CN218853934U - Carbon dioxide adjustable system for preparing reducing gas of shaft furnace by coke oven gas - Google Patents
Carbon dioxide adjustable system for preparing reducing gas of shaft furnace by coke oven gas Download PDFInfo
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- CN218853934U CN218853934U CN202223598997.4U CN202223598997U CN218853934U CN 218853934 U CN218853934 U CN 218853934U CN 202223598997 U CN202223598997 U CN 202223598997U CN 218853934 U CN218853934 U CN 218853934U
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Abstract
The utility model discloses a coke oven gas preparation shaft furnace is carbon dioxide adjustable system of reducing gas, it includes: a shaft furnace having a top gas outlet and a reducing gas inlet; the furnace top gas treatment unit comprises a first heat exchanger, a scrubber and a desulfurization and decarburization device which are sequentially connected, wherein the first heat exchanger is connected with a furnace top gas outlet; coke oven gas processing unitComprises an adsorption refining device; a reducing gas generation unit comprising a first generation line and a second line; wherein the first generation pipeline is provided with a first pressurizing device, a first heat exchanger and a reforming furnace, the reforming furnace is connected with a reducing gas inlet, and the first pressurizing device is connected with the adsorption refining device; one end of the second pipeline is connected with the desulfurization and decarburization device of the top gas treatment unit, and the other end is connected with the reducing gas inlet. The utility model solves the problems that the top gas can not be directly used as the reducing gas, the operation temperature of the reforming furnace is lower, and the CO in the raw material gas in the reforming furnace is low 2 The problem of non-adjustability.
Description
Technical Field
The utility model relates to a ferrous metallurgy technical field especially relates to a coke oven gas preparation shaft furnace is carbon dioxide adjustable system of reducing gas.
Background
The steel and iron industry is the third CO in China 2 The emission industry accounts for about 15% of the total carbon emission in China, and the emission reduction pressure is huge. In the long process (blast furnace + converter process), blast furnace ironmaking accounts for 67.02% of the total emission of the long process. Is accompanied by SO X 、NO X And the generation of harmful pollutants such as dioxin. The hydrogen-based shaft furnace adopts hydrogen-rich reduction to mainly generate water, has no pollution and reduces emission of CO 2 The amplitude is large. The Direct Reduction Iron (also called 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, and the technology mainly uses natural gas as a raw material and converts the natural gas into H-rich iron 2 And after the gas of CO and the iron ore are mixed, the solid reduction is directly carried out on the gas and the iron ore under the high-temperature condition to produce the sponge iron. The method for preparing the hydrogen-rich gas by using the coke oven gas not only solves the problems of gas emission and utilization, but also provides a method for obtaining the hydrogen-rich reducing gas for producing the direct reduced iron at the present stage。
In general, the Midrex process, the hill process (HYL process), is an absolute advantage of the gas-based shaft furnace process. With the development of the technology, the requirement on the reducing gas is more extensive, namely the requirement phi (H) 2+ CO)/φ(CO 2 +H 2 O) is greater than 10, phi (H) 2 ) The pressure is more than 0.3 and 0.1 to 0.90MPa. Because the coke oven gas contains H 2 S、CS 2 、COS、NH 3 And impurities such as BTX (benzene, toluene, xylene, etc.), tar and naphthalene, 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.
The current gas-based shaft furnace process is limited by the materials of a heating furnace and a reforming furnace, so that the pressure of main equipment is lower, the operating temperature of the reforming furnace is relatively lower, and CO in raw material gas in the process is 2 Is not adjustable.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a coke oven gas preparation shaft furnace is carbon dioxide adjustable system of reducing gas solves the furnace roof gas and can not directly be reducing gas to and reformer operating temperature is lower and in it CO in the raw material gas 2 The problem of non-adjustability.
