaction furnace in the step S1 is 900-1050 ℃, and the reaction pressure is 0.2-0.6 MPa.
Further, in the step S2, the first path gas of the hydrogen-rich synthesis gas source and the reduction reaction furnace top tail gas heat exchange and then the temperature is raised to 100-; the temperature of the sponge iron product falling from the middle part of the reduction reaction furnace in the step S1 discharged from the discharge outlet at the bottom of the reduction reaction furnace by heat exchange is 180-220 ℃.
Further, the heating furnace heats the first channel gas of the hydrogen-rich synthesis gas source to 900-1050 ℃.
The decarbonization device in the system and the process comprises an absorption unit and a desorption unit, wherein the main component of the absorption unit is a carbon dioxide absorbent, and the carbon dioxide absorbent can be one or more of methanol, organic ammonium, ethanolamine, diethanolamine, triethanolamine and methylethanolamine; the carbon dioxide absorbing operation conditions of the carbon dioxide absorbent are as follows: the pressure is from normal pressure to 0.4 MPa; the temperature is between normal temperature and 40 ℃; the carbon dioxide absorbent enters a desorption unit for desorption after absorbing carbon dioxide to obtain carbon dioxide, one part of the carbon dioxide obtained by desorption enters a feeding part and a discharging part of a reduction reaction furnace from the upper part and the lower part to be used as sealing gas, and the other part of the carbon dioxide is used as downstream fine chemical raw materials.
And (3) cooling the tail gas at the top of the reduction reaction furnace, then feeding the tail gas into a dust remover for dust removal and drainage, and discharging the sewage with dust from the bottom of the dust remover.
The process takes the synthesis gas as a raw material, one part of the synthesis gas is preheated to 100-.
The tail gas obtained by the reaction is discharged in the form of reduction reaction furnace top tail gas, the tail gas exchanges heat with the raw material synthesis gas firstly to preheat the raw material synthesis gas, then the dust and the moisture are removed through a dust remover to obtain pure furnace top tail gas at about 40 ℃, the tail gas is compressed to reach the pressure required by a decarburization process, and then the tail gas enters a decarburization device to remove carbon dioxide to obtain circulating synthesis gas, and the circulating synthesis gas is recycled as a raw material.
When the raw synthesis gas contains a small amount of carbon dioxide, the raw synthesis gas needs to be sent into a decarbonization device for removing the carbon dioxide. When the content of carbon dioxide in the raw material synthesis gas is extremely low, the decarbonization is not needed, and the circulating synthesis gas is decarbonizedAfter carbon dioxide is removed, the mixed raw material is mixed with raw material synthesis gas to be used as a mixed raw material. CO obtained by a carbon dioxide removal system2The content of the gas reaches more than 99 percent, one part of carbon dioxide enters the feeding part and the discharging part of the reduction reaction furnace from the upper part and the lower part to be used as sealing gas, the reaction pressure in the reduction reaction furnace is ensured to be maintained at 0.2-0.6MPa, and one part of carbon dioxide is used as downstream fine chemical raw materials. The decarbonization apparatus includes an absorption unit and a desorption unit. The carbon dioxide absorbent can be methanol, organic ammonium, ethanolamine, diethanolamine, triethanolamine and methylethanolamine, and absorbs the carbon dioxide in the tail gas through physical and chemical absorption, wherein the absorption operation conditions are as follows: the pressure is from normal pressure to 0.4MPa, the absorption temperature does not exceed 40 ℃, then the carbon dioxide is recovered by desorption and desorption through pressure reduction and temperature rise, the absorbent is reused, and the process is green, environment-friendly and energy-saving.
The process of the invention has the following beneficial effects:
1) by utilizing the process, the tail gas at the top of the reduction reaction furnace exchanges heat with the raw material synthesis gas and the fuel gas of the heating furnace to preheat, the raw material synthesis gas and the fuel gas can reach 100-200 ℃ after preheating, the consumption of the fuel gas is reduced by 10-30%, a part of raw materials are introduced into the reduction reaction furnace from the bottom, not only can participate in the reduction reaction, but also can cool and cool the sponge iron product, fully recover heat, reduce the usage amount of a refrigerator required by the refrigeration of the product by 30-40%, achieve the effect of process energy saving, reduce investment and energy consumption, and save energy.
