CN213772103U - System for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide - Google Patents
System for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide Download PDFInfo
- Publication number
- CN213772103U CN213772103U CN202022850747.XU CN202022850747U CN213772103U CN 213772103 U CN213772103 U CN 213772103U CN 202022850747 U CN202022850747 U CN 202022850747U CN 213772103 U CN213772103 U CN 213772103U
- Authority
- CN
- China
- Prior art keywords
- gas
- shaft furnace
- reducing gas
- reducing
- mea
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- 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
Abstract
The utility model relates to a system of coke oven gas coupling carbon dioxide preparation shaft furnace reduction gas, including adsorbing refined tower, reduction gas reformer and MEA desulphurization unit, the raw gas outlet of adsorbing refined tower and the raw material gas access connection of reduction gas reformer, the desorption gas outlet of adsorbing refined tower and the fuel gas access connection of reduction gas reformer, the reduction gas outlet of reduction gas reformer and the reduction gas access connection of shaft furnace, the top gas outlet of shaft furnace and MEA desulphurization unit's top gas access connection, MEA desulphurization unit's process gas outlet respectively with the fuel gas inlet of reduction gas reformer, the raw material gas inlet of reduction gas reformer and the desorption gas access connection of adsorption refined tower, MEA desulphurization unit's regeneration gas outlet passes through the raw material gas access connection of carbon dioxide separator and reduction gas reformer. The utility model solves the technical problem that coke oven gas can not be further processed in the prior art so as to provide the reducing gas for the gas-based shaft furnace.
Description
Technical Field
The utility model relates to a ferrous metallurgy technical field especially relates to a system of coke oven gas coupling carbon dioxide preparation shaft furnace reducing gas.
Background
The steel production has two long and short processes, wherein the long process is the combination of blast furnace iron making and converter steel making, and the short process is the combination of direct reduced iron and electric furnace steel making. The traditional blast furnace iron making has the characteristics of long flow, high energy consumption, heavy pollution, coke consumption and the like, and although various energy-saving and emission-reducing measures have certain effects, the method is based on carbonThe metallurgical thermodynamic reaction involved in the long process of reduction tends to the limit level, and the CO emission reduction is continued2Has very limited potential, so a new breakthrough process for solving the CO in the steel industry must be found2High emission problem, and CO discharged by per ton steel produced by short process2Much lower than the long run.
At present, the social and economic structure of China cannot provide enough scrap steel as a raw material of a short process, and iron ore needs to be adopted to replace the scrap steel as the raw material. Direct Reduction Iron (sponge Iron) in a short process is also called as sponge Iron, has stable components and low content of harmful impurity elements, is a high-quality raw material for steelmaking, can be used as a raw material for electric furnace steelmaking and a coolant for converter steelmaking to supplement the deficiency of steel scrap resources, and plays an irreplaceable role in ensuring the quality of steel and producing high-quality pure steel. The world advanced direct reduced iron technology is a gas-based shaft furnace direct reduction technology which mainly takes natural gas as raw material and is rich in CH4And CO2Is reacted to become H-rich2And after the CO gas is mixed, the reaction product is directly subjected to reduction reaction with iron ore under the high-temperature condition to produce sponge iron. Because natural gas resources in China are deficient, the development of the gas-based shaft furnace reduction technology is limited. The coke oven gas resources in China are relatively rich, and the hydrogen-rich gas is prepared by using the coke oven gas, so that the problems of gas emission and utilization are solved, and a method for obtaining the hydrogen-rich reducing gas is provided for producing the direct reduced iron at the present stage. The method for preparing the reducing gas by adopting the coke oven gas is a preferred technical route which accords with the national conditions of China and is an important direction for developing a novel iron-making technology in China.
With the development of the technology, the requirements of the gas-based shaft furnace on reducing gas are more extensive, and the requirements are further met
Greater than 10 (wherein,
as a volume fraction),
more than 0.3 and the pressure is 0.1-0.90 MPa. Compared with natural gas, the coke oven gas resource in China is relatively rich, but the subsequent utilization process is not matched, so that a large amount of coke oven gas is wasted. Coke oven gas containing H2S、CS2、COS、NH3And impurities such as BTX (benzene, toluene, xylene, etc.), tar, naphthalene, etc., which cause the conventional gas-based shaft furnace process using natural gas as a gas source to be incapable of running, and a gas-based shaft furnace reducing gas process suitable for coke oven gas needs to be developed.
In order to solve the problem that coke oven gas cannot be further processed in the related art so as to provide reduction gas for a shaft furnace, an effective solution is not provided at present.
Therefore, the inventor provides a system for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide by virtue of experience and practice of related industries for many years, so as to overcome the defects in the prior art.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a system of coke oven gas coupling carbon dioxide preparation shaft furnace reduction gas can adsorb the desorption to the impurity in the coke oven gas, and desorption gas after the regeneration can be delivered to the reduction gas reborner and burn the heat supply, and MEA desulphurization unit can carry out desulfurization treatment to the top of a furnace gas to with absorbent CO2Introducing the regenerated coke oven gas and the purified top gas into a reducing gas converter to be catalytically converted into reducing gas used by the shaft furnace, and adding CO2Can make the catalytic reaction more sufficient, effectively solves the problems of more impurities and difficult purification in the coke oven gas, has the advantage of adjustable raw material gas components of the reducing gas converter, and achieves the purposes of saving energy and reducing emission of CO2The method is beneficial to reasonable configuration of resources and protection of the environment.
The purpose of the utility model can be realized by adopting the following technical scheme:
the utility model provides a system for coke oven gas coupling carbon dioxide preparation shaft furnace is gaseous with original reduction, including carrying out purification treatment's absorption refining tower, turning into the coke oven gas after purifying the reduction gas reborner of the gaseous with original reduction and carrying out purification treatment's MEA desulphurization unit to shaft furnace exhaust top gas, wherein:
the coke oven gas inlet of the adsorption refining tower is connected with a coke oven gas pipeline, the raw gas outlet of the adsorption refining tower is connected with the raw gas inlet of the reducing gas converter, the desorption gas outlet of the adsorption refining tower is connected with the fuel gas inlet of the reducing gas converter, the reducing gas outlet of the reducing gas converter is connected with the reducing gas inlet of the shaft furnace, the top gas outlet of the shaft furnace is connected with the top gas inlet of the MEA desulfurization device, the process gas outlet of the MEA desulfurization device is respectively connected with the fuel gas inlet of the reducing gas converter, the raw gas inlet of the reducing gas converter and the desorption gas inlet of the adsorption refining tower, and the regeneration gas outlet of the MEA desulfurization device is connected with the raw gas inlet of the reducing gas converter through a carbon dioxide separation device.
In a preferred embodiment of the present invention, the fuel gas inlet of the reducing gas reformer is connected to the coke oven gas pipeline.
In a preferred embodiment of the present invention, the adsorption purification tower is filled with a molecular sieve material which can adsorb impurities contained in the coke oven gas and can be desorbed and regenerated after being heated.