The above implementation objective of the present invention is mainly realized by the following technical solutions:
a carbon dioxide adjustable system for preparing reducing gas of a shaft furnace from coke oven gas comprises:
a shaft furnace having a top gas outlet and a reducing gas inlet;
the furnace top gas treatment unit comprises a first heat exchanger, a scrubber and a desulfurization and decarburization device which are sequentially connected, wherein the first heat exchanger is connected with the furnace top gas outlet;
the coke oven gas treatment unit comprises an adsorption refining device for treating the coke oven gas;
a reducing gas generating unit comprising a first generating line and a second line; wherein the first production line has a first pressurizing device, the first heat exchanger, and a reformer, an outlet of the reformer is connected to the reducing gas inlet, and an inlet of the first pressurizing device is connected to an outlet of the adsorption refining device; one end of the second pipeline is connected with an outlet of the desulfurization and decarburization device of the top gas treatment unit, and the other end of the second pipeline is connected with the reducing gas inlet.
In a preferred embodiment of the present invention, the reducing gas generating unit further includes a carbon dioxide injection line connected between an outlet of the desulfurization and decarbonization apparatus and an inlet of the first heat exchanger of the reducing gas generating unit.
In a preferred embodiment of the present invention, the top gas treatment unit further comprises a second heat exchanger connected between the first heat exchanger and the scrubber.
In a preferred embodiment of the present invention, the outlet of the adsorption refining device is connected to the inlet of the second heat exchanger, and the outlet of the second heat exchanger is connected to the inlet of the adsorption refining device.
In a preferred embodiment of the present invention, the top gas treatment unit further comprises a second pressurizing device connected between the scrubber and the desulfurization and decarbonization device.
In a preferred embodiment of the present invention, the outlet of the top gas treatment unit of the desulfurization and decarburization device is further connected with a process gas output pipeline for delivering the process gas to a gas user.
In a preferred embodiment of the present invention, the inlet of the first heat exchanger is connected to a steam inlet pipe, and the outlet of the first pressurizing device is connected to the steam inlet pipe.
In a preferred embodiment of the present invention, the reforming furnace includes a furnace body, an oxygen inlet and a coke oven gas inlet are provided at an upper portion of the furnace body, the oxygen inlet is connected to an oxygen inlet pipe, and the coke oven gas inlet is connected to an outlet of the first heat exchanger; the lower part of the furnace body is provided with a reducing gas outlet which is connected with the reducing gas inlet.
In a preferred embodiment of the present invention, a catalyst layer is disposed inside the furnace body, and the catalyst in the catalyst layer is a nickel-based catalyst or a carbon-based catalyst.
In a preferred embodiment of the present invention, the operating pressure of the reformer is 0.1MPa to 3.0MPa, and the operating temperature thereof is 800 ℃ to 1100 ℃.
In a preferred embodiment of the present invention, the pressure of the reducing gas injected into the reducing gas inlet is 0.08MPa to 2.0MPa, and the temperature of the reducing gas is 850 ℃ to 1100 ℃.
In a preferred embodiment of the present invention, the adsorption purification apparatus is filled with a hydrophobic adsorption material.
In a preferred embodiment of the present invention, the hydrophobic adsorption material is a molecular sieve material having an adsorption capacity at 20 ℃ to 100 ℃ and capable of desorption regeneration at 160 ℃ to 350 ℃.
Compared with the prior art, technical scheme have following characteristics and advantage:
1. the utility model discloses a coke oven gas preparation shaft furnace carbon dioxide adjustable system of reducing gas adopts molecular sieve absorption desorption coke oven gas sulphur and BTX, and desorption gas utilizes the heating of furnace roof gas, and the device is simple, and energy utilization is high, and investment is low compared with traditional purification method, and is with low costs, no secondary pollution;
2. the utility model discloses a coke oven gas preparation shaft furnace carbon dioxide adjustable system of reducing gas, adopt the reforming furnace, the furnace body can adopt refractory material, can operate under higher pressure and temperature, compare with traditional shell and tube reforming furnace and do not have the material restriction, whole equipment is small, invests in lowly;
3. the utility model discloses a coke oven gas preparation shaft furnace is carbon dioxide adjustable system of reducing gas adopts coke oven gas and carbon dioxide catalytic conversion to richly contain H 2 Reduction of CO, reduction of CO 2 The discharge amount of (c);
4. the utility model discloses a carbon dioxide adjustable system of coke oven gas preparation shaft furnace reducing gas directly does reducing gas after the furnace crown gas desulfurization decarbonization, reduces the reforming furnace load, and the investment reduces, and reducing gas component is adjustable.
5. The utility model discloses a coke oven gas preparation shaft furnace is carbon dioxide adjustable system of reducing gas, adds CO in a flexible way to the reformer through desulfurization decarbonization device 2 Carbon deposition of the catalyst can be inhibited; meanwhile, the reforming furnace can operate at high temperature, and the reaction rate is high.
Drawings
In order to illustrate the embodiments of the present invention or the technical solutions in the prior art more clearly, the drawings used in the description of the embodiments or the prior art will be briefly introduced, obviously, the drawings in the description below are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts. In the drawings:
FIG. 1 is a schematic view of the structural connection of a carbon dioxide adjustable system for preparing reducing gas of a shaft furnace from coke oven gas according to the present invention;
FIG. 2 is a schematic structural diagram of the desulfurization and decarbonization device of the present invention.
The reference numbers illustrate:
10. a shaft furnace; 11. a top gas outlet; 12. a reducing gas inlet; 20. a top gas processing unit; 21. a first heat exchanger; 22. a second heat exchanger; 23. a washer; 24. a second pressurizing device; 25. a desulfurization and decarburization device; 251. an absorption tower; 252. a stripping column; 253. a third heat exchanger; 30. a coke oven gas processing unit; 31. an adsorption refining device; 40. a reducing gas generation unit; 41. a first production pipeline; 411. a reforming furnace; 412. a furnace body; 413. an oxygen inlet; 414. a coke oven gas inlet; 415. a reducing gas outlet; 416. a catalyst layer; 42. a second pipeline; 43. a carbon dioxide injection line; 44. a first pressurizing device; 50. a process gas output pipeline; 60. steam enters the pipeline; 70. oxygen enters the pipeline; A. top gas of the furnace; B. process gas; C. coke oven gas; D. carbon dioxide; E. reducing gas; F. water vapor; G. oxygen gas; H. desorbing gas; I. and (4) desorbing the gas.
Detailed Description
In order to make the technical solutions in the present invention better understood, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, but not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person of ordinary skill in the art without creative efforts shall fall within the protection scope of the present invention.
It will be understood that when an element is referred to as being "disposed on" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. As used herein, the terms "vertical," "horizontal," "left," "right," and the like are for purposes of illustration only and do not denote a single embodiment.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.
The above implementation objective of the present invention is mainly realized by the following technical solutions:
a carbon dioxide adjustable system for preparing reducing gas of a shaft furnace by coke oven gas is shown in figure 1 and comprises:
a shaft furnace 10 having a top gas outlet 11 and a reducing gas inlet 12;
the top gas treatment unit 20 comprises a first heat exchanger 21, a scrubber 23 and a desulfurization and decarburization device 25 which are connected in sequence, wherein the first heat exchanger 21 is connected with the top gas outlet 11;
a coke oven gas treatment unit 30 including an adsorption purification device 31 for treating the coke oven gas C;
a reducing gas generating unit 40 including a first generating line 41 and a second line 42; wherein the first production line 41 has a first pressurizing device 44, a first heat exchanger 21, and a reforming furnace 411, an outlet of the reforming furnace 411 is connected to the reducing gas inlet 12, and an inlet of the first pressurizing device 44 is connected to an outlet of the adsorption refining device 31; one end of the second line 42 is connected to the outlet of the desulfurization and decarbonization apparatus 25 of the top gas treatment unit 20, and the other end of the second line 42 is connected to the reducing gas inlet 12.