2) CO obtained by carbon dioxide removal device2The content of the gas reaches more than 99 percent, a part of carbon dioxide respectively enters the feeding part and the discharging part of the reduction reaction furnace from top to bottom to be used as sealing gas to ensure that the reaction pressure in the reduction reaction furnace is maintained at 0.2-0.6MPa, and a part of carbon dioxide is used as a downstream fine chemical raw material, so that the condition that the inert gas is introduced into the system to cause the accumulation of the inert gas in the system to influence the proceeding degree of the reduction reaction can be avoided, the carbon dioxide is used as the sealing gas to fully utilize the carbon dioxide of a system byproduct, the emission of the carbon dioxide is reduced, the obvious environmental protection effect is realized, the process costProviding process economics.
Drawings
These and/or other aspects and advantages of the present invention will become more apparent and more readily appreciated from the following detailed description of the embodiments of the invention, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a schematic diagram of the structural composition of a system and a process for producing sponge iron by direct reduction of hydrogen-rich syngas according to example 1 of the present invention;
fig. 2 is a schematic diagram of the structural composition of the system and the process for producing sponge iron by direct reduction of hydrogen-rich syngas in example 2 of the present invention.
Detailed Description
In order that those skilled in the art will better understand the present invention, the following detailed description of the invention is provided in conjunction with the accompanying drawings and the detailed description of the invention.
Example 1
A system for producing sponge iron by directly reducing hydrogen-rich synthesis gas is structurally shown in figure 1 and comprises: the system comprises a hydrogen-rich synthesis gas source, a heating furnace 2, a reduction reaction furnace 1, a heat exchanger 6, a dust remover 3, a decarbonization device 4, a first compressor 5 and a second compressor 7; two gas communication passages are arranged between the hydrogen-rich synthesis gas source and the reduction reaction furnace 1 and are used for sending gas in the hydrogen-rich synthesis gas source into the reduction reaction furnace 1 through a pipeline, wherein the first gas passage is communicated with the middle part of the reduction reaction furnace 1, and a heating furnace 2 is arranged on the gas passage; the second gas passage is communicated with the bottom of the reduction reaction furnace 1; the reduction reaction furnace 1 is a reactor for carrying out sealed reaction on iron ore and hydrogen-rich synthesis gas, and comprises a bottom discharge hole and a top exhaust port; the top exhaust port is connected with the inlet of the dust remover 3, and the outlet of the dust remover 3 is connected with the inlet of the decarburization device 4 through a first compressor 5; a first outlet of the decarbonization device 4 is connected to an outlet of a hydrogen-rich synthesis gas source, and a second outlet of the decarbonization device is respectively connected with a top exhaust port and a bottom discharge port of the reduction reaction furnace 1 after passing through a second compressor 7; the heat exchanger 6 is arranged on a cross passage of a first gas passage of the hydrogen-rich synthesis gas source and a furnace top tail gas passage of the reduction reaction furnace 1 and is used for exchanging heat between the furnace top tail gas of the reduction reaction furnace and the gas of the first gas passage at the front end of the heating furnace.
Example 2
A system for producing sponge iron by directly reducing hydrogen-rich synthesis gas is structurally shown in figure 2 and is different from the embodiment in that an outlet of a hydrogen-rich synthesis gas source is communicated with an outlet of a dust remover 3 and then enters an inlet of a decarburization device 4 through a first compressor 5, so that the reduction reaction furnace top tail gas subjected to dust removal and dehydration treatment is mixed with the gas in the hydrogen-rich synthesis gas source, compressed and then sent to the decarburization device 4 for decarburization.