In a preferred embodiment of the present invention, the number of the adsorption purification towers is plural, and at least one of the adsorption purification towers is a spare adsorption purification tower.
The utility model discloses an in a preferred embodiment, coke oven gas coupling carbon dioxide preparation shaft furnace reduction gas's system still includes to MEA desulphurization unit exhaust process gas and the heat recovery unit that intensification was preheated to absorption refining tower exhaust raw gas, MEA desulphurization unit's process gas export is passed through heat recovery unit respectively with the fuel gas entry of reduction gas reformer the raw gas entry of reduction gas reformer and the desorption gas access connection of absorption refining tower, the raw gas export of absorption refining tower passes through heat recovery unit with the raw gas access connection of reduction gas reformer.
In a preferred embodiment of the present invention, the flue gas outlet of the reducing gas reformer is connected to the flue gas inlet of the heat recovery device, and the flue gas outlet of the heat recovery device is directly connected to the outside.
In a preferred embodiment of the present invention, the regeneration gas outlet of the MEA desulfurization apparatus is connected to the raw gas inlet of the reducing gas reformer sequentially through the carbon dioxide separation apparatus and the heat recovery apparatus.
The utility model discloses a in a preferred embodiment, coke oven gas coupling carbon dioxide preparation shaft furnace is system of reducing gas still includes heat transfer device and scrubber, heat transfer device include the heat exchanger and with the steam pocket that the heat exchanger is connected, the air inlet of heat exchanger with the top gas outlet of shaft furnace is connected, the gas outlet of heat exchanger with the air inlet of scrubber is connected, the gas outlet of scrubber with MEA desulphurization unit's top gas access connection, the hot steam outlet of steam pocket with MEA desulphurization unit's heat source access connection.
In a preferred embodiment of the present invention, the MEA desulfurization apparatus includes at least one reaction tower and at least one regeneration tower connected to the reaction tower, the reaction tower is filled with an MEA solution capable of adsorbing carbon dioxide and hydrogen sulfide, an air inlet of the reaction tower is connected to an air outlet of the scrubber, an air outlet of the reaction tower is connected to a fuel gas inlet of the reducing gas reformer, a raw material gas inlet of the reducing gas reformer, and a desorption gas inlet of the adsorption refining tower, respectively, and an air inlet of the regeneration tower is connected to a hot steam outlet of the steam drum;
the gas inlet of the reaction tower is a furnace top gas inlet of the MEA desulfurization device, the gas outlet of the reaction tower is a process gas outlet of the MEA desulfurization device, and the gas inlet of the regeneration tower is a heat source inlet of the MEA desulfurization device.
In a preferred embodiment of the present invention, the carbon dioxide separation device is provided with a combustion device inside or the tail gas outlet of the carbon dioxide separation device is connected to the incinerator.
In a preferred embodiment of the present invention, a pressurizing device for adjusting the gas transmission pressure is provided between the process gas outlet of the MEA desulfurization device and the raw gas inlet of the reducing gas reformer.
In a preferred embodiment of the present invention, the inside of the reducing gas reformer is provided with a plurality of catalyst tubes for catalytically reforming the raw gas discharged from the adsorption refining tower, the process gas discharged from the MEA desulfurization device, and the regenerated gas discharged from the MEA desulfurization device into the reducing gas required for reducing iron ore, each of the catalyst tubes being connected in parallel between the raw gas inlet of the reducing gas reformer and the reducing gas outlet of the reducing gas reformer.
In a preferred embodiment of the present invention, the catalyst tube is filled with a nickel-based catalyst.
In a preferred embodiment of the present invention, the top gas outlet is disposed at the top of the shaft furnace, and an iron ore inlet is disposed at the top of the shaft furnace and above the top gas outlet;
the reducing gas inlet is arranged at the bottom of the shaft furnace, and a sponge iron outlet is arranged at the bottom of the shaft furnace and below the reducing gas inlet.
From the above, the utility model discloses a system for coke oven gas coupling carbon dioxide preparation shaft furnace is the gas that reduces of characteristics and advantage are: the coke oven gas is purified by the adsorption refining tower to achieve the effect of adsorbing and removing impurities such as inorganic sulfur, organic sulfur, tar, benzene, naphthalene and the like in the coke oven gas, the desorbed gas regenerated by the adsorption refining tower can be sent to a reducing gas converter for combustion and heat supply, the MEA desulfurization device can perform desulfurization treatment on the oven top gas and absorb CO2Introducing the regenerated coke oven gas and the purified top gas into a reducing gas converter to be catalytically converted into rich H for the shaft furnace2And CO reducing gasCO added2Can make catalytic reaction more abundant complete to produce sufficient reducing gas and take place reduction reaction with the iron ore in the shaft furnace, solved many, the difficult problem of purification of impurity in the coke oven gas, the utility model discloses not only have the feed gas component adjustable advantage of reducing gas reformer, reach energy-conservation and emission reduction CO moreover2The method has the advantages of being beneficial to reasonable allocation of resources and protection of the environment, upgrading and transformation of a steel mill and improvement of product quality, and having great development prospect.
Drawings
The drawings are only intended to illustrate and explain the present invention and do not limit the scope of the invention. Wherein:
FIG. 1: is a schematic structural diagram of a system for preparing shaft furnace reducing gas by coupling coke oven gas and carbon dioxide.
FIG. 2: is a structural schematic diagram of a reducing gas converter in a system for preparing the reducing gas of the shaft furnace by coupling coke oven gas and carbon dioxide.
FIG. 3: is a structural schematic diagram of a heat exchange device in a system for preparing shaft furnace reducing gas by coupling coke oven gas and carbon dioxide.
FIG. 4: is one of the process flow charts of the preparation method adopted by the system for preparing the shaft furnace reducing gas by coupling the coke oven gas and the carbon dioxide.
FIG. 5: the second technical flow chart of the preparation method adopted by the system for preparing the shaft furnace reducing gas by coupling the coke oven gas and the carbon dioxide.
FIG. 6: the third process flow chart of the preparation method adopted by the system for preparing the shaft furnace reducing gas by coupling the coke oven gas and the carbon dioxide is shown.
The utility model provides an reference numeral does:
1. an adsorption refining tower; 2. A reducing gas reformer;
201. a raw material gas inlet; 202. A reducing gas outlet;
203. a fuel gas inlet; 204. A flue gas outlet;
205. a catalyst tube; 3. A heat exchanger;
4. a steam drum; 401. A hot steam outlet;
5. a scrubber; 6. An MEA desulfurization device;
7. a carbon dioxide separation unit; 8. A heat recovery device;
9. a pressurizing device; 10. A shaft furnace;
1001. a top gas outlet; 1002. A reducing gas inlet;
1003. an iron ore inlet; 1004. A sponge iron outlet;
11. a first gas transmission pipeline; 12. A second gas transmission pipeline;
13. a third gas transmission pipeline; 14. A fourth gas transmission pipeline;
15. a fifth gas transmission pipeline; 16. A sixth gas transmission pipeline;
17. a seventh gas transmission pipeline; 18. An eighth gas transmission pipeline;
19. a ninth gas transmission pipeline; 20. A tenth gas transmission pipeline;
21. an eleventh gas transmission pipeline; 22. A twelfth gas transmission pipeline;
23. a thirteenth gas transmission pipeline; 24. A fourteenth gas transmission pipeline;
25. and a heat exchange device.
