CN213772106U - Gas-based shaft furnace reducing gas preparation system - Google Patents
Gas-based shaft furnace reducing gas preparation system Download PDFInfo
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- CN213772106U CN213772106U CN202022857598.XU CN202022857598U CN213772106U CN 213772106 U CN213772106 U CN 213772106U CN 202022857598 U CN202022857598 U CN 202022857598U CN 213772106 U CN213772106 U CN 213772106U
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Abstract
The utility model relates to a gas-based shaft furnace reduction gas preparation system, this system is including adsorbing refined tower, reduction gas reborner and top gas purifier, the coke oven gas import and the coke oven gas pipe connection of adsorbing refined tower, the feed gas export of adsorbing refined tower and the feed gas access connection of reduction gas reborner, the desorption gas export of adsorbing refined tower and the fuel gas access connection of reduction gas reborner, the reduction gas export of reduction gas reborner and the reduction gas access connection of shaft furnace, the top gas export of shaft furnace and top gas purifier's top gas access connection, top gas purifier's process gas export respectively with the fuel gas entry of reduction gas reborner, the feed gas entry of reduction gas reborner and the desorption gas access connection of adsorbing refined tower. 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, it is further, relate to a gas-based shaft furnace reducing gas preparation system, especially relate to a system that adopts coke oven gas 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 reduction of iron ore and electric furnace steel making. The traditional blast furnace iron making has the characteristics of long process, high energy consumption, heavy pollution, coke consumption and the like, and although various energy-saving and emission-reduction measures have been implemented to achieve certain effects, the metallurgical thermodynamic reaction related to the long process based on carbon reduction tends to the limit level, and the CO emission is continuously reduced2Has 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 the present stage, the social and economic structure of China cannot provide enough scrap steel as a raw material of a short process, and sponge iron needs to be adopted to replace the scrap steel as the raw material. Direct Reduction Iron (also called sponge Iron) in short process, stable in composition and harmful impuritiesThe element content is low, the steel is a high-quality raw material for steelmaking, the steel can be used as a raw material for electric furnace steelmaking and a coolant for converter steelmaking to supplement the shortage of scrap steel resources, and the steel can be irreplaceable for 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、NH3The impurities such as BTX (benzene, toluene, xylene and the like), tar, naphthalene and the like cause that the traditional gas-based shaft furnace process using natural gas as a gas source cannot run, and the development of the gas-based shaft furnace process suitable for a coke oven is neededA gas-based shaft furnace reduction gas process of coal gas.
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 gas-based shaft furnace reducing gas preparation system 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 gas-based shaft furnace reduction gas preparation system, can adsorb the desorption to the impurity in the coke oven gas, desorption gas after the regeneration can be sent to the reduction gas reborner and burns the heat supply, coke oven gas after the purification mixes and catalytic conversion is the reduction gas that the shaft furnace used with the top gas after the purification treatment, it is many to have solved impurity in the coke oven gas, purify difficult problem, not only have the feed gas component adjustable advantage of reduction gas reborner, and reach energy-conservation and emission reduction 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 gas-based shaft furnace reduction gas preparation system, including the absorption refining tower that carries out purification treatment to coke oven gas, turn into the reduction gas reborner of reduction gas with coke oven gas after purifying and carry out purification treatment's top gas purifier 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 top gas purification device, and the process gas outlet of the top gas purification 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.
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, gas-based shaft furnace reduction gas preparation system still include to furnace roof gas purifier exhaust process gas and the raw gas that the absorption refining tower got rid of preheats the heat recovery unit who heaies up, furnace roof gas purifier's process gas export passes 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 top gas purification device comprises a heat exchanger, a scrubber and an adsorption desulfurization tower, wherein an air inlet of the heat exchanger is connected to a top gas outlet of the shaft furnace, an air outlet of the heat exchanger is connected to an air inlet of the scrubber, an air outlet of the scrubber is connected to an air inlet of the adsorption desulfurization tower, and an air outlet of the adsorption desulfurization tower is connected to a fuel gas inlet of the reducing gas reformer and a raw material gas inlet of the reducing gas reformer respectively;
the gas inlet of the heat exchanger is the top gas inlet of the top gas purification device, and the gas outlet of the adsorption desulfurization tower is the process gas outlet of the top gas purification device.