Example 3
A process for preparing sponge iron by direct reduction of hydrogen-rich synthetic gas features that the hydrogen-rich synthetic gas source as by-product of preparing acetylene from natural gas is composed of H2: CO volume ratio of 3:1, H2With a CO content of 88% of the total2The content is very low and is lower than 1%, so the system and the process schematic diagram for producing sponge iron by directly reducing hydrogen-rich synthesis gas shown in figure 1 are used and referred, the synthesis gas is used as a raw material, the pressure is increased to 0.4MPa after compression, the synthesis gas is divided into two paths, the first path is heated to 950 ℃ by a heating furnace 2, enters a reduction reaction furnace 1 to perform reduction reaction with iron ore raw materials added from the top of the reaction furnace to generate a sponge iron product with the metallization rate of more than or equal to 92%, the second path enters the reduction reaction furnace 1 from the bottom, the sponge iron is cooled to about 200 ℃ through heat exchange with the generated sponge iron product and then is discharged out of the reaction furnace, and the second path of synthesis gas enters the reduction reaction furnace after being heated to continue to perform reduction reaction with the iron ore raw materials or is discharged from the top; the tail gas generated by the reaction in the reduction furnace is discharged in the form of reduction reaction furnace top tail gas, the tail gas exchanges heat with the first path of raw material synthesis gas to preheat the raw material synthesis gas, so that the synthesis gas is preheated to 180 ℃, the heat consumed by a subsequent heating furnace can be obviously reduced, then, the dust and the moisture are removed by a dust remover 3 to obtain pure furnace top tail gas at about 40 ℃, and the circulating synthesis gas (CO + H) is obtained after the furnace top tail gas is dedusted and drained2Volume content 95%) is compressed by a first compressor 5 to reach the pressure required by the decarburization process, and then enters a decarburization device 4 to remove carbon dioxide to obtain the recycle synthesis gas which is recycled as the raw material and used together with the raw material synthesis gasMixing the above raw materials, and using. CO obtained by a carbon dioxide removal system2The content of the gas reaches 99 percent, a part of carbon dioxide is pressurized to be more than 0.4MPa through a second compressor 7, enters the feeding part and the discharging part of the reduction reaction furnace 1 from the upper part and the lower part and is used as sealing gas, the reaction pressure in the reduction reaction furnace is ensured to be maintained at 0.2-0.6MPa, and a part of carbon dioxide is used as downstream fine chemical raw materials. The decarbonization device 4 adopts ethanolamine to absorb carbon dioxide, and the absorption operating conditions are as follows: the pressure is 0.2MPa, the absorption temperature is normal temperature, then the carbon dioxide is recovered by desorbing and removing through normal pressure temperature rise, the absorbent is reused, and the process is environment-friendly and energy-saving.
Example 4
A process for preparing spongy iron by direct reduction of hydrogen-enriched synthetic gas features that the synthetic gas as by-product of preparing acetylene from natural gas is H2: CO volume ratio of 2:1, H2And a CO content of 85%, wherein CO2The content is 2%, so the system and the process schematic diagram for producing sponge iron by directly reducing hydrogen-rich synthesis gas shown in fig. 2 are used and referred, the synthesis gas is used as a raw material, the synthesis gas is compressed by a first compressor 5 and then enters a decarburization device 4 for decarburization, then one path of the synthesis gas enters a heating furnace 2 for heating to 950 ℃, enters a reduction reaction furnace 1 for reduction reaction with iron ore raw material added from the top of the reaction furnace to generate sponge iron product with metallization rate more than or equal to 92%, the other path of the synthesis gas enters the reduction reaction furnace 1 from the bottom, the sponge iron is cooled to about 200 ℃ by heat exchange with the generated sponge iron product and then discharged out of the reaction furnace, and the synthesis gas enters the reduction reaction furnace after being heated to continue reduction reaction with the iron ore raw material.