Detailed Description
In order to clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will be described with reference to the accompanying drawings.
Implementation mode one
As shown in fig. 1 to 3, the utility model provides a system for preparing shaft furnace reducing gas by coke oven gas coupling carbon dioxide, this system for preparing shaft furnace reducing gas by coke oven gas coupling carbon dioxide includes absorption refining tower 1, reducing gas reformer 2 and MEA desulphurization unit 6, absorption refining tower 1 is used for carrying out purification treatment to coke oven gas, reducing gas reformer 2 is used for turning into reducing gas with the coke oven gas after purifying, MEA desulphurization unit 6 is used for carrying out adsorption treatment to carbon dioxide and hydrogen sulfide in the top gas of shaft furnace 10 exhaust. Wherein: the coke oven gas inlet of the adsorption refining tower 1 is connected with the coke oven gas pipeline, the fuel gas inlet 203 of the reducing gas reforming furnace 2 is connected with the coke oven gas pipeline through a first gas transmission pipeline 11, the raw gas outlet of the adsorption refining tower 1 is connected with the raw gas inlet 201 of the reducing gas reforming furnace 2, the desorption gas outlet of the adsorption refining tower 1 is connected with the fuel gas inlet 203 of the reducing gas reforming furnace 2, the reducing gas outlet 202 of the reducing gas reforming furnace 2 is connected with the reducing gas inlet 1002 of the shaft furnace 10 through a fifth gas transmission pipeline 15, the top gas outlet 1001 of the shaft furnace 10 is connected with the top gas inlet of the MEA desulfurization device 6, the process gas outlet of the MEA desulfurization device 6 is respectively connected with the fuel gas inlet 203 of the reducing gas reforming furnace 2, the raw gas inlet 201 of the reducing gas reforming furnace 2 and the desorption gas inlet of the adsorption refining tower 1, the regeneration gas outlet of the MEA desulfurization device 6 is connected with the gas inlet of the carbon dioxide separation device 7 through a thirteenth gas transmission pipeline 23, the gas outlet of the carbon dioxide separation device 7 is connected to the raw gas inlet 201 of the reducing gas converter 2 through a fourteenth gas transmission pipeline 24.
The utility model discloses an it carries out purification treatment to adsorb refined tower 1 coke oven gas, reaches the effect that inorganic sulphur, organic sulphur, tar, benzene and impurity such as naphthalene adsorbed the desorption in the coke oven gas, adsorbs the desorption gas after 1 regeneration of refined tower and can send to reduction gas reborner 2 and burn the heat supply, MEA desulphurization unit 6 can carry out desulfurization treatment to the top of a furnace gas to with absorptive CO2Introducing the regenerated coke oven gas and the purified top gas into a reducing gas converter 2 for catalytic conversion into rich H for a shaft furnace 102And a reducing gas of CO, the CO added2Can make catalytic reaction more abundant complete to produce sufficient reducing gas and take place the reduction reaction with the iron ore in the shaft furnace 10, solved many, the difficult problem of purification of impurity in the coke oven gas, the utility model discloses not only have the feed gas component adjustable advantage of reducing gas reformer, reach energy-conservation and emission reduction CO moreover2The method is beneficial to reasonable configuration of resources and protection of the environment.
Specifically, as shown in fig. 1, a top gas outlet 1001 is provided at the top of the shaft furnace 10, and an iron ore inlet 1003 is provided at the top of the shaft furnace 10 above the top gas outlet 1001; a reducing gas inlet 1002 is provided at the bottom of the shaft furnace 10, and a sponge iron outlet 1004 is provided at the bottom of the shaft furnace 10 below the reducing gas inlet 1002.
Further, the pressure of the reducing gas in the fifth gas transmission pipeline 15 is 0.08MPa to 0.4MPa, the temperature of the reducing gas is 850 ℃ to 1100 ℃, and the reducing gas is in the reducing gas
Greater than 10 in reducing gas
Is greater than 0.3 of the total weight of the rubber,
preferably, in a reducing gas
Is 1 to 3.
In an optional embodiment of the present invention, the adsorption purification tower 1 is filled with a molecular sieve material that can adsorb impurities (inorganic sulfur, organic sulfur, tar, benzene, naphthalene, etc.) contained in the coke oven gas and can be desorbed and regenerated after being heated.
Preferably, the molecular sieve material is a hydrophobic microcrystalline material, can adsorb impurities such as inorganic sulfur, organic sulfur, tar, benzene, naphthalene and the like, has adsorption capacity within the temperature range of 20-100 ℃, and can perform desorption regeneration within the temperature range of 160-350 ℃; the molecular sieve material has a service life of 5-7 years, can be repeatedly regenerated, and is high-temperature resistant.
Furthermore, the hydrophobic microcrystalline material can be made of a material containing at least one element of magnesium, calcium, strontium, yttrium, lanthanum, cerium, europium, iron, cobalt, nickel, copper, silver, zinc and the like; specifically, the hydrophobic microcrystalline material is selected from at least one of an X-type molecular sieve, a Y-type molecular sieve, an a-type molecular sieve, a ZSM-type molecular sieve, mordenite, a beta-type molecular sieve, an MCM-type molecular sieve, and a SAPO-type molecular sieve, and in actual implementation, a person skilled in the art can reasonably set the amount of the catalyst according to the needs of field operation.
Further, the number of the adsorption purification columns 1 is plural, and at least one of the adsorption purification columns 1 is a spare adsorption purification column.
In an optional embodiment of the utility model, as shown in fig. 1, the system for preparing shaft furnace reducing gas by coke oven gas coupling carbon dioxide further comprises a heat recovery device 8, the heat recovery device 8 is used for preheating the process gas exhausted by the MEA desulfurization device 6 and the raw material gas exhausted by the adsorption refining tower 1, the process gas outlet of the MEA desulfurization device 6 is respectively connected with the fuel gas inlet 203 of the reducing gas reformer 2, the raw material gas inlet 201 of the reducing gas reformer 2 and the desorption gas inlet of the adsorption refining tower 1 through the heat recovery device 8, and the raw material gas outlet of the adsorption refining tower 1 is connected with the raw material gas inlet 201 of the reducing gas reformer 2 through the heat recovery device 8. The process gas and the feed gas before entering the reducing gas reformer 2 are preheated by the heat recovery device 8.
Further, as shown in fig. 1, the flue gas outlet of the reducing gas reformer 2 is connected to the flue gas inlet of the heat recovery device 8 through a sixth gas transmission pipeline 16, and the flue gas outlet of the heat recovery device 8 is directly communicated with the outside.
Further, as shown in fig. 1, the regeneration gas outlet of the MEA desulfurization device 6 passes through the carbon dioxide separation device 7, and then is connected to the raw material gas inlet 201 of the reducing gas reformer 2 via the heat recovery device 8, and CO in the regeneration gas discharged from the MEA desulfurization device 6 is recovered by the heat recovery device 82Preheating and raising the temperature.