The utility model discloses a consecutive top gas processing unit 20, coke oven gas processing unit 30 and reduction gas generation unit 40, with the top gas A and the coke oven gas C of the shaft furnace 10 through handling catalytic conversion in reforming furnace 411 into reduction gas E, but have simple process, high-pressure operation, equipment are small, energy-conserving, CO 2 Low emission and the like; meanwhile, the top gas A is directly used as reducing gas E after passing through the desulfurization and decarburization device 25, so that the load of the reforming furnace 411 is reduced, and the investment is low.
Specifically, as shown in fig. 1, iron ore enters from the top of a shaft furnace 10, a reducing gas inlet 12 is arranged at the lower part of the shaft furnace 10, reducing gas E enters into the shaft furnace 10 through the reducing gas inlet 12, the reducing gas E flows from bottom to top in the shaft furnace 10 and performs a reduction reaction with the iron ore to obtain direct reduced iron and top gas a, the direct reduced iron enters the bottom of the shaft furnace 10, and the top gas a flows out of the shaft furnace 10 through a top gas outlet 11 arranged at the upper part of the shaft furnace 10 and enters into a top gas processing unit 20.
The top gas treatment unit 20 is mainly used for performing heat exchange treatment, impurity removal treatment and desulfurization treatment on top gas a generated by the shaft furnace 10, and the top gas a is subjected to the treatment to generate process gas B capable of being primarily utilized. The top gas treatment unit 20 comprises a first heat exchanger 21, a scrubber 23 and a desulfurization and decarburization device 25 which are connected in sequence, the first heat exchanger 21 is connected with the top gas outlet 11 of the shaft furnace 10, the top gas A is firstly cooled by the first heat exchanger 21 to cool the furnaceThe residual heat of the top gas A is recovered, and then enters a scrubber 23 for dust removal treatment, and then enters a desulfurization and decarbonization device 25 for organic sulfur, inorganic sulfur and CO 2 Removing; in this embodiment, as shown in fig. 2, the desulfurization and decarbonization device 25 is an MDEA desulfurization and decarbonization device, the top gas a is pressurized by the second pressurization device 24 and then sent to the absorption tower 251, the top gas a flows from bottom to top in the absorption tower 251, the MDEA solution flows from top to bottom, and the MDEA solution absorbs CO in the top gas a 2 And sulfur, absorb CO 2 The MDEA solution after sulfur mixing is a rich solution, the rich solution flows out from the bottom of the absorption tower 251, exchanges heat with the lean solution through a third heat exchanger 253, and the rich solution is heated and then sent to the top of the stripping tower 252. The bottom of the stripper 252 is heated by steam to remove CO from the MDEA solution 2 And sulfur, etc. to generate acid gas, which moves relative to the rich liquid to remove CO from the rich liquid 2 The gas such as hydrogen sulfide is stripped and removed, the acid gas is discharged from the top of the stripping tower 252, and CO in the acid gas is removed 2 Separated and mixed with the coke oven gas C to be used as the feed gas of the reforming furnace 411. Removal of CO 2 The MDEA solution of sulfur is called lean solution, the lean solution is cooled by a third heat exchanger 253, the cooled lean solution is sent to the top of an absorption tower 251, and CO in the top gas A of the absorption tower is absorbed 2 And sulfur.
The coke oven gas treatment unit 30 mainly performs adsorption refining treatment on the impurities in the primarily purified coke oven gas C, and in this embodiment, the adsorption refining device 31 mainly performs adsorption treatment on the primarily purified coke oven gas C, and the adsorption refining device 31 can adsorb and remove the impurities such as inorganic sulfur, organic sulfur, tar, benzene, naphthalene, and the like in the coke oven gas C. In this embodiment, at least 2 adsorption purification devices 31 are provided, and at least 1 adsorption purification device is provided, and the packing material for adsorbing coke oven gas C in the adsorption purification device 31 may be a molecular sieve, preferably a hydrophobic material. The coke oven gas C passed through the adsorption refining device 31 enters the first pressurizing device 44 in the reducing gas generating unit 40.
The reducing gas generating unit 40 is mainly used for processing the refined coke oven gas C generated by the coke oven gas processing unit 30 to generate the reducing gas E. Specifically, as shown in FIG. 1, in the first production line 41, a coke ovenThe outlet of the adsorption refining device 31 in the gas treatment unit 30 is connected to the inlet of the first pressurizing device 44 in the reducing gas generation unit 40, and the coke oven gas C is pressurized to 0.1MPa to 2.0MPa in the first pressurizing device 44; pressurizing the coke oven gas C, then entering a first heat exchanger 21 through a pipeline, and performing heat exchange treatment on the coke oven gas C and the top gas A in the first heat exchanger 21, wherein the temperature of the coke oven gas C after heat exchange is more than 300 ℃; the coke oven gas C enters the reforming furnace 411 after passing through the first heat exchanger 21, the coke oven gas C is mixed with oxygen G at the inlet of the reforming furnace 411 to generate partial oxidation reaction, and CH in the coke oven gas C 4 、H 2 CO and high molecular hydrocarbon are subjected to partial oxidation reaction with oxygen G to release a large amount of heat; cracking of macromolecular hydrocarbons to CO and H 2 ，CH 4 、CO、H 2 With oxygen G to form H 2 O、CO 2 Etc., partial oxidation of the product with unreacted CH 4 、CO 2 Is catalytically reformed into CO and H in the lower part of the reformer 411 2 (ii) a The catalytic reforming reaction is an endothermic reaction, and the heat required is derived from the heat evolved by the upper partial oxidation. Enriched in H after catalytic reforming in reformer 411 2 And CO as a reducing gas E, into the shaft furnace 10. In the second pipeline 42, the outlet of the desulfurization and decarbonization device 25 in the top gas treatment unit 20 is connected to the reducing gas inlet 12 of the shaft furnace 10 by a pipeline, and the process gas B generated by the desulfurization and decarbonization device 25 can be directly used as the reducing gas E to be mixed with the reducing gas E generated by the reducing gas generation unit 40 and then enter the reducing gas inlet 12 of the shaft furnace 10.
In one possible embodiment of the present invention, the reducing gas generating unit 40 further includes a carbon dioxide injection line 43, and the carbon dioxide injection line 43 is connected between the outlet of the desulfurization and decarbonization apparatus 25 and the inlet of the first heat exchanger 21 of the reducing gas generating unit 40.
Introducing CO into the first generation line 41 of the reducing gas generation unit 40 through the carbon dioxide outlet of the desulfurization and decarbonization device 25 2 Further regulate CO entering the reforming furnace 411 2 The ratio (c) is favorable for the catalytic reforming reaction inside the reformer 411.
Concretely, it isAs shown in FIG. 1, a carbon dioxide injection line 43 has one end connected to the carbon dioxide outlet of the desulfurization and decarbonization apparatus 25 and the other end connected to a line between the first pressurizing apparatus 44 and the first heat exchanger 21 in the first production line 41, thereby supplying CO produced by the desulfurization and decarbonization apparatus 25 2 Into the first production line 41.
In a possible embodiment of the present invention, the top gas treatment unit 20 further comprises a second heat exchanger 22, the second heat exchanger 22 being connected between the first heat exchanger 21 and the scrubber 23. Further, the outlet of the adsorption refining device 31 is connected with the inlet of the second heat exchanger 22, and the outlet of the second heat exchanger 22 is connected with the inlet of the adsorption refining device 31.
The utility model discloses a second heat exchanger 22 and at second heat exchanger 22 and the connecting line between absorption refining plant 31 mainly used adsorb the regeneration to the adsorbent in the absorption refining plant 31.
Specifically, as shown in fig. 1, the outlet of the adsorption purification device 31 is connected to the inlet of the second heat exchanger 22, the outlet of the second heat exchanger 22 is connected to the inlet of the adsorption purification device 31, and 2000 Nm/min is extracted after the adsorption purification device 31 reaches a certain saturation level 3 /h～6000Nm 3 The purified coke oven gas C is used as desorption gas H, the desorption gas H enters the second heat exchanger 22 through a pipeline to exchange heat with the top gas A, the temperature of the desorption gas H after heat exchange is raised to about 260 ℃, the desorption gas H after temperature rise enters the adsorption refining device 31 through a pipeline to regenerate the adsorbent, the regeneration is divided into three stages of temperature rise, heat preservation and cold blowing, and the regeneration period is about 60 hours; during regeneration, impurities adsorbed by the adsorbent in the adsorption refining device 31 are desorbed into desorption gas H, the desorption gas H after component change is called desorption gas I, organic sulfur is converted into inorganic sulfur and enters the desorption gas I during desorption of the desorption gas I, the desorption gas I is sent to a coking primary cooler, and benzene, naphthalene, tar, sulfur and the like in the desorption gas I are recovered through chemical production; or as fuel gas, wherein hydrocarbons such as tar, benzene, naphthalene and the like are converted into carbon dioxide and water, sulfur is converted into sulfur dioxide to be discharged along with the flue gas, and the sulfur is purified by the flue gas to reach the standard and discharged.
In a possible embodiment of the present invention, the top gas treatment unit 20 further comprises a second pressurizing device 24, and the second pressurizing device 24 is connected between the scrubber 23 and the desulfurization and decarbonization device 25. The top gas A passing through the scrubber 23 is pressurized by the second pressurizing device 24, and then enters the desulfurization and decarburization device 25 for desulfurization and decarburization, and the rate of desulfurization and decarburization of the top gas A can be increased by pressurizing the top gas A.
In a possible embodiment of the present invention, the outlet of the desulfurization and decarbonization device 25 of the top gas treatment unit 20 is further connected to a process gas output pipeline 50 for delivering to a gas user.
Part of the process gas B output from the process gas B outlet via the desulfurization and decarbonization device 25 can be directly introduced into the shaft furnace 10 as reducing gas E via the second pipeline 42, and the other part can be delivered to the plant gas users via the process gas output pipeline 50 for the daily use of the gas users.
In a possible embodiment of the present invention, the inlet of the first heat exchanger 21 is connected to a steam inlet pipe 60, and the outlet of the first pressurizing device 44 is connected to the steam inlet pipe 60.
The H in the reducing gas E generated in the reforming furnace 411 can be adjusted by appropriately adding steam F to the coke oven gas C through the steam inlet pipe 60 before the coke oven gas C pressurized by the first pressurizing device 44 is fed to the reforming furnace 411 2 The ratio to CO; in this embodiment, H 2 The adjustable range of the ratio of/CO is 0.5-5.
In a possible embodiment of the present invention, the reforming furnace 411 includes a furnace body 412, an oxygen inlet 413 and a coke oven gas inlet 414 are disposed at the upper portion of the furnace body 412, the oxygen inlet 413 is connected to the oxygen inlet pipe 70, and the coke oven gas inlet 414 is connected to the outlet of the first heat exchanger 21; the furnace body 412 is provided at its lower portion with a reducing gas outlet 415, which reducing gas outlet 415 is connected to the reducing gas inlet 12 of the shaft furnace 10.
The utility model discloses a cylinder reformer 411 compares with traditional shell and tube reformer 411 and does not have the material restriction, and whole equipment is small, invests in lowly.
In particular, the coke oven coal after being pressurizedThe gas C and the water vapor F are mixed and preheated by a first heat exchanger 21, then enter a reforming furnace 411 through a coke oven gas inlet 414 on the reforming furnace 411, and oxygen G enters the reforming furnace 411 from an oxygen inlet 413; the coke oven gas C is mixed with oxygen G at the burner of the reforming furnace 411 to generate partial oxidation reaction, and CH in the coke oven gas C 4 、H 2 CO and high molecular hydrocarbon are subjected to partial oxidation reaction to release heat, and the product CO after partial oxidation 2 、H 2 O, etc. and unreacted CH 4 、CO 2 And CO in the process gas B 2 、H 2 O is mixed and enters the lower part of the reforming furnace 411 together to perform catalytic reforming reaction, CH 4 、CO 2 Conversion to CO and H 2 (ii) a The catalytic reforming reaction is an endothermic reaction, and the required heat is derived from the heat released by the oxidation of the upper part of the furnace body 412. The generated CO and H are rich 2 The reducing gas E flows out through a reducing gas outlet 415 at the bottom of the reforming furnace 411, is mixed with the process gas B in the second pipeline 42, is connected with a reducing gas inlet 12 of the shaft furnace 10 through a pipeline, and is introduced into the shaft furnace 10; wherein phi (H) in the reducing gas E 2+ CO)/φ(CO 2 +H 2 O) is greater than 10, phi (H) 2 ) The value of/φ (CO) is greater than 0.3, preferably between 1 and 3.
In one possible embodiment of the present invention, a catalyst layer 416 is disposed inside the furnace body 412, and the catalyst in the catalyst layer 416 is a nickel-based catalyst or a carbon-based catalyst. The catalyst in the catalyst layer 416 provided inside the furnace body 412 catalyzes the catalytic reforming reaction inside the reforming furnace 411 to accelerate the reaction.
In a practical embodiment of the present invention, the operation pressure of the reforming furnace 411 is 0.1 MPa-3.0 MPa, and the operation temperature thereof is 800 ℃ to 1100 ℃. In this embodiment, the furnace body 412 is made of refractory material and can operate at a relatively high pressure and temperature.
In a practical embodiment of the present invention, the pressure of the reducing gas E injected into the reducing gas inlet 12 is 0.08MPa to 2.0MPa, and the temperature of the reducing gas E is 850 ℃ to 1100 ℃. The high-temperature and high-pressure reducing gas E fed into the shaft furnace 10 facilitates the reduction reaction inside the shaft furnace 10, and accelerates the generation efficiency of direct reduced iron.
In one possible embodiment of the present invention, the adsorption refining device 31 is filled with a hydrophobic adsorption material. Furthermore, the hydrophobic adsorption material is a molecular sieve material which has adsorption capacity at 20-100 ℃ and can be desorbed and regenerated at 160-350 ℃.
In the embodiment, the adsorbent material is a molecular sieve, preferably a hydrophobic adsorption material, can adsorb impurities such as inorganic sulfur, organic sulfur, tar, benzene, naphthalene and the like, has adsorption capacity at 20-100 ℃, and can be desorbed and regenerated at 160-350 ℃; the service life of the adsorbent is 5-7 years, and the adsorbent can be repeatedly regenerated and resists high temperature.
In order to further explain the adjustable system of carbon dioxide for preparing the reducing gas of the shaft furnace by coke oven gas, the working process of the adjustable system of carbon dioxide for preparing the reducing gas of the shaft furnace by coke oven gas is explained in detail below.
As shown in FIG. 1, after the iron ore is processed into pellets or lump ore, the ore is fed from the upper feed port of the shaft furnace 10, and the reducing gas E flows from bottom to top inside the shaft furnace 10 and undergoes a reduction reaction with the iron ore at a temperature of 930 ℃ to obtain direct reduced iron and a top gas A. The top gas A is discharged from the top gas outlet 11 and enters the first heat exchanger 21 to exchange heat with the coke oven gas C entering the reforming furnace 411, the temperature of the coke oven gas C is raised to 400 ℃, and the coke oven gas C enters the reforming furnace 411. The furnace top gas A enters a second heat exchanger 22 after heat exchange through a first heat exchanger 21, exchanges heat with desorption gas H extracted from an outlet of an adsorption refining device 31, the desorption gas H is heated to 280 ℃, the furnace top gas A enters a scrubber 23 after heat exchange, enters a second pressurizing device 24 for pressurizing after cooling and dedusting, and then enters a desulfurization and decarburization device 25 for removing hydrogen sulfide, organic sulfur and CO 2 The process gas B generated later is divided into two parts, wherein one part of the process gas B accounting for 35 percent of the total amount is sent to gas users in a plant area through a process gas output pipeline 50 and is used for daily use of the gas users; another portion is conveyed directly as reducing gas E through the second production line 42 to the reducing gas inlet 12 of the shaft furnace 10.
Wherein the primarily purified coke oven gas C is 55000Nm 3 H, total sulfur content250mg/Nm 3 Containing 20mg/Nm of tar 3 Containing 500mg/Nm of benzene 3 Containing 500mg/Nm of naphthalene 3 Enters an adsorption refining device 31 for purification, and the purified coke oven gas C contains less than 1mg/Nm of sulfur 3 Containing benzene less than 1mg/Nm 3 Containing naphthalene in an amount of less than 1mg/Nm 3 。
In this example, the adsorption purification apparatus 31 employs 6 purification columns, 5 purification columns are operated, and 1 purification column is on standby. When the adsorption of the refining tower reaches a certain saturation level, about 4000Nm is extracted from an outlet pipeline of the adsorption refining device 31 3 The coke oven gas C of the/H is taken as desorption gas H, the temperature is raised to 280 ℃ through a second heat exchanger 22, and the refining tower is regenerated. The regeneration of the refining tower is divided into three stages of temperature rise, heat preservation and cooling, and the regeneration period is 3 days. During regeneration, impurities such as sulfur, benzene, naphthalene, tar and the like enter desorption gas I, wherein organic sulfur is converted into inorganic sulfur, and the desorption gas I is sent to a coking primary cooler and then useful resources are recovered through chemical production facilities. The purified coke oven gas C is pressurized by the first pressurizing device 44, is firstly mixed with the steam F entering the pipeline 60, and then enters the first heat exchanger 21 for preheating at the preheating temperature of 400 ℃. The preheated coke oven gas C enters the reforming furnace 411 from the coke oven gas inlet 414, the oxygen G enters the reforming furnace 411 from the oxygen inlet pipe 70, the coke oven gas C and the oxygen G generate oxidation reaction and catalytic reforming reaction in the reforming furnace 411 to generate reducing gas E, and the temperature of the reducing gas E obtained by the reaction is 960 ℃ and phi (H is H) 2 ) Has a value of 1.5,/phi (CO), phi (H) 2 )+φ(CO)>90 percent of the reaction gas E is mixed with part of the process gas B generated by the desulfurization and decarburization device 25 to be used as the reducing gas E, the reducing gas E enters the shaft furnace 10 from a reducing gas inlet 12 at the lower part of the shaft furnace 10 and reacts with the iron ore in the shaft furnace 10 to produce direct reduced iron, and the sponge iron with the temperature of 450 ℃ is output from the lower part of the shaft furnace 10.
The above-mentioned embodiments, further detailed description of the objects, technical solutions and advantages of the present invention, it should be understood that the above-mentioned embodiments are only specific embodiments of the present invention, and are not intended to limit the scope of the present invention, and any modifications, equivalent substitutions, improvements and the like made within the spirit and principle of the present invention should be included in the scope of the present invention.
Claims (13)
1. A carbon dioxide adjustable system for preparing shaft furnace reducing gas from coke oven gas is characterized by comprising the following components:
a shaft furnace having a top gas outlet and a reducing gas inlet;
the furnace top gas treatment unit comprises a first heat exchanger, a scrubber and a desulfurization and decarburization device which are sequentially connected, wherein the first heat exchanger is connected with the furnace top gas outlet;
the coke oven gas treatment unit comprises an adsorption refining