The tail gas obtained by the reduction reaction is discharged in the form of the reduction reaction furnace top tail gas, the tail gas exchanges heat with the first path of raw material synthesis gas to preheat the raw material synthesis gas, the temperature of the tail gas is reduced, and then the tail gas is dedusted by a deduster 3 to remove dust and moisture to obtain the circulating synthesis gas (CO + H)295% by volume), mixing the recycle synthesis gas with raw synthesis gas continuously discharged from a hydrogen-rich synthesis gas source to obtain CO + H2The synthesis gas with the content of about 90 percent is compressed by a first compressor 5 and then has pressureIncreased to 0.4MPa, and then sent to the decarburization device 4 for decarburization.
CO obtained by a carbon dioxide removal system2The content of the gas reaches 99 percent, a part of carbon dioxide is pressurized to be more than 0.4MPa by a compressor and enters the feeding part and the discharging part of the reduction reaction furnace 1 from the upper part and the lower part to be used as sealing gas, so that the reaction pressure in the reduction reaction furnace is ensured to be maintained at 0.2-
0.6MPa, and a part of carbon dioxide is used as a downstream fine chemical raw material.
The decarbonizing device 4 adopts triethanolamine to absorb carbon dioxide, and the absorption operating conditions are as follows: the pressure is 0.2MPa, the absorption temperature is normal temperature, then the carbon dioxide is recovered by desorbing and removing through normal pressure temperature rise, the absorbent is reused, and the process is environment-friendly and energy-saving.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (10)
1. A system for producing sponge iron by directly reducing hydrogen-rich synthesis gas is characterized by comprising: a hydrogen-rich synthesis gas source, a heating furnace (2), a reduction reaction furnace (1), a heat exchanger (6), a dust remover (3) and a decarburization device (4);
two gas communication passages are arranged between the hydrogen-rich synthesis gas source and the reduction reaction furnace (1) and are used for sending gas in the hydrogen-rich synthesis gas source into the reduction reaction furnace (1) through a pipeline, wherein a first gas passage is communicated with the middle part of the reduction reaction furnace (1), a heating furnace (2) is arranged on the gas passage, and the first gas passage at the front end of the heating furnace (2) passes through the inside of a heat exchanger (6); the second gas passage is communicated with the bottom of the reduction reaction furnace (1);
the reduction reaction furnace (1) is a reactor for carrying out sealed reaction on iron ore and hydrogen-rich synthesis gas, and comprises a bottom discharge hole and a top exhaust port; the top exhaust port is connected with an inlet of the dust remover (3), and a connecting passage passes through the inside of the heat exchanger (6); the outlet of the dust remover (3) is connected with the inlet of the decarburization device (4); the top exhaust port is connected with an inlet at one side of the heat medium of the heat exchanger (6);
a first outlet of the decarburization device (4) is connected to an outlet of a hydrogen-rich synthesis gas source, and a second outlet is respectively connected with a top exhaust port and a bottom discharge port of the reduction reaction furnace (1);
the heat exchanger (6) is used for heat exchange between the tail gas at the top of the reduction reaction furnace and the gas in the first gas passage at the front end of the heating furnace.
2. The system for producing sponge iron by direct reduction of hydrogen-rich syngas according to claim 1, further comprising a compressor; the number of the compressors is 1 or more than 1, and the compressors are used for compressing and boosting the pressure of the gas in the pipeline.
3. System for producing sponge iron by direct reduction of hydrogen-rich synthesis gas according to claim 1, characterized in that an independently controlled gas line is connected between the inlet of the decarbonization device (4) and the outlet of the hydrogen-rich synthesis gas source for filtering CO from the hydrogen-rich synthesis gas source2。
4. The system for producing sponge iron by directly reducing hydrogen-rich synthesis gas as claimed in claim 1, wherein the outlet of the hydrogen-rich synthesis gas source and the outlet of the dust remover (3) are connected to the inlet of the decarburization device (4) together, so that the reduction reactor top tail gas after dust removal and dehydration treatment is mixed with the gas in the hydrogen-rich synthesis gas source and then enters the decarburization device (4) through the same pipeline.
5. A process for producing sponge iron by directly reducing hydrogen-rich synthesis gas, which is characterized in that the system for producing sponge iron by directly reducing hydrogen-rich synthesis gas as described in claims 1-4 is used, and comprises the following steps:
s1, sending the gas raw material in the hydrogen-rich synthesis gas source out through two paths, wherein the first path enters the middle part of the reduction reaction furnace (1) through the heating furnace (2) and performs reduction reaction with iron ore to generate sponge iron; the second path is directly fed into the reduction reaction furnace from the bottom of the reduction reaction furnace (1) and exchanges heat with the sponge iron product falling from the middle part of the reduction reaction furnace in the rising process;
s2, the tail gas at the top of the reduction reaction furnace is subjected to heat exchange with the gas in the first passage of the hydrogen-rich synthesis gas source before heating through a heat exchanger (6) to reduce the temperature, then the dust and the moisture are removed through a dust remover (3), then the tail gas enters a decarburization device (4) to remove carbon dioxide, then the circulating synthesis gas is obtained, and the circulating synthesis gas is sent to the exhaust passage of the hydrogen-rich synthesis gas source through the first outlet of the decarburization device (4) to be recycled as the raw material;
s3, when the carbon dioxide removed by the decarbonization device reaches saturation, carrying out desorption treatment to obtain CO2The mixture is sent to a top feeding hole and a bottom discharging hole of the reduction reaction furnace through a second outlet of the decarburization device to be used as sealing gas;
wherein the hydrogen-rich synthetic gas in the hydrogen-rich synthetic gas source is a byproduct mixed gas of a process for preparing acetylene from natural gas, and the hydrogen-rich synthetic gas comprises H with a volume ratio of more than 2:12: the sum of the contents of the CO and the CO accounts for more than 85 percent of the total volume of the byproducts.
6. The process of producing sponge iron by direct reduction of hydrogen-rich syngas according to claim 5, wherein in step S2, the tail gas from the top of the reduction reactor and the first path gas of the hydrogen-rich syngas source before heating are cooled by heat exchange, and then enter the heating furnace and then enter the dust remover.
7. The process for producing sponge iron by direct reduction of hydrogen-rich syngas according to claim 5, wherein when the hydrogen-rich syngas contains carbon dioxide gas, the gas in the hydrogen-rich syngas of step S1 enters the decarbonization device through the pipeline between the outlet of the hydrogen-rich syngas and the inlet of the decarbonization device (4) to remove CO2And then sent out through two paths.
8. The process for producing sponge iron by direct reduction of hydrogen-rich syngas as claimed in claim 5, wherein the reduction reaction temperature in the middle of the reduction reaction furnace (1) in step S1 is 900-.
9. The process of claim 5, wherein the temperature of the first path gas of the hydrogen-rich syngas source in step S2 is raised to 100-200 ℃ after heat exchange with the top tail gas of the reduction reaction; and in the step S1, the sponge iron product falling from the middle part of the reduction reaction furnace is discharged from a discharge outlet at the bottom of the reduction reaction furnace (1) after heat exchange, and the temperature of the discharged sponge iron product is 180-220 ℃.
10. The process for producing sponge iron by direct reduction of hydrogen-rich synthesis gas according to claim 5, wherein the heating furnace (2) heats the first path gas of the hydrogen-rich synthesis gas source to 900 ℃ -1050 ℃.
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| CN113403441A (en) * | 2021-06-17 | 2021-09-17 | 北京金博威科技有限公司 | Production method, production system and application of granular direct reduced iron |
| CN113582214A (en) * | 2021-09-06 | 2021-11-02 | 上海源晗能源技术有限公司 | Green low-carbon closed-loop metallurgy and carbon dioxide capture and utilization process |
| SE2150290A1 (en) * | 2021-03-12 | 2022-09-13 | Greeniron H2 Ab | Method and system for producing direct reduced metal |
| CN116536468A (en) * | 2023-05-22 | 2023-08-04 | 河钢集团有限公司 | Production process for directly reducing iron ore |
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| CN116536468B (en) * | 2023-05-22 | 2024-04-23 | 河钢集团有限公司 | Production process for directly reducing iron ore |
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