In a preferred embodiment of the present invention, the desorption gas outlet of the adsorption desulfurization tower is connected to the desorption gas inlet of the heat exchanger, and the desorption gas outlet of the heat exchanger is connected to the desorption gas inlet of the adsorption desulfurization tower.
In a preferred embodiment of the present invention, the desorption gas outlet of the adsorption desulfurization tower is connected to the fuel gas inlet of the reducing gas reformer through the heat recovery unit.
In a preferred embodiment of the present invention, the adsorption desulfurization tower is filled with a molecular sieve material that can adsorb organic sulfur and inorganic sulfur contained in the top gas and can be desorbed and regenerated after being heated.
In a preferred embodiment of the present invention, the number of the adsorption desulfurization towers is plural, and at least one of the adsorption desulfurization towers is a spare adsorption desulfurization tower.
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 top gas purification 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 and the process gas discharged from the top gas purification apparatus into the reducing gas required for reducing the iron ore, and each of the catalyst tubes is 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 foregoing, the utility model discloses a gas-based shaft furnace is original gas preparation system's characteristics and advantage are: the coke oven gas is purified by an 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, desorption gas generated after the regeneration of the adsorption refining tower can be sent to a reducing gas conversion furnace for combustion and heat supply, the purified coke oven gas is mixed with purified top gas and is catalytically converted into H-rich gas in the reducing gas conversion furnace2And the reducing gas of CO can be used for carrying out reduction reaction with the iron ore in the shaft furnace, solves the problems of more impurities and difficult purification in the coke oven gas, and has the advantages of adjustable components of the raw material gas of the reducing gas converter, energy conservation and emission reduction of CO2The 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 the reducing gas preparation system of the gas-based shaft furnace.
FIG. 2: is a structural schematic diagram of a furnace top gas purification device in the gas-based shaft furnace reducing gas preparation system of the utility model.
FIG. 3: is a schematic structural diagram of a reducing gas converter in the gas-based shaft furnace reducing gas preparation system of the utility model.
FIG. 4: is one of the process flow charts of the preparation method adopted by the gas-based shaft furnace reducing gas preparation system of the utility model.
FIG. 5: the second technical flow chart of the preparation method adopted by the gas-based shaft furnace reducing gas preparation system of the utility model.
FIG. 6: the third process flow chart of the preparation method adopted by the gas-based shaft furnace reducing gas preparation system of the utility model 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 top gas purification device;
301. a heat exchanger; 302. A scrubber;
303. an adsorption desulfurization tower; 4. A heat recovery device;
5. a pressurizing device; 6. A shaft furnace;
601. a top gas outlet; 602. A reducing gas inlet;
603. an iron ore inlet; 604. A sponge iron outlet;
10. a first gas transmission pipeline; 11. A second gas transmission pipeline;
12. a third gas transmission pipeline; 13. A fourth gas transmission pipeline;
14. a fifth gas transmission pipeline; 15. A sixth gas transmission pipeline;
16. a seventh gas transmission pipeline; 17. An eighth gas transmission pipeline;
18. a ninth gas transmission pipeline; 19. A tenth gas transmission pipeline;
20. an eleventh gas transmission pipeline; 21. A twelfth gas transmission pipeline;
22. a thirteenth gas transmission pipeline; 23. A fourteenth gas transmission pipeline.
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
The utility model provides a gas-based shaft furnace reduction gas preparation system, this gas-based shaft furnace reduction gas preparation system are including adsorbing refined tower 1, reduction gas reborner 2 and top gas purification device 3, adsorb refined tower 1 and are used for carrying out purification treatment to coke oven gas, and reduction gas reborner 2 is used for turning into the coke oven gas after purifying into reduction gas, and top gas purification device 3 is used for carrying out purification treatment to 6 exhaust top gases of shaft furnace. Wherein: the coke oven gas inlet of the adsorption refining tower 1 is connected with a coke oven gas pipeline, the fuel gas inlet 203 of the reducing gas reforming tower 2 is connected with the coke oven gas pipeline through a first gas transmission pipeline 10, the raw gas outlet of the adsorption refining tower 1 is connected with the raw gas inlet 201 of the reducing gas reforming tower 2, the desorption gas outlet of the adsorption refining tower 1 is connected with the fuel gas inlet 203 of the reducing gas reforming tower 2, the reducing gas outlet 202 of the reducing gas reforming tower 2 is connected with the reducing gas inlet 602 of the shaft furnace 6 through a fifth gas transmission pipeline 14, the top gas outlet 601 of the shaft furnace 6 is connected with the top gas inlet of the top gas purifying device 3, and the process gas outlet of the top gas purifying device 3 is respectively connected with the fuel gas inlet 203 of the reducing gas reforming tower 2, the raw gas inlet 201 of the reducing gas reforming tower 2 and the desorption gas inlet of the adsorption refining tower 1.
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, and the desorption gas after adsorbing refined tower 1 regeneration can be delivered to reduction gas reborner 2 and burn the heat supply, and coke oven gas after the purification mixes with the top gas after the purification treatment to catalytic conversion is rich in H in reduction gas reborner 22And the reducing gas of CO can be used for carrying out reduction reaction with the iron ore in the shaft furnace 6, solves the problems of more impurities and difficult purification in the coke oven gas, and the utility model discloses not only have the advantage of the feed gas component adjustable of the reducing gas reformer, reach energy saving 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 601 is provided at the top of the shaft furnace 6, and an iron ore inlet 603 is provided at the top of the shaft furnace 6 and above the top gas outlet 601; a reducing gas inlet 602 is provided at the bottom of the shaft furnace 6 and a sponge iron outlet 604 is provided at the bottom of the shaft furnace 6 below the reducing gas inlet 602.
Further, the pressure of the reducing gas in the fifth gas transmission pipeline 14 is 0.08MPa to 0.5MPa, 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 which can adsorb impurities such as inorganic sulfur, organic sulfur, tar, benzene, and naphthalene 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 gas-based shaft furnace reducing gas preparation system further includes a heat recovery device 4, the heat recovery device 4 is used for preheating the process gas exhausted from the furnace top gas purification device 3 and the raw gas exhausted from the adsorption refining tower 1, the process gas outlet of the furnace top gas purification device 3 is 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 4, respectively, and the raw gas outlet of the adsorption refining tower 1 is connected with the raw gas inlet 201 of the reducing gas reformer 2 through the heat recovery device 4. The process gas and the feed gas before entering the reducing gas reformer 2 are preheated by the heat recovery device 4.
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 4 through a sixth gas transmission pipeline 15, and the flue gas outlet of the heat recovery device 4 is directly communicated with the outside.
In an alternative embodiment of the present invention, as shown in fig. 1, a pressurizing device 5 is disposed between the process gas outlet of the top gas purifying device 3 and the raw gas inlet 201 of the reducing gas reformer 2, and the pressurizing device 5 adjusts the gas pressure to pressurize the process gas and the raw gas and then deliver the pressurized process gas and the raw gas to the raw gas inlet 201 of the reducing gas reformer 2.
Further, the pressing device 5 may be, but is not limited to, a press.
In an alternative embodiment of the present invention, as shown in fig. 1 and 2, the top gas cleaning device 3 comprises a heat exchanger 301, the gas inlet of the heat exchanger 301 is connected with a top gas outlet 601 of the shaft furnace 6 through a ninth gas transmission pipeline 18, the gas outlet of the heat exchanger 301 is connected with the gas inlet of the scrubber 302 through a tenth gas transmission pipeline 19, the gas outlet of the scrubber 302 is connected with the gas inlet of the adsorption desulfurization tower 303 through an eleventh gas transmission pipeline 20, the gas outlet of the adsorption desulfurization tower 303 is connected with a fuel gas inlet 203 of the reducing gas reformer 2 through an eighth gas transmission pipeline 17, the gas outlet of the adsorption desulfurization tower 303 is further connected with a raw gas inlet 201 of the reducing gas reformer 2 through a seventh gas transmission pipeline 16, the seventh gas transmission pipeline 16 and the eighth gas transmission pipeline 17 both pass through the heat recovery device 4, and the pressurizing device 5 is arranged on the seventh gas transmission pipeline 16. Wherein, the air inlet of the heat exchanger 301 is the top gas inlet of the top gas purification device 3, and the air outlet of the adsorption desulfurization tower 303 is the process gas outlet of the top gas purification device 3.
Further, as shown in fig. 1, the desorbed gas outlet of the adsorption refining tower 1 is connected to the eighth gas transmission pipeline 17 through the fourth gas transmission pipeline 13, and the desorbed gas from the adsorption refining tower 1 is transmitted to the reducing gas converter 2 through the fourth gas transmission pipeline 13 and the eighth gas transmission pipeline 17 in sequence 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 16 through a second gas transmission pipeline 11, and the raw material gas output from the adsorption refining tower 1 sequentially passes through the second gas transmission pipeline 11, the seventh gas transmission pipeline 16 and the heat recovery device 4, 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, a desorption gas inlet of the adsorption refining tower 1 is connected to a seventh gas transmission pipeline 16 through a third gas transmission pipeline 12, the process gas in the seventh gas transmission pipeline 16 can be used as desorption gas of the adsorption refining tower 1 and conveyed into the adsorption refining tower 1 for desorption and regeneration of the adsorption refining tower 1, and the desorption gas of the adsorption refining tower 1 is directly conveyed into the reducing gas converter 2 for combustion and heat supply.
Further, as shown in fig. 1, a desorption gas outlet of the adsorption desulfurization tower 303 is connected with a desorption gas inlet of the heat exchanger 301 through a thirteenth gas conveying pipeline 22, and a desorption gas outlet of the heat exchanger 301 is connected with a desorption gas inlet of the adsorption desulfurization tower 303 through a twelfth gas conveying pipeline 21.
Further, as shown in fig. 1, the desorption gas outlet of the adsorption desulfurization tower 303 is connected to the fuel gas inlet 203 of the reducing gas reformer 2 sequentially through the fourteenth gas transmission pipeline 23 and the eighth gas transmission pipeline 17, and is preheated by the heat recovery device 4, and then introduced into the reducing gas reformer 2 for combustion and heat supply.
In an alternative embodiment of the present invention, the adsorption desulfurization tower 303 is filled with a molecular sieve material that can adsorb organic sulfur and inorganic sulfur contained in the top gas and can be desorbed and regenerated after heating. Wherein, the pressure difference between the air inlet of the adsorption desulfurization tower 303 and the air outlet of the adsorption desulfurization tower 303 is 4kPa, and the operating pressure of the adsorption desulfurization tower 303 is 5kPa to 0.1 MPa.
Preferably, the molecular sieve material is a hydrophobic microcrystalline material, can adsorb inorganic sulfur and organic sulfur, 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 7-10 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 desulfurization towers 303 is plural, and at least one of the adsorption desulfurization towers 303 is a spare adsorption desulfurization tower.
In an optional embodiment of the present invention, as shown in fig. 1 and fig. 3, 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 and the process gas discharged from the top gas purification apparatus 3 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 6 from the iron ore inlet 603 of the shaft furnace 6, the reducing gas flows from bottom to top in the shaft furnace 6, and the reducing gas (rich in H) flows from bottom to top2And 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 601 of the shaft furnace 6 and firstly enters the heat exchanger 301, and the top gas and part of desorption gas (rich in H) output by the adsorption desulfurization tower 3032CO and CO2Gas) is subjected to heat exchange, the gas enters the scrubber 302 for dedusting and cooling, then enters the adsorption desulfurization tower 303 for removing organic sulfur, inorganic sulfur and other impurities in the top gas by adopting a molecular sieve material, the process gas purified by the adsorption desulfurization tower 303 is divided into two parts, one part of the process gas is mixed with the desorption gas output by the adsorption desulfurization tower 302 and is conveyed to the heat recovery device 4 for preheating and heating to about 300 ℃, and then is mixed with the primarily purified coke oven gas which does not pass through the adsorption refining tower 1 (namely: fuel gas) is mixed and enters the reducing gas reformer 2 as fuel for the reducing gas reformer 2 to burn and heat; the other part of the process gas is mixed with the raw material gas purified by the adsorption refining tower 1, after the pressure is increased to 0.1MPa to 0.5MPa by the pressure device 5, the mixture is preheated to 500 ℃ to 700 ℃ by the heat recovery device 4 and is conveyed to the reducing gas converter 2, the mixed gas of the process gas and the raw material gas generates catalytic reforming reaction in the catalyst pipe 205 in the reducing gas converter 2, and CH in the raw material gas4、CO2And CO in the process gas is used as raw material gas to react to generate CO and H2(chemical formula of reaction: CH)4+CO2＝2CO+2H2) Since the catalytic reforming reaction is an endothermic reaction, the required heat is generated by burning part of the process gas, the fuel gas, the desorption gas generated by the adsorption refining tower 1, and the desorption gas generated by the adsorption desulfurization tower 303. Finally, the reaction is carried out to produce H-rich2And CO as a reducing gas, is conveyed into the shaft furnace 6 through a reducing gas inlet 602.
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 enters an adsorption refining tower 1, andthe impurities such as inorganic sulfur, organic sulfur, tar, benzene and naphthalene in the coke oven gas are absorbed and removed, the purified coke oven gas (namely, raw material gas) is mixed with the process gas, pressurized by a pressurizing device 5 and conveyed into a reducing gas conversion furnace 2. When the adsorption refining tower 1 reaches a preset saturation threshold value, extracting 4000Nm3The process gas is used as desorption gas of the adsorption refining tower 1, the desorption gas of the adsorption refining tower 1 exchanges heat with high-temperature flue gas through a heat recovery device 4 until the temperature of the desorption gas of the adsorption refining tower 1 is raised to about 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 of the adsorption refining tower 1, the desorption gas is called as desorption gas of the adsorption refining tower 1, the desorption gas, fuel gas and air of the adsorption refining tower 1 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 and is discharged along with flue gas, and the mixture is purified by the flue gas and is discharged after reaching the standard.
Second embodiment
As shown in fig. 4, the preparation method of the reducing gas preparation system of the basic shaft furnace of the present invention comprises the following steps:
step S1: the primarily purified coke oven gas passes through the adsorption refining tower 1 to remove impurities such as tar, benzene, naphthalene, sulfur and the like mixed in the primarily purified coke oven gas so as to form a feed gas.
Further, in step S1, a portion of the primarily purified coke oven gas passes through the adsorption refining tower 1 to form a raw material gas, and another portion of the primarily purified coke oven gas enters the reducing gas reformer 2 to be combusted for heat supply. Wherein the gas amount of the primary purification coke oven entering the adsorption refining tower 1 is 48000Nm3The amount of the primarily purified coke oven gas introduced into the reducing gas reformer 2 is 2000Nm3/h。
In an optional embodiment of the present invention, 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 regeneration, and the desorption gas of 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 0.2MPa by the pressurizing means 5 and preheated to 650 ℃ by the heat recovery means 4.
Step S3: the reducing gas passes through the shaft furnace 6 and performs reduction reaction with the iron ore in the shaft furnace 6 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 6 from an iron ore inlet 603 of the shaft furnace 6;
step S302: the reducing gas flows from bottom to top in the shaft furnace 6 and performs a reduction reaction with the iron ore in the shaft furnace 6 to obtain sponge iron and top gas.
Further, in step S3, the temperature condition for the reduction reaction of the reducing gas and the iron ore is 900 ℃.
Step S4: the top gas is discharged from the shaft furnace 6 and subjected to a desulfurization treatment by the top gas purification apparatus 3 to form a process gas.
Further, as shown in fig. 6, step S4 includes:
step S401: the top gas is discharged from the shaft furnace 6 and enters the heat exchanger 301 to exchange heat with the desorption gas output by the adsorption desulfurization tower 303;
step S402: the top gas after heat exchange enters a scrubber 302 for cooling and dust removal, and the desorption gas after heat exchange in the heat exchanger 301 enters an adsorption desulfurization tower 303 for regeneration;
step S403: the cooled and dedusted top gas enters an adsorption desulfurization tower 303 to remove inorganic sulfur and organic sulfur, and then process gas is formed;
step S404: the desorption gas generated by the adsorption desulfurization tower 303 enters the reducing gas converter 2 along with a part of process gas for combustion and heat supply; the other part of the process gas enters a reducing gas converter 2 to be catalytically converted into reducing gas; and the third part of the process gas is used as desorption gas of the adsorption desulfurization tower 303 and enters the heat exchanger 301 for heat exchange.
Further, in step S404, a part of the process gas generated by the adsorption desulfurization tower 303 is introduced into the adsorption purification tower 1 as desorption gas required by the adsorption purification tower 1 to regenerate the adsorption purification tower 1. The amount of desorbed gas required for desorption and regeneration of the adsorption refining tower 1 is 5000Nm3And heating desorption gas required by the adsorption refining tower 1 to 280 ℃ through a heat recovery device 4.
Step S5: the process gas 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 is mixed with the raw material gas and then passes through the reducing gas converter 2, and the mixed gas of the process gas and the raw material gas generates the reducing gas again under the action of the catalyst in the reducing gas converter 2.
Further, in step S5, a part of the process gas introduced into the reducing gas reformer 2 for combustion needs to be preheated by the heat recovery device 4 to reach 300 ℃.
Further, in step S5, the mixed gas of the other part of the process gas and the raw material gas, which is catalytically reacted by the reducing gas reformer 2, needs to be pressurized to 0.2MPa by the pressurizing device 5 and preheated to 650 ℃ by the heat recovery device 4.
Further, in step S5, the pressure of the reducing gas is 0.08MPa to 0.5MPa, 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 S5, 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 S5, the process gas introduced into the reducing gas reformer 2 for combustion accounts for 30% of the total amount; the process gas introduced into the reducing gas reformer 2 for the reforming reaction accounts for 70% of the total amount.
Step S6: the reducing gas passes through the shaft furnace 6 again and performs reduction reaction with the iron ore in the shaft furnace 6 to obtain sponge iron and top gas.
Further, in step S6, the temperature condition for the reduction reaction of the reducing gas and the iron ore is 900 ℃.
Step S7: and (4) circulating the steps S4 to S6 until the iron ore in the shaft furnace 6 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 603 of the shaft furnace 6, reducing gas reversely flows from bottom to top in the shaft furnace 6 and is subjected to reduction reaction with the iron ore at the temperature of 900 ℃ to obtain sponge iron (Fe) and top gas (rich in H)2CO and CO2Gas). The top gas is discharged from the top gas outlet 601 of the shaft furnace 6, enters the heat exchanger 301, and is desorbed (rich in H) with the desorption gas output from the adsorption desulfurization tower 303 in the heat exchanger 3012CO and CO2Gas) to raise the temperature of desorbed gas output by the adsorption desulfurization tower 303 to 260 ℃, and to regenerate the adsorption desulfurization tower 303. The top gas enters a scrubber 302 for cooling and dedusting after exchanging heat in a heat exchanger 301, then enters an adsorption desulfurization tower 303 for removing hydrogen sulfide and organic sulfur mixed in the top gas, the process gas output after passing through the adsorption desulfurization tower 303 is divided into two parts, one part of the process gas (accounting for 10-50% of the total amount, preferably 30%) is preheated by a heat recovery device 4 until the temperature reaches 300 ℃, and then enters a reducing gas reformer 2 for combustion through a fuel gas inlet 203 of the reducing gas reformer 2 to supply heat for the reducing gas reformer 2; another part of the process gas (50-90%, preferably 70% of the total amount) is pressurized to 0.2MPa by a pressurizing device 5 and passed throughAfter the overheating recovery device 4, preheating the mixture to a temperature of 650 ℃, entering the catalyst tube 205 in the reducing gas converter 2 through the raw gas inlet 201 of the reducing gas converter 2, and carrying out a reforming reaction on the mixed gas of the process gas and the raw gas under the action of the catalyst in the catalyst tube 205 to remove 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 900 ℃,
and is about 1.5 of the total weight of the alloy,
the reducing gas is fed into the shaft furnace 6 through the reducing gas inlet 602 to react with the iron ore in the shaft furnace 6 to produce sponge iron, and the sponge iron with the temperature of 500 ℃ is output from the sponge iron outlet 604 at the lower part of the shaft furnace 6.
Wherein, the number of the adsorption desulfurization tower 303 is 4, and 1 is a standby adsorption desulfurization tower. When the adsorption of the adsorption desulfurization tower 303 reaches a preset saturation threshold, 3000Nm is extracted3The process gas of/h enters a heat exchanger 301, is heated to 260 ℃, and then enters an adsorption desulfurization tower 303 for desorption and regeneration. The regeneration of the adsorption desulfurization tower 303 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-containing compounds and the like adsorbed by the molecular sieve material enter the desorption gas of the adsorption desulfurization tower 303, and the desorption gas of the adsorption desulfurization tower 303 and the process gas are mixed and enter the reducing gas conversion furnace 2 for combustion treatment.
Wherein, the primary purified coke oven gas is 50000Nm3H, total sulfur content 300mg/Nm3Tar content of 20mg/Nm and benzene content of 500mg/Nm3Naphthalene content of 500mg/Nm3One part of the coke oven gas is primarily purified (48000 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 (2000 Nm)3H) to a reducing gas reformer 2The combustion heat supply is carried out.
Wherein, the number of the adsorption refining towers 1 is 6, 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 280 ℃ through a heat recovery device 4, and then the process gas is introduced into an 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 of the adsorption refining tower 1, the desorption gas of the adsorption refining tower 1, 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 for providing 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 gas-based shaft furnace is original gas preparation system's characteristics and advantage are:
firstly, this gas-based shaft furnace reducing gas preparation system adsorbs desorption processing through the impurities such as inorganic sulphur, organic sulphur, tar, benzene and naphthalene in the coke oven gas of the molecular sieve material in the absorption refining tower 1, and the desorption gas after absorption refining tower 1 regeneration can be sent to reducing gas reformer 2 and burn the heat supply as fuel gas, and simple structure, energy utilization is high, and it is few to invest in with low costs, no secondary pollution with traditional purifier.
Secondly, the gas-based shaft furnace reducing gas preparation system is filled with molecular sieve materials in the adsorption desulfurization tower 303, inorganic sulfur and organic sulfur in the top gas of the furnace are adsorbed and removed through the molecular sieve materials, and the desorbed gas heats the converter, so that the desulfurization precision is high, the selectivity is high, and carbon dioxide is not lost.
Thirdly, the gas-based shaft furnace reducing gas preparation system adopts the coke oven gas purified by the adsorption refining tower 1 and the CO generated by the shaft furnace 62Catalytic conversion to H-rich2Reducing CO gas to achieve energy conservation and emission reduction of CO2The effect of (1).
And fourthly, the heat recovery device 4 and the heat exchanger 301 are arranged in the gas-based shaft furnace reducing gas preparation system, the process gas entering the reducing gas converter 2 is preheated, the temperature of the process gas is raised, the reducing gas produced by the reducing gas converter 2 can be directly conveyed to the shaft furnace 6 to carry out reduction reaction with the iron ore, the energy consumption is low, and the flow 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 (15)
1. A gas-based shaft furnace reducing gas preparation system is characterized by comprising an adsorption refining tower (1) for purifying coke oven gas, a reducing gas conversion furnace (2) for converting the purified coke oven gas into reducing gas, and a top gas purification device (3) for purifying top gas discharged from a shaft furnace (6), wherein:
a coke oven gas inlet of the adsorption refining tower (1) is connected with a coke oven gas pipeline, 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), 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 reformer (2) is connected with the reducing gas inlet (602) of the shaft furnace (6), a top gas outlet (601) of the shaft furnace (6) is connected with a top gas inlet of the top gas purification device (3), and a process gas outlet of the furnace top gas purification device (3) is respectively connected with a fuel gas inlet (203) of the reducing gas converter (2), a raw gas inlet (201) of the reducing gas converter (2) and a desorption gas inlet of the adsorption refining tower (1).
2. The gas-based shaft furnace reducing gas production system according to claim 1, wherein the fuel gas inlet (203) of the reducing gas reformer (2) is connected to a coke oven gas pipeline.
3. The gas-based shaft furnace reducing gas production system according to claim 1, wherein the adsorption refining tower (1) is filled with a molecular sieve material that can adsorb impurities contained in coke oven gas and can be desorbed and regenerated after heating.
4. The gas-based shaft furnace reducing gas production system according to claim 3, wherein the number of said adsorption purification tower (1) is plural, and at least one of said adsorption purification towers (1) is a spare adsorption purification tower.
5. The gas-based shaft furnace reducing gas production system according to claim 1, further comprising a heat recovery device (4) for preheating and raising the temperature of the process gas discharged from the top gas purification device (3) and the raw gas discharged from the adsorption refining tower (1), wherein the process gas outlet of the top gas purification device (3) is connected to the fuel gas inlet (203) of the reducing gas conversion furnace (2), the raw gas inlet (201) of the reducing gas conversion furnace (2) and the desorption gas inlet of the adsorption refining tower (1) through the heat recovery device (4), and the raw gas outlet of the adsorption refining tower (1) is connected to the raw gas inlet (201) of the reducing gas conversion furnace (2) through the heat recovery device (4).
6. The gas-based shaft furnace reducing gas production system according to claim 5, wherein the flue gas outlet of the reducing gas reformer (2) is connected to the flue gas inlet of the heat recovery device (4), and the flue gas outlet of the heat recovery device (4) is directly communicated with the outside.
7. The gas-based shaft furnace reducing gas production system according to claim 5, wherein said top gas cleaning device (3) comprises a heat exchanger (301), a scrubber (302) and an adsorption desulfurization tower (303), wherein a gas inlet of said heat exchanger (301) is connected to a top gas outlet (601) of said shaft furnace (6), a gas outlet of said heat exchanger (301) is connected to a gas inlet of said scrubber (302), a gas outlet of said scrubber (302) is connected to a gas inlet of said adsorption desulfurization tower (303), and a gas outlet of said adsorption desulfurization tower (303) is connected to a fuel gas inlet (203) of said reducing gas reformer (2) and a raw gas inlet (201) of said reducing gas reformer (2), respectively;
the air inlet of the heat exchanger (301) is the top gas inlet of the top gas purification device (3), and the air outlet of the adsorption desulfurization tower (303) is the process gas outlet of the top gas purification device (3).
8. The gas-based shaft furnace reducing gas production system according to claim 7, wherein the stripping gas outlet of the adsorption desulfurization tower (303) is connected to the stripping gas inlet of the heat exchanger (301), and the stripping gas outlet of the heat exchanger (301) is connected to the stripping gas inlet of the adsorption desulfurization tower (303).
9. The gas-based shaft furnace reducing gas production system according to claim 7, wherein the desorbed gas outlet of the adsorption desulfurization tower (303) is connected to the fuel gas inlet (203) of the reducing gas converter (2) through the heat recovery device (4).
10. The gas-based shaft furnace reducing gas production system according to claim 7, wherein the adsorption desulfurization tower (303) is internally filled with a molecular sieve material capable of adsorbing organic sulfur and inorganic sulfur contained in the top gas and undergoing desorption regeneration after heating.
11. The gas-based shaft furnace reducing gas production system according to claim 7, wherein the number of said adsorption desulfurization towers (303) is plural, and at least one of said adsorption desulfurization towers (303) is a spare adsorption desulfurization tower.
12. The gas-based shaft furnace reducing gas production system according to claim 1, wherein a pressurizing device (5) for adjusting the gas transmission pressure is provided between the process gas outlet of the top gas cleaning device (3) and the raw gas inlet (201) of the reducing gas reformer (2).
13. The gas-based shaft furnace reducing gas production system according to claim 1, wherein a plurality of catalyst pipes (205) for catalytically reforming the raw gas discharged from the adsorption refining tower (1) and the process gas discharged from the top gas purification device (3) into the reducing gas required for reducing iron ore are provided inside the reducing gas converter (2), and each of the catalyst pipes (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).
14. The gas-based shaft furnace reducing gas production system according to claim 13, wherein said catalyst tube (205) is filled with a nickel-based catalyst.
15. The gas-based shaft furnace reducing gas production system according to claim 1, wherein said top gas outlet (601) is provided at the top of said shaft furnace (6), and an iron ore inlet (603) is provided at the top of said shaft furnace (6) above said top gas outlet (601);
the reducing gas inlet (602) is arranged at the bottom of the shaft furnace (6), and a sponge iron outlet (604) is arranged at the bottom of the shaft furnace (6) and below the reducing gas inlet (602).
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| CN114574648A (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 reducing gas of gas-based shaft furnace |
| CN114574648B (en) * | 2020-12-02 | 2023-10-31 | 北京京诚泽宇能源环保工程技术有限公司 | System and method for preparing reducing gas of gas-based shaft furnace |
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