CN213895741U - Shaft furnace reducing gas preparation and humidification carbon elimination system - Google Patents
Shaft furnace reducing gas preparation and humidification carbon elimination system Download PDFInfo
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- CN213895741U CN213895741U CN202022850782.1U CN202022850782U CN213895741U CN 213895741 U CN213895741 U CN 213895741U CN 202022850782 U CN202022850782 U CN 202022850782U CN 213895741 U CN213895741 U CN 213895741U
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Abstract
The utility model relates to a shaft furnace is original gas preparation and humidification carbon system that disappears, including adsorbing refined tower, original gas reborner and furnace roof gas purifier, the air inlet of adsorbing refined tower and the fuel gas entry of original gas reborner are connected with coke oven gas pipeline respectively, the gas outlet of adsorbing refined tower is connected with the fuel gas entry of original gas reborner and the feed gas entry of original gas reborner respectively, the original gas export of original gas reborner and the original gas entry of shaft furnace are connected, the furnace roof gas export of shaft furnace is connected with furnace roof gas purifier's air inlet, furnace roof gas purifier's gas outlet respectively with the fuel gas entry of original gas reborner and the feed gas entry of original gas reborner be connected, be provided with humidification device between furnace roof gas purifier's gas outlet and the feed gas entry of original gas reborner. 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 shaft furnace is gaseous preparation and humidification carbon elimination system still, especially relate to a coke oven gas preparation shaft furnace is gaseous and humidification carbon elimination system still.
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 iron making 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 (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 shaft furnace reducing gas preparation and humidifying and carbon elimination 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 shaft furnace is gaseous preparation of reducing gas and humidification carbon system that disappears, can adsorb the desorption to the impurity in the coke oven gas, desorption gas after the regeneration can be sent to the reducing gas reborner and burns the heat supply, the coke oven gas after the purification mixes the humidification with the top gas after the purification treatment and handles, and catalytic conversion is the reducing gas that the shaft furnace used, 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 reducing 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 shaft furnace reduction gas preparation and humidification carbon elimination 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 furnace top gas purifier to shaft furnace exhaust furnace top gas, wherein:
the gas inlet of the adsorption refining tower and the fuel gas inlet of the reducing gas converter are respectively connected with a coke oven gas pipeline, the gas outlet of the adsorption refining tower is respectively connected with the fuel gas inlet of the reducing gas converter and the raw material 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 gas inlet of a top gas purification device, the gas outlet of the top gas purification device is respectively connected with the fuel gas inlet of the reducing gas converter and the raw material gas inlet of the reducing gas converter, and a humidifying device is arranged between the gas outlet of the top gas purification device and the raw material gas inlet of the reducing gas converter.
In a preferred embodiment of the present invention, the adsorption refining 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;
and a raw gas outlet of the adsorption refining tower is connected with a raw gas inlet of the reducing gas converter, and a desorption gas outlet of the adsorption refining tower is connected with a fuel gas inlet of the reducing gas converter.
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, shaft furnace reduction gas preparation and humidification carbon removal system still includes preheats the heat recovery unit who heaies up to furnace roof gas purifier exhaust process gas and absorption refining tower exhaust raw gas, furnace roof gas purifier's gas outlet 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 air inlet of the heat exchanger is the air inlet of the furnace top gas purification device, and the air outlet of the adsorption desulfurization tower is the air outlet of the furnace top gas purification device.
In a preferred embodiment of the present invention, the water inlet of the humidifying device is connected to the water outlet of the scrubber.
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 pressure of the gas to be delivered is provided between the gas outlet of the top gas purification device and the raw gas inlet of the reducing gas reformer, and the pressurizing device is connected in series with the humidifying device.
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 above, the utility model discloses a characteristics and advantage of shaft furnace reducing gas preparation and humidification carbon elimination system 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 first desorption gas generated after the regeneration of the adsorption refining tower can be sent to the reducing gas conversion furnace for combustion and heat supply, the purified coke oven gas is mixed with the top gas generated after the purification, and the mixture can be catalytically converted into H-rich gas after the humidification by the humidification device2And 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 a shaft furnace reducing gas preparation and humidifying carbon-removing system.
FIG. 2: is a schematic structural diagram of a furnace top gas purification device in a shaft furnace reducing gas preparation and humidifying carbon-removing system.
FIG. 3: is a schematic structural diagram of a reducing gas converter in a shaft furnace reducing gas preparation and humidifying carbon-removing system.
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 humidifying device;
7. a shaft furnace; 701. A top gas outlet;
702. a reducing gas inlet; 703. An iron ore inlet;
704. 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.
As shown in fig. 1 to 3, the utility model provides a shaft furnace reducing gas preparation and humidification carbon elimination system, this shaft furnace reducing gas preparation and humidification carbon elimination system includes absorption refining tower 1, reducing gas converter 2 and top gas purification device 3, and absorption refining tower 1 is used for carrying out purification treatment to coke oven gas, and reducing gas converter 2 is used for turning into reducing gas with the coke oven gas after purifying, and top gas purification device 3 is used for carrying out purification treatment to the top gas of shaft furnace 7 exhaust. Wherein: the 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 reformer 2 is connected with the coke oven gas pipeline through a first gas transmission pipeline 10, the gas outlet of the adsorption refining tower 1 is respectively connected with the fuel gas inlet 203 of the reducing gas reformer 2 and the raw material gas inlet 201 of the reducing gas reformer 2, the reducing gas outlet 202 of the reducing gas reformer 2 is connected with the reducing gas inlet 702 of the shaft furnace 7 through a fifth gas transmission pipeline 14, the top gas outlet 701 of the shaft furnace 7 is connected with the gas inlet of the top gas purification device 3, the gas outlet of the top gas purification device 3 is respectively connected with the fuel gas inlet 203 of the reducing gas reformer 2 and the raw material gas inlet 201 of the reducing gas reformer 2, and a humidification device 6 is arranged between the gas outlet of the top gas purification device 3 and the raw material gas inlet 201 of the reducing gas reformer 2.
The utility model discloses an adsorb refining tower 1 and carry out purification treatment to coke oven gas, reach the effect that inorganic sulphur in the coke oven gas, organic sulphur, tar, impurity such as benzene and naphthalene adsorbed the desorption, adsorb first desorption gas after refining tower 1 regeneration and can send to reduction gas reborner 2 and burn the heat supply, coke oven gas after the purification mixes with the top gas after the purification treatment, and carry out the humidification processing back through humidification device 6, can catalytic conversion become rich H2And CO, eliminating the reducing gas reformer 2Carbon deposition is carried out, the carbon content of sponge iron in the shaft furnace 7 is adjusted, and the sponge iron can be used for carrying out reduction reaction with iron ore in the shaft furnace 7, so that the problems of more impurities and difficult purification in coke oven gas are solved, and the purposes of saving energy and reducing emission of CO are achieved2The method is beneficial to reasonable configuration of resources and protection of the environment.
Specifically, as shown in fig. 1, a top gas outlet 701 is provided at the top of the shaft furnace 7, and an iron ore inlet 703 is provided at the top of the shaft furnace 7 and above the top gas outlet 701; a reducing gas inlet 702 is provided at the bottom of the shaft furnace 7, and a sponge iron outlet 704 is provided at the bottom of the shaft furnace 7 below the reducing gas inlet 702.
Further, in the reducing gas in the fifth gas transmission pipeline 14
Greater than 10 in reducing gas
Preferably, in a reducing gas
Is 1 to 3.
Furthermore, the inside of the adsorption refining tower 1 is filled with a molecular sieve material which can adsorb impurities (inorganic sulfur, organic sulfur, tar, benzene, naphthalene and the like) contained in coke oven gas and can be desorbed and regenerated after being heated; the raw gas outlet of the adsorption refining tower 1 is connected with the raw gas inlet 201 of the reducing gas converter 2, and the desorption gas outlet of the adsorption refining tower 1 is connected with the fuel gas inlet 203 of the reducing gas converter 2.
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 present invention, as shown in fig. 1, the shaft furnace reducing gas preparation and humidification carbon-elimination 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 gas outlet of the furnace top gas purification device 3 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 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 to 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 optional embodiment of the present invention, as shown in fig. 1, a pressurizing device 5 is disposed between the gas outlet of the top gas purifying device 3 and the raw gas inlet 201 of the reducing gas reformer 2, the pressurizing device 5 and the humidifying device 6 are connected in series and disposed between the gas outlet of the top gas purifying device 3 and the raw gas inlet 201 of the reducing gas reformer 2, the pressure of the gas is adjusted by the pressurizing device 5, and the process gas and the raw gas are pressurized and then delivered to the raw gas inlet 201 of the reducing gas reformer 2. In addition, the moisture in the gas is adjusted through the humidifying device 6, carbon deposition generated in the reducing gas converter 2 is eliminated, and the carbon content of the sponge iron in the shaft furnace 7 is adjusted.
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 701 of the shaft furnace 7 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 and the humidifying device 6 are connected in series on the seventh gas transmission pipeline 16. Wherein, the air inlet of the heat exchanger 301 is the air inlet of the top gas purification device 3, and the air outlet of the adsorption desulfurization tower 303 is the air 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 an eighth gas transmission pipeline 17 through a fourth gas transmission pipeline 13, and the first desorbed gas desorbed from the adsorption refining tower 1 is sequentially transmitted to the reducing gas converter 2 through the fourth gas transmission pipeline 13 and the eighth gas transmission pipeline 17 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 the first desorption gas to be conveyed into the adsorption refining tower 1 for desorption and regeneration of the adsorption refining tower 1, and the desorbed first desorption gas is directly conveyed into the reducing gas converter 2 for combustion and heat supply.
In an optional embodiment of the utility model, the water inlet of humidification device 6 is connected with the delivery port of scrubber 302, and humidification device 6's inside is provided with packs and shower nozzle, can provide 50 ℃ to 80 ℃ of water for humidification device 6 through scrubber 302 to satisfy the humidification demand to the feed gas and process gas.
Furthermore, the filler in the humidifying device 6 can be a water-absorbing filler or a non-water-absorbing filler, wherein the water-absorbing filler gradually evaporates in the air flow after absorbing water so as to achieve the humidifying effect; the non-water-absorbing filler is controlled by water flow, and a layer of water film is formed on the surface of the non-water-absorbing filler and gradually evaporated in air flow, so that the humidifying effect is achieved.
Further, the humidifying device 6 may be, but is not limited to, a humidifier.
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 the second desorption gas generated by the adsorption desulfurization tower 303 is preheated by the heat recovery device 4, and then introduced into the reducing gas reformer 2 for combustion and heat supply.
Further, the inside of 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 being heated.
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 device 3 are catalytically reformed into the reducing gas required for reducing 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 basic operating principle does: the iron ore is fed into the shaft furnace 7 from the iron ore inlet 703 of the shaft furnace 7, the reducing gas flows from the bottom to the top in the shaft furnace 7, and the reducing gas (rich in H) is introduced into the shaft furnace 72And 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 701 of the shaft furnace 7, firstly enters the heat exchanger 301, and then is mixed with the second desorption gas (rich in H) output by the adsorption desulfurization tower 3032CO and CO2Gas) is subjected to heat exchange, 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 of the adsorption desulfurization tower 303 after being purified by the adsorption desulfurization tower 303 is divided into two parts, and one part of the process gas is conveyed to the heat recovery device 4 for preheating and heating to about 300 ℃ and then is output by the adsorption desulfurization tower 303The desorption gas and the primary purified coke oven gas (namely, fuel gas) which does not pass through the adsorption refining tower 1 are mixed and enter the reducing gas converter 2 to be used as fuel for the combustion and the temperature rise of the reducing gas converter 2; the other part of the process gas is mixed with the raw material gas purified by the adsorption refining tower 1, the mixture is pressurized to 0.1MPa to 0.5MPa by a pressurizing device 5, enters a humidifying device 6 for humidifying, is preheated to 500 ℃ to 700 ℃ by a heat recovery device 4 and is conveyed to the reducing gas conversion furnace 2, the mixed gas of the process gas and the raw material gas generates catalytic reforming reaction in a catalyst pipe 205 in the reducing gas conversion furnace 2, and CH in the raw material gas4And CO2CO in process gas2And increased water vapor (i.e., H)2O) as raw material gas to generate CO and H2(chemical formula of reaction: CH)4+CO2＝2CO+2H2、CH4+H2O＝CO+3H2) Since the catalytic reforming reaction is endothermic, the heat required is derived from the combustion of part of the process gas, fuel gas and first desorbed gas. Finally, the reaction is carried out to produce H-rich2And CO as a reducing gas is fed into the shaft furnace 7 through a reducing gas inlet 702.
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) The coke oven gas enters an adsorption refining tower 1, impurities such as inorganic sulfur, organic sulfur, tar, benzene and naphthalene in the coke oven gas are adsorbed and removed, and the purified coke oven gas (namely: raw gas) is mixed with the process gas, pressurized by the pressurizing device 5 and conveyed into the reducing gas reformer 2. When the adsorption refining tower 1 reaches a preset saturation threshold value, extracting 4000Nm3The process gas is used as a first desorption gas, the first desorption gas exchanges heat with the high-temperature flue gas through the heat recovery device 4 until the temperature of the first desorption gas is raised to about 260 ℃, and the molecular sieve in the adsorption refining tower 1 is adsorbedRegenerating the material, wherein 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 first desorption gas, namely first desorption gas, the first desorption gas, fuel gas and air in 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, the carbon dioxide, the organic sulfur and the inorganic sulfur are 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.
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 703 of the shaft furnace 7, reducing gas reversely flows from bottom to top in the shaft furnace 7 and is subjected to reduction reaction with the iron ore at the temperature of 950 ℃ to obtain sponge iron (Fe) and top gas (rich in H)2CO and CO2Gas). The top gas is discharged from a top gas outlet 701 of the shaft furnace 7, enters the heat exchanger 301, and is mixed with the second desorption gas (rich in H) output from the adsorption desulfurization tower 303 in the heat exchanger 3012CO and CO2Gas) to raise the temperature of the second desorbed gas to 260 ℃, and the adsorption desulfurization tower 303 is regenerated. 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 35%) 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; the other part of the process gas (accounting for 50 to 90 percent of the total amount, preferably 65 percent of the total amount) is pressurized to 0.3MPa by a pressurizing device 5, and is preheated to the temperature of 650 ℃ after sequentially passing through a humidifying device 6 and a heat recovery device 4, the other part of the process gas enters a catalyst tube 205 in the reducing gas conversion furnace 2 through a raw material gas inlet 201 of the reducing gas conversion furnace 2, the mixed gas of the process gas and the raw material gas is subjected to reforming reaction under the action of a catalyst in the catalyst tube 205, and CH is removed4、CO2And H2Reforming of O 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 950 ℃,
and is about 2.0 of the total weight of the alloy,
reducing gas is delivered into the shaft furnace 7 through a reducing gas inlet 702 to react with iron ore in the shaft furnace 7 to produce sponge iron, and the sponge iron with the temperature of 500 ℃ is output from a sponge iron outlet 704 at the lower part of the shaft furnace 7.
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 second desorption gas, and the second desorption gas 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/Nm3Part of the coke oven gas is primarily purified (47500 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 (2500 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 6, and 1 is a standby adsorption refining tower. When the adsorption of the adsorption refining tower 1 reaches a preset saturation threshold, extracting 4000Nm3The temperature of the process gas is raised to 280 ℃ through a heat recovery device 4, and the process gas is introduced into an adsorption refining tower 1 for desorptionAnd (4) performing 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 the first 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 shaft furnace is original gas preparation and humidification carbon system that disappears's characteristics and advantage are:
firstly, the shaft furnace reducing gas preparation and humidifying carbon elimination system 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 first 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 shaft furnace reducing gas preparation and humidifying carbon elimination system is simple in structure, high in energy utilization rate, less in investment compared with a traditional purification device, low in cost and free of secondary pollution.
Secondly, the shaft furnace reducing gas preparation and humidifying and carbon elimination 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 removed through adsorption of the molecular sieve materials, and the desorbed gas heats the converter, so that the shaft furnace reducing gas preparation and humidifying and carbon elimination system is high in desulfurization precision, high in selectivity and free of carbon dioxide loss.
Thirdly, the shaft furnace reducing gas preparation and humidifying and carbon elimination system humidifies the purified coke oven gas and the purified top gas (namely, the process gas) by a humidifying device 6 (namely, H is added into the purified coke oven gas and the purified top gas)2O), can react with coke oven gas and CO2Conversion to H-rich by reaction2Reducing gas of CO, eliminating carbon deposition in the reducing gas converter 2, thereby being used for carrying out reduction reaction with iron ore in the shaft furnace 7, adjusting the carbon content of sponge iron in the shaft furnace 7, achieving the purposes of saving energy and reducing emission of CO2The reducing gas component is adjustable.
And fourthly, the shaft furnace reducing gas preparation and humidifying and carbon elimination system is internally provided with a heat recovery device 4 and a heat exchanger 301, 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 7 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 (15)
1. A shaft furnace reducing gas preparation and humidification carbon elimination 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 (7), wherein:
the gas inlet of the adsorption refining tower (1) and the fuel gas inlet (203) of the reducing gas conversion furnace (2) are respectively connected with a coke oven gas pipeline, the gas outlet of the adsorption refining tower (1) is respectively connected with the fuel gas inlet (203) of the reducing gas conversion furnace (2) and the raw gas inlet (201) of the reducing gas conversion furnace (2), the reducing gas outlet (202) of the reducing gas conversion furnace (2) is connected with the reducing gas inlet (702) of the shaft furnace (7), the top gas outlet (701) of the shaft furnace (7) is connected with the gas inlet of the top gas purification device (3), the gas outlet of the top gas purification device (3) is respectively connected with the fuel gas inlet (203) of the reducing gas conversion furnace (2) and the raw gas inlet (201) of the reducing gas conversion furnace (2), and the gas outlet of the top gas purification device (3) is arranged between the raw gas inlet (201) of the reducing gas conversion furnace (2) A humidifying device (6).
2. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 1, characterized in that the interior of the adsorption and refining tower (1) is filled with a molecular sieve material which can adsorb impurities contained in coke oven gas and can be desorbed and regenerated after being heated;
the raw gas outlet of the adsorption refining tower (1) is connected with the raw gas inlet (201) of the reducing gas converter (2), and the desorption gas outlet of the adsorption refining tower (1) is connected with the fuel gas inlet (203) of the reducing gas converter (2).
3. The shaft furnace reducing gas producing and humidifying and decarbonizing system according to claim 2, characterized in that the number of the adsorption refining tower (1) is plural, and at least one of the adsorption refining towers (1) is a spare adsorption refining tower.
4. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 2, characterized in that the shaft furnace reducing gas preparation and humidification and decarbonization system further comprises a heat recovery device (4) for preheating and heating the process gas discharged from the top gas purification device (3) and the raw gas discharged from the adsorption refining tower (1), wherein the gas outlet of the top gas purification device (3) is connected with 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 with the raw gas inlet (201) of the reducing gas conversion furnace (2) through the heat recovery device (4).
5. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 4, 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 (4), and the flue gas outlet of the heat recovery device (4) is directly communicated with the outside.
6. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 4, characterized in that the top gas purification device (3) comprises a heat exchanger (301), a scrubber (302) and an adsorption desulfurization tower (303), wherein a gas inlet of the heat exchanger (301) is connected with a top gas outlet (701) of the shaft furnace (7), a gas outlet of the heat exchanger (301) is connected with a gas inlet of the scrubber (302), a gas outlet of the scrubber (302) is connected with a gas inlet of the adsorption desulfurization tower (303), and a gas outlet of the adsorption desulfurization tower (303) is respectively connected with a fuel gas inlet (203) of the reducing gas converter (2) and a raw gas inlet (201) of the reducing gas converter (2);
the air inlet of the heat exchanger (301) is the air inlet of the furnace top gas purification device (3), and the air outlet of the adsorption desulfurization tower (303) is the air outlet of the furnace top gas purification device (3).
7. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 6, characterized in that the water inlet of the humidifying device (6) is connected with the water outlet of the scrubber (302).
8. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 6, characterized in that a desorption gas outlet of the adsorption desulfurization tower (303) is connected with a desorption gas inlet of the heat exchanger (301), and a desorption gas outlet of the heat exchanger (301) is connected with a desorption gas inlet of the adsorption desulfurization tower (303).
9. The shaft furnace reducing gas producing and humidifying decarbonizing system according to claim 6, characterized in that the desorbed gas outlet of the adsorption desulfurization tower (303) is connected with the fuel gas inlet (203) of the reducing gas converter (2) through the heat recovery device (4).
10. The shaft furnace reducing gas producing and humidifying decarbonizing system according to claim 6, characterized in that the interior of the adsorption desulfurization tower (303) is filled with a molecular sieve material which can adsorb organic sulfur and inorganic sulfur contained in the top gas and can be desorbed and regenerated after being heated.
11. The shaft furnace reducing gas producing and humidifying and decarbonizing system according to claim 6, wherein 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.
12. The reduction gas preparation and humidification and decarbonization system of the shaft furnace according to claim 1, characterized in that a pressurizing device (5) for adjusting the gas transmission pressure is arranged between the gas outlet of the top gas purification device (3) and the raw gas inlet (201) of the reduction gas converter (2), and the pressurizing device (5) and the humidifying device (6) are arranged in series.
13. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 1, characterized in that a plurality of catalyst tubes (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 arranged inside the reducing gas converter (2), and each catalyst tube (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 shaft furnace reducing gas producing and humidifying decarbonizing system according to claim 13, characterized in that the catalyst tube (205) is filled with a nickel-based catalyst.
15. The shaft furnace reducing gas preparation and humidification and decarbonization system according to claim 1, characterized in that the top gas outlet (701) is arranged at the top of the shaft furnace (7), and an iron ore inlet (703) is arranged at the top of the shaft furnace (7) and above the top gas outlet (701);
the reducing gas inlet (702) is arranged at the bottom of the shaft furnace (7), and a sponge iron outlet (704) is arranged at the bottom of the shaft furnace (7) and below the reducing gas inlet (702).
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