In an alternative embodiment of the present invention, as shown in fig. 1, a pressurizing device 9 for adjusting the gas transmission pressure is disposed between the process gas outlet of the MEA desulfurization device 6 and the raw gas inlet 201 of the reducing gas reformer 2, and the gas transmission pressure is adjusted by the pressurizing device 9, so as to pressurize the process gas and the raw gas and then deliver the process gas and the raw gas to the raw gas inlet 201 of the reducing gas reformer 2.
Further, the pressing device 9 may be, but is not limited to, a press.
In an alternative embodiment of the present invention, as shown in fig. 1 and 3The system for preparing the shaft furnace reducing gas by coupling the coke oven gas with the carbon dioxide also comprises a heat exchange device 25 and a scrubber 5, wherein the heat exchange device 25 comprises a heat exchanger 3 and a steam drum 4 connected with the heat exchanger 3, a gas inlet of the heat exchanger 3 is connected with a top gas outlet 1001 of the shaft furnace 10 through a ninth gas transmission pipeline 19, a gas outlet of the heat exchanger 3 is connected with a gas inlet of the scrubber 5 through a tenth gas transmission pipeline 20, a gas outlet of the scrubber 5 is connected with a top gas inlet of an MEA desulfurization device 6 through an eleventh gas transmission pipeline 21, a hot steam outlet 401 of the steam drum 4 is connected with a heat source inlet of the MEA desulfurization device 6 through a twelfth gas transmission pipeline 22, a process gas outlet of the MEA desulfurization device 6 is connected with a fuel gas inlet 203 of the reducing gas reforming furnace 2 through an eighth gas transmission pipeline 18, a process gas outlet of the MEA desulfurization device 6 is also connected with a raw material gas inlet 201 of the reducing gas reforming furnace 2 through a seventh gas transmission pipeline 17, the seventh gas transmission pipeline 17 and the eighth gas transmission pipeline 18 both penetrate through the heat recovery device 8, and the pressurizing device 9 is arranged on the seventh gas transmission pipeline 17. The heat exchange is carried out on the furnace top gas through the heat exchanger 3, the hot steam obtained by the heat exchange is conveyed to the MEA desulfurization device 6 through the steam drum 4 for the regeneration of MEA solution, the dedusted and cooled furnace top gas after the heat exchange is carried out through the scrubber 5, and the furnace top gas is conveyed to the MEA desulfurization device 6 for H in the furnace top gas2S and CO2Absorbing and removing, wherein the top gas purified by the MEA desulfurization device 6 is the process gas.
Specifically, the MEA desulfurization device 6 includes at least one reaction tower and at least one regeneration tower connected to the reaction tower, the reaction tower is filled with MEA (monoethanolamine) solution capable of adsorbing carbon dioxide and hydrogen sulfide, the gas inlet of the reaction tower is connected to the gas outlet of the scrubber 5, the gas outlet of the reaction tower is connected to the fuel gas inlet 203 of the reducing gas reformer 2, the raw gas inlet 201 of the reducing gas reformer 2 and the desorbed gas inlet of the adsorption refining tower 1, respectively, and the gas inlet of the regeneration tower is connected to the hot steam outlet 401 of the steam drum 4; wherein, the air inlet of the reaction tower is the furnace top gas inlet of the MEA desulfurization device 6, the air outlet of the reaction tower is the process gas outlet of the MEA desulfurization device 6, and the air inlet of the regeneration tower is the heat source inlet of the MEA desulfurization device 6. The top gas after being dedusted and cooled by the scrubber 5 is firstly conveyed into the reaction tower to be treated with H2S toAnd CO2Absorbing and removing, feeding the MEA solution in the reaction tower into a regeneration tower after the MEA solution reaches a preset saturation threshold, and absorbing H in the MEA solution under the heating of high-temperature steam in the regeneration tower2S and CO2And releasing the regenerated gas into the regenerated gas, conveying the regenerated gas into a carbon dioxide separation device 7, and refluxing the regenerated MEA solution into the reaction tower for recycling.
Wherein the operating pressure of the reaction tower is 5kPa to 0.1MPa, and the operating pressure of the regeneration tower is 5kPa to 60 kPa.
Furthermore, a combustion device is arranged in the carbon dioxide separation device 7 or a tail gas outlet of the carbon dioxide separation device 7 is connected with the incinerator, and the carbon dioxide separation device 7 is used for CO in the regeneration gas2Separating to obtain H in regenerated gas2S can be ignited in the carbon dioxide separation device 7 or be delivered to an external incinerator for combustion to generate SO2And purifying and removing the waste water by a subsequent treatment facility.
Further, as shown in fig. 1, the desorbed gas outlet of the adsorption refining tower 1 is connected to the eighth gas transmission pipeline 18 through the fourth gas transmission pipeline 14, and the desorbed gas from the adsorption refining tower 1 is sequentially transmitted to the reducing gas converter 2 through the fourth gas transmission pipeline 14 and the eighth gas transmission pipeline 18 for combustion and heat supply.
Further, as shown in fig. 1, a raw material gas outlet of the adsorption refining tower 1 is connected to a seventh gas transmission pipeline 17 through a second gas transmission pipeline 12, and the raw material gas output from the adsorption refining tower 1 sequentially passes through the second gas transmission pipeline 12, the seventh gas transmission pipeline 17 and the heat recovery device 8, and then enters the reduction gas conversion furnace 2 as a raw material gas to perform a catalytic reforming reaction.
Further, as shown in fig. 1, the gas outlet of the carbon dioxide separation device 7 is connected to the seventh gas transmission pipeline 17 through the fourteenth gas transmission pipeline 24, and the CO separated by the carbon dioxide separation device 72The gas enters the reducing gas converter 2 as the raw material gas to perform the catalytic reforming reaction after passing through the fourteenth gas transmission pipeline 24, the seventh gas transmission pipeline 17 and the heat recovery device 8 in sequence.
Further, as shown in fig. 1, a desorption gas inlet of the adsorption refining tower 1 is connected to a seventh gas transmission pipeline 17 through a third gas transmission pipeline 13, the process gas in the seventh gas transmission pipeline 17 can be used as desorption gas to be transmitted into the adsorption refining tower 1 for desorption and regeneration of the adsorption refining tower 1, and the desorbed desorption gas is directly transmitted into the reducing gas converter 2 for combustion and heat supply.
In an optional embodiment of the present invention, as shown in fig. 1 and fig. 2, a plurality of catalyst tubes 205 are disposed inside the reducing gas reformer 2, each catalyst tube 205 is connected in parallel between the raw gas inlet 201 of the reducing gas reformer 2 and the reducing gas outlet 202 of the reducing gas reformer 2, and the raw gas discharged from the adsorption refining tower 1, the process gas discharged from the MEA desulfurization device 6, and the regeneration gas discharged from the MEA desulfurization device 6 are catalytically reformed into the reducing gas required for reducing the iron ore through each catalyst tube 205.
Further, the catalyst packed in the catalyst tube 205 may be, but is not limited to, a nickel-based catalyst.
The utility model discloses a theory of operation does: the iron ore is fed into the shaft furnace 10 from the iron ore inlet 1003 of the shaft furnace 10, the reducing gas flows from the bottom to the top in the shaft furnace 10, and the reducing gas (rich in H) flows into the shaft furnace 102And CO gas) with iron ore (Fe)2O3) Reacting to generate sponge iron (Fe) and top gas (rich in H)2CO and CO2A gas); the top gas is firstly output through a top gas outlet 1001 of the shaft furnace 10, firstly enters the heat exchange device 25, exchanges heat with water in the heat exchange device 25, and transmits the generated hot steam to a regeneration tower of the MEA desulfurization device 6 for heating the MEA solution during regeneration; the heat-exchanged top gas enters a scrubber 5 for dedusting and cooling, then enters a desulfurizing tower of an MEA desulfurizing device 6, and H mixed in the top gas is treated by MEA solution2S and CO2Absorbing and removing, wherein the process gas obtained after the purification of the MEA desulfurization device 6 is divided into two parts, one part (accounting for 10 percent to 50 percent of the total amount) of the process gas is conveyed into a heat recovery device 8 to be preheated and heated to 200 ℃ to 400 ℃ (preferably 300 ℃), and then is mixed with desorption gas of an adsorption refining tower 1 and primarily purified coke oven gas (namely fuel gas) which does not pass through the adsorption refining tower 1 to enter a reducing gas converter 2 to be used as fuel for the combustion and heating of the reducing gas converter 2; the other part of the process gas (in total)50% to 90%) of the amount of CO in the raw material gas purified by the adsorption refining tower 1 and the regeneration gas of the MEA desulfurization device 62Mixing, pressurizing to 0.1-0.5 MPa by a pressurizing device 9, preheating to 500-700 ℃ by a heat recovery device 8, and conveying to a reducing gas converter 2, CO in the process gas, the raw material gas and the regeneration gas2Catalytic reforming reaction occurs in the catalyst tubes 205 in the reducing gas reformer 2, and CH in the raw material gas4、CO2CO in process gas and CO in regeneration gas2Reacting as raw material gas to generate CO and H2(chemical formula of reaction: CH)4+CO2＝2CO+2H2) Since the catalytic reforming reaction is endothermic, the heat required is derived from the combustion of part of the process gas, fuel gas and desorbed gases. Finally, the reaction is carried out to produce H-rich2And CO as a reducing gas, is conveyed into the shaft furnace 10 through the reducing gas inlet 1002.
Wherein the MEA solution can react with H in the top gas2S and CO2Absorbing the H absorbed by the MEA solution by heating2S and CO2Released into the regeneration gas, the regeneration gas in the MEA desulfurization device 6 is conveyed to a carbon dioxide separation device 7 to separate CO in the regeneration gas2Separated and sent to a reducing gas converter 2 for CO increase2Content of (2) separating CO from the regeneration gas2H left over after2S is ignited in the carbon dioxide separation device 7 or is transported to an external incinerator for combustion, and the generated SO2And purifying and removing the waste water by a subsequent treatment facility.
The total sulfur content in the primarily purified coke oven gas (namely the coke oven gas which is not purified by the adsorption refining tower 1) is less than or equal to 500mg/Nm3(i.e., 500mg/Nm or less)3) The tar content is less than or equal to 50mg/Nm3(i.e., less than or equal to 50 mg/Nm)3) The BTX (benzene, toluene, xylene, etc.) content is less than or equal to 2500mg/Nm3(i.e., less than or equal to 2500 mg/Nm)3) The naphthalene content is less than or equal to 500mg/Nm3(i.e., 500mg/Nm or less)3) Firstly, about 5 percent of the primarily purified coke oven gas is conveyed to a reducing gas converter for combustion and heat supply, and about 95 percent of the primarily purified coke oven gas is conveyed to a reducing gas converter for combustion and heat supplyThe purified coke oven gas enters an adsorption refining tower 1, impurities such as inorganic sulfur, organic sulfur, tar, benzene, naphthalene and the like in the coke oven gas are adsorbed and removed, the purified coke oven gas (namely, raw gas) is mixed with process gas, pressurized by a pressurizing device 9 and conveyed into a reducing gas conversion furnace 2. After the adsorption refining tower 1 reaches a preset saturation threshold, 2000Nm is extracted3From h to 6000Nm3H (preferably 4000 Nm)3The process gas of/h) is used as desorption gas, the desorption gas is subjected to heat exchange with high-temperature flue gas through a heat recovery device 8 until the temperature of the desorption gas is raised to about 160-350 ℃ (preferably 260 ℃), the molecular sieve material in the adsorption refining tower 1 is regenerated, the regeneration is divided into three stages of temperature rise, heat preservation and cold blowing, and the regeneration period is about 60 hours; in the regeneration process, impurities adsorbed by the molecular sieve material are desorbed into desorption gas, namely desorption gas, the desorption gas in the adsorption refining tower 1, part of the primarily purified coke oven gas and air are mixed and enter the reducing gas conversion furnace 2 for combustion, hydrocarbon such as tar, benzene, naphthalene and the like in the mixed gas is converted into carbon dioxide, water, organic sulfur and inorganic sulfur to be converted into sulfur dioxide, the sulfur dioxide is discharged along with flue gas, and the sulfur dioxide is purified and discharged after reaching the standard.
Second embodiment
As shown in fig. 4, the preparation method of the system for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide of the utility model comprises the following steps:
step S1: the primarily purified coke oven gas passes through the adsorption refining tower 1 to remove impurities mixed in the primarily purified coke oven gas so as to form feed gas.
Further, in step S1, a part of the primarily purified coke oven gas passes through the adsorption refining tower 1 to form a raw material gas, and another part of the primarily purified coke oven gas enters the reducing gas converter 2 to be combusted for heat supply. Wherein the gas amount of the primary purification coke oven entering the adsorption refining tower 1 is 65000Nm3H, the amount of the primarily purified coke oven gas entering the reducing gas reformer 2 is 5000Nm3/h。
Further, in step S1, after the adsorption of the adsorption refining tower 1 reaches the preset saturation threshold, the process gas is extracted and heated, and then introduced into the adsorption refining tower 1 for desorption and regeneration, and the desorbed gas from the adsorption refining tower 1 enters the reducing gas converter 2 for combustion and heat supply.
Step S2: the raw material gas passes through the reducing gas converter 2, and the raw material gas generates reducing gas under the action of the catalyst in the reducing gas converter 2.
Further, in step S2, the raw material gas passing through the reducing gas reformer 2 is required to be pressurized to 0.1MPa to 0.5MPa by the pressurizing device 9 and preheated to 500 ℃ to 700 ℃ by the heat recovery device 8.
Step S3: the reducing gas passes through the shaft furnace 10 and undergoes a reduction reaction with the iron ore in the shaft furnace 10 to obtain sponge iron and top gas.
Further, as shown in fig. 5, step S3 includes:
step S301: processing the iron ore into pellets or lump ore, and feeding the pellets or lump ore into the shaft furnace 10 from an iron ore inlet 1003 of the shaft furnace 10;
step S302: the reducing gas flows from bottom to top in the shaft furnace 10 and undergoes a reduction reaction with the iron ore in the shaft furnace 10 to obtain sponge iron and top gas.
Step S4: the top gas is discharged from the shaft furnace 10, and hydrogen sulfide and carbon dioxide in the top gas are absorbed by the MEA desulfurization apparatus 6 to form a process gas.
Step S5: the MEA desulfurization device 6 is heated to release the absorbed hydrogen sulfide and carbon dioxide into the regeneration gas.
Further, as shown in fig. 6, step S5 includes:
step S501: the saturated MEA solution enters a regeneration tower from a desulfurization tower, wherein the operation pressure of the desulfurization tower is 5kPa to 0.1MPa, and the operation pressure of the regeneration tower is 5kPa to 60 kPa;
step S502: heating the regeneration tower by hot steam to release hydrogen sulfide and carbon dioxide absorbed in the MEA solution into regeneration gas; wherein, the hot steam is generated after the heat exchanger 3 exchanges heat with the top gas.
Step S503: and returning the regenerated MEA solution from the regeneration tower to the desulfurization tower for recycling.
Step S6: separating carbon dioxide in the regeneration gas, and combusting hydrogen sulfide in the regeneration gas.
Further, the regeneration gas is passed into a carbon dioxide separation device 7 to remove CO in the regeneration gas2Separating, and arranging combustion equipment in the carbon dioxide separator 7 or connecting the carbon dioxide separator 7 with the incinerator to separate CO2After that, H remaining in the regeneration gas2S can be ignited in the carbon dioxide separation device 7 or be delivered to an external incinerator for combustion to generate SO2And purifying and removing the waste water by a subsequent treatment facility.
Further, in step S6, the carbon dioxide separated from the regeneration gas of the MEA desulfurization apparatus 6 needs to be preheated by the heat recovery apparatus 8 to be raised to 500 to 700 ℃.
Step S7: the process gas in the step S4 is divided into two parts, one part of the process gas enters the reducing gas converter 2 to be combusted for heat supply, the other part of the process gas, the feed gas and the carbon dioxide separated from the regeneration gas are mixed and then pass through the reducing gas converter 2, and the mixed gas of the process gas, the feed gas and the carbon dioxide separated from the regeneration gas generates the reducing gas again under the action of the catalyst in the reducing gas converter 2.
Further, in step S7, a part of the process gas entering the reducing gas reformer 2 for combustion needs to be preheated by the heat recovery device 8 to be raised to 200 to 400 ℃.
Further, in step S7, another part of the process gas and the raw material gas for the catalytic reaction by the reducing gas reformer 2 is pressurized to 0.25MPa by the pressurizing device 9 and preheated to 500 to 700 ℃ by the heat recovery device 8.
Further, in step S7, the pressure of the reducing gas is 0.08MPa to 0.4MPa, the temperature of the reducing gas is 850 ℃ to 1100 ℃, and the reducing gas is
Greater than 10 in reducing gas
Greater than 0.3.
Preferably, in a reducing gas
Is 1 to 3.
Further, in step S7, the process gas introduced into the reducing gas reformer 2 for combustion accounts for 10% to 50% of the total amount; the process gas entering the reducing gas reformer 2 for the reforming reaction accounts for 50 to 90% of the total.
Further, in step S7, the process gas introduced into the reducing gas reformer 2 for combustion accounts for 20% of the total amount; the process gas entering the reducing gas reformer 2 for the reforming reaction accounts for 80% of the total amount.
Step S8: the reducing gas passes through the shaft furnace 10 again and undergoes a reduction reaction with the iron ore in the shaft furnace 10 to obtain sponge iron and top gas.
Further, in step S8, the temperature condition for the reduction reaction of the reducing gas and the iron ore is 930 ℃.
Step S9: and (4) circulating the steps S4 to S8 until the iron ore in the shaft furnace 10 is completely reacted to generate the sponge iron.
The utility model discloses a concrete embodiment does:
iron ore (Fe)2O3) After being processed into pellets or lump ore, the raw materials are fed from an iron ore inlet 1003 of the shaft furnace 10, reducing gas reversely flows from bottom to top in the shaft furnace 10 and is subjected to reduction reaction with the iron ore at 930 ℃ to obtain sponge iron (Fe) and top gas (rich in H)2CO and CO2Gas). The top gas is discharged from a top gas outlet 1001 of the shaft furnace 10 and enters the heat exchanger 3, the top gas exchanges heat with water conveyed by the steam drum 4 in the heat exchanger 3, and hot steam enters the steam drum 4 and is conveyed to the MEA desulfurization device 6 for heating and regeneration of the MEA solution. The heat-exchanged top gas enters a scrubber 5 for cooling and dust removal, and then enters an MEA desulfurization device 6 for mixing H in the top gas2S and CO2The process gas output after passing through the MEA desulfurization device 6 is divided into two parts, wherein one part of the process gas accounts for 10-50% of the total amount, and the preferred part is 20%After being preheated to the temperature of 300 ℃ by the heat recovery device 8, the waste gas enters the reducing gas reformer 2 through the fuel gas inlet 203 of the reducing gas reformer 2 to be combusted so as to supply heat to the reducing gas reformer 2; the other part of the process gas (50 to 90% of the total amount, preferably 70%) is pressurized to 0.25MPa by the pressurizing device 9, and after passing through the heat recovery device 8, preheated to a temperature of 600 ℃, and enters the catalyst tube 205 in the reducing gas converter 2 through the raw gas inlet 201 of the reducing gas converter 2. The mixed gas of the process gas and the raw material gas undergoes a reforming reaction under the action of the catalyst in the catalyst tube 205 to convert CH4And CO2Reforming to H2And CO. In the reducing gas reformer 2, the catalyst tube 205 is heated by high-temperature flue gas burned from the outside, the temperature of the reducing gas obtained by the reaction is about 930 ℃,
and is about 1.6 of the total weight of the alloy,
the reducing gas is fed into the shaft furnace 10 through the reducing gas inlet 1002 to react with the iron ore in the shaft furnace 10 to produce sponge iron, and the sponge iron with the temperature of 500 ℃ is output from the sponge iron outlet 1004 at the lower part of the shaft furnace 10.
Wherein, the MEA desulfurization device 6 absorbs H by adopting MEA solution2S and CO2The operating temperature of the desulfurizing tower is 40 ℃, and H is absorbed2S and CO2The saturated MEA solution enters a regeneration tower for regeneration, the regeneration temperature is 110 ℃, and the regenerated MEA solution returns to the desulfurization tower for recycling; when the MEA solution is regenerated, the MEA solution is heated by water vapor, and the regenerated gas mainly contains H2S and CO2The regenerated gas enters a carbon dioxide separation device 7, and CO separated out2The residual H is separated from the process gas in the reducing gas converter 22S is converted into sulfur dioxide through combustion to be purified.
Wherein, the primary purified coke oven gas is 70000Nm3H, total sulfur content 300mg/Nm3Tar content of 20mg/Nm and benzene content of 500mg/Nm3Naphthalene content of 500mg/Nm3A part of preliminary purificationCoke oven gas (65000 Nm)3H) enters an adsorption refining tower 1 for purification, and the content of sulfur in the purified coke oven gas is less than 1mg/Nm3Benzene content of less than 1mg/Nm3Naphthalene content of less than 1mg/Nm3The other part of the coke oven gas is primarily purified (5000 Nm)3H) conveying the gas to the reducing gas reformer 2 for combustion and heat supply.
Wherein, the number of the adsorption refining towers 1 is 7, and 1 is a standby adsorption refining tower. After the adsorption of the adsorption refining tower 1 reaches a preset saturation threshold, extracting 5000Nm3The temperature of the process gas is raised to 260 ℃ through a heat recovery device 8, and then the process gas is introduced into the adsorption refining tower 1 for desorption and regeneration. The regeneration of the adsorption refining tower 1 is divided into three stages of temperature rise, heat preservation and cooling, and the regeneration period is 3 days. In the regeneration process, impurities such as sulfur, benzene, naphthalene, tar and the like adsorbed by the molecular sieve material enter desorption gas, the desorption gas, part of the primarily purified coke oven gas and part of the process gas are mixed and enter the reducing gas converter 2 to be combusted to provide heat, and pollutants in the mixed gas are converted into H2O、CO2And SO2Enters the flue gas, is purified and discharged after reaching the standard.
The utility model discloses a system for coke oven gas coupling carbon dioxide preparation shaft furnace is the gas that reduces of characteristics and advantage are:
firstly, the system for preparing the shaft furnace reducing gas by coupling the coke oven gas with the carbon dioxide carries out adsorption and desorption treatment on inorganic sulfur, organic sulfur, tar, benzene, naphthalene and other impurities in the coke oven gas through the molecular sieve material in the adsorption refining tower 1, and the regenerated desorption gas can be sent to the reducing gas conversion furnace 2 to be used as fuel gas to carry out combustion and heat supply, and the system has the advantages of simple structure, high energy utilization rate, less investment compared with the traditional purification device, low cost and no secondary pollution.
Secondly, the system for preparing the shaft furnace reducing gas by coupling the coke oven gas with the carbon dioxide absorbs and removes the hydrogen sulfide and the carbon dioxide in the top gas through the MEA desulfurization device 6, the heat required by the regeneration of the MEA solution comes from the heat exchanger 3, not only can the heat carried by the top gas be recycled and fully utilized, but also the carbon dioxide in the regenerated gas after the regeneration of the MEA solution is introduced into the reducing gas conversion furnace 2 for catalytic conversion into the shaft furnace 10Reducing gas used, CO added2The catalytic reaction can be more fully and completely carried out.
Thirdly, the system for preparing shaft furnace reducing gas by coupling the coke oven gas with the carbon dioxide adopts the coke oven gas purified by the adsorption refining tower 1 and CO generated by the shaft furnace 102Catalytic conversion to H-rich2Reducing CO gas to achieve energy conservation and emission reduction of CO2The reducing gas component is adjustable.
The system for preparing the shaft furnace reducing gas by coupling the coke oven gas with the carbon dioxide is provided with a heat recovery device 8 and a heat exchange device 25, the process gas entering the reducing gas converter 2 is preheated, the reducing gas produced by the reducing gas converter 2 can be directly conveyed to the shaft furnace 10 to carry out reduction reaction with iron ore, the energy consumption is low, and the process is simple.
The above description is only exemplary of the present invention, and is not intended to limit the scope of the present invention. Any person skilled in the art should also realize that such equivalent changes and modifications can be made without departing from the spirit and principles of the present invention.
Claims (14)
1. A system for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide is characterized by comprising an adsorption refining tower (1) for purifying the coke oven gas, a reducing gas converter (2) for converting the purified coke oven gas into the reducing gas and an MEA (MEA) desulfurization device (6) for purifying the top gas discharged from a shaft furnace (10), wherein:
the coke oven gas inlet of the adsorption refining tower (1) is connected with a coke oven gas pipeline, the raw gas outlet of the adsorption refining tower (1) is connected with the raw gas inlet (201) of the reducing gas converter (2), the desorption gas outlet of the adsorption refining tower (1) is connected with the fuel gas inlet (203) of the reducing gas converter (2), the reducing gas outlet (202) of the reducing gas converter (2) is connected with the reducing gas inlet (1002) of the shaft furnace (10), the top gas outlet (1001) of the shaft furnace (10) is connected with the top gas inlet of the MEA desulfurization device (6), the process gas outlet of the MEA desulfurization device (6) is respectively connected with the fuel gas inlet (203) of the reducing gas converter (2), the raw gas inlet (201) of the reducing gas converter (2) and the desorption gas inlet of the adsorption refining tower (1), the regeneration gas outlet of the MEA desulfurization device (6) is connected with the raw gas inlet (201) of the reducing gas converter (2) through a carbon dioxide separation device (7).
2. The system for preparing the reducing gas of the shaft furnace by coupling the coke oven gas with the carbon dioxide as claimed in claim 1, wherein the fuel gas inlet (203) of the reducing gas reformer (2) is connected with a coke oven gas pipeline.
3. The system for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide according to claim 1, characterized in that the adsorption and refining tower (1) is filled with molecular sieve materials which can adsorb impurities contained in coke oven gas and can be desorbed and regenerated after being heated.
4. The system for preparing the reducing gas of the shaft furnace by coupling coke oven gas with carbon dioxide as claimed in claim 3, wherein the number of the adsorption and purification towers (1) is multiple, and at least one of the adsorption and purification towers (1) is a spare adsorption and purification tower.
5. The system for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide according to claim 1, the system is characterized by also comprising a heat recovery device (8) for preheating and raising the temperature of the process gas discharged by the MEA desulfurization device (6) and the raw gas discharged by the adsorption refining tower (1), the process gas outlet of the MEA desulfurization device (6) is respectively connected with the fuel gas inlet (203) of the reducing gas reformer (2), the raw gas inlet (201) of the reducing gas reformer (2) and the desorption gas inlet of the adsorption refining tower (1) through the heat recovery device (8), and a raw material gas outlet of the adsorption refining tower (1) is connected with a raw material gas inlet (201) of the reducing gas converter (2) through the heat recovery device (8).
6. The system for preparing the reducing gas of the shaft furnace by coupling coke oven gas and carbon dioxide according to claim 5, characterized in that the flue gas outlet of the reducing gas reformer (2) is connected with the flue gas inlet of the heat recovery device (8), and the flue gas outlet of the heat recovery device (8) is directly communicated with the outside.
7. The system for preparing the reducing gas of the shaft furnace by coupling coke oven gas and carbon dioxide according to claim 5, characterized in that the regeneration gas outlet of the MEA desulfurization device (6) is connected with the raw material gas inlet (201) of the reducing gas converter (2) sequentially through the carbon dioxide separation device (7) and the heat recovery device (8).
8. The system for preparing the shaft furnace reducing gas by coupling the coke oven gas with the carbon dioxide according to claim 1, further comprising a heat exchange device (25) and a scrubber (5), wherein the heat exchange device (25) comprises a heat exchanger (3) and a steam drum (4) connected with the heat exchanger (3), an air inlet of the heat exchanger (3) is connected with a top gas outlet (1001) of the shaft furnace (10), an air outlet of the heat exchanger (3) is connected with an air inlet of the scrubber (5), an air outlet of the scrubber (5) is connected with a top gas inlet of the MEA desulfurization device (6), and a hot steam outlet (401) of the steam drum (4) is connected with a heat source inlet of the MEA desulfurization device (6).
9. The system for preparing the reducing gas of the shaft furnace by coupling coke oven gas with carbon dioxide according to claim 8, wherein the MEA desulfurization device (6) comprises at least one reaction tower and at least one regeneration tower connected with the reaction tower, the reaction tower is filled with an MEA solution capable of adsorbing carbon dioxide and hydrogen sulfide, the gas inlet of the reaction tower is connected with the gas outlet of the scrubber (5), the gas outlet of the reaction tower is respectively connected with the fuel gas inlet (203) of the reducing gas reformer (2), the raw gas inlet (201) of the reducing gas reformer (2) and the stripping gas inlet of the adsorption refining tower (1), and the gas inlet of the regeneration tower is connected with the hot steam outlet (401) of the steam drum (4);
the gas inlet of the reaction tower is a furnace top gas inlet of the MEA desulfurization device (6), the gas outlet of the reaction tower is a process gas outlet of the MEA desulfurization device (6), and the gas inlet of the regeneration tower is a heat source inlet of the MEA desulfurization device (6).
10. The system for preparing reducing gas of the shaft furnace by coupling coke oven gas and carbon dioxide according to claim 1, characterized in that a combustion device is arranged inside the carbon dioxide separation device (7) or a tail gas outlet of the carbon dioxide separation device (7) is connected with an incinerator.
11. The system for preparing the reducing gas of the shaft furnace by coupling coke oven gas and carbon dioxide according to claim 1, wherein a pressurizing device (9) for adjusting the gas transmission pressure is arranged between the process gas outlet of the MEA desulfurization device (6) and the raw gas inlet (201) of the reducing gas conversion furnace (2).
12. The system for preparing the reducing gas of the shaft furnace by coupling coke oven gas with carbon dioxide according to claim 1, wherein a plurality of catalyst pipes (205) for catalytically reforming the raw gas discharged from the adsorption refining tower (1), the process gas discharged from the MEA desulfurization device (6) and the regeneration gas discharged from the MEA desulfurization device (6) into the reducing gas required for reducing iron ore are arranged in the reducing gas converter (2), and each catalyst pipe (205) is connected in parallel between the raw gas inlet (201) of the reducing gas converter (2) and the reducing gas outlet (202) of the reducing gas converter (2).
13. The system for preparing the reducing gas of the shaft furnace by coupling coke oven gas and carbon dioxide according to claim 12, wherein the catalyst pipe (205) is filled with a nickel-based catalyst.
14. The system for preparing reducing gas of the shaft furnace by coupling coke oven gas with carbon dioxide according to claim 1, wherein the top gas outlet (1001) is arranged at the top of the shaft furnace (10), and an iron ore inlet (1003) is arranged at the top of the shaft furnace (10) and above the top gas outlet (1001);
the reducing gas inlet (1002) is arranged at the bottom of the shaft furnace (10), and a sponge iron outlet (1004) is arranged at the bottom of the shaft furnace (10) and below the reducing gas inlet (1002).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022850747.XU CN213772103U (en) | 2020-12-02 | 2020-12-02 | System for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022850747.XU CN213772103U (en) | 2020-12-02 | 2020-12-02 | System for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213772103U true CN213772103U (en) | 2021-07-23 |
Family
ID=76895601
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022850747.XU Active CN213772103U (en) | 2020-12-02 | 2020-12-02 | System for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213772103U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114574647A (en) * | 2020-12-02 | 2022-06-03 | 北京京诚泽宇能源环保工程技术有限公司 | System and method for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide |
-
2020
- 2020-12-02 CN CN202022850747.XU patent/CN213772103U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114574647A (en) * | 2020-12-02 | 2022-06-03 | 北京京诚泽宇能源环保工程技术有限公司 | System and method for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide |
| CN114574647B (en) * | 2020-12-02 | 2023-10-03 | 北京京诚泽宇能源环保工程技术有限公司 | System and method for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104803819B (en) | A kind of method and system utilizing fine coal preparing ethylene | |
| RU2532757C2 (en) | Method of reduction based on reforming-gas with reduced nox emissions | |
| CN107115775B (en) | Iron ore sintering flue gas sectional enrichment self-heat exchange emission reduction SOxAnd NOxMethod of producing a composite material | |
| CN103805728B (en) | Method and device for producing reduced iron through synthetic gas prepared from high-nitrogen content retort gas | |
| CN113736943A (en) | Direct reduction method for producing sponge iron by converting hydrocarbon-rich gas | |
| CN111847381B (en) | Method and device for preparing hydrogen from industrial waste gas | |
| CN101239702A (en) | High temperature coke oven crude gas hydrogen generating system device and technique | |
| CN213772103U (en) | System for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide | |
| CN111270036A (en) | System and process method for producing sponge iron by direct reduction of hydrogen energy | |
| CN213772106U (en) | Gas-based shaft furnace reducing gas preparation system | |
| CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
| CN114574647B (en) | System and method for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide | |
| CN108011119B (en) | Method and system for clean power generation and resource utilization of hydrogen-containing waste gas coupled fuel cell | |
| CN113955718B (en) | Direct reforming process and system for non-catalytic partial oxidation of high-temperature raw gas | |
| CN213772104U (en) | Shaft furnace reducing gas preparation and self desorption system | |
| CN213895742U (en) | Shaft furnace reducing gas preparation and desorption gas self-heating system | |
| CN213772105U (en) | Shaft furnace reducing gas preparation and dry desulphurization system | |
| CN113373274B (en) | Coal gas treatment process for full hydrogen shaft furnace | |
| CN213895743U (en) | Shaft furnace reducing gas preparation and oxygen spraying temperature rising system | |
| CN213895738U (en) | System for preparing gas-based shaft furnace reducing gas by purifying coke oven gas | |
| CN114574648B (en) | System and method for preparing reducing gas of gas-based shaft furnace | |
| CN213895741U (en) | Shaft furnace reducing gas preparation and humidification carbon elimination system | |
| CN212102909U (en) | System for producing sponge iron by direct reduction of hydrogen energy | |
| CN114774611A (en) | Hydrogen rich gas CO2Method for producing iron by oxidation conversion and hydrogen-based shaft furnace direct reduction | |
| CN210885331U (en) | Device for producing synthetic ammonia by utilizing sodium cyanide tail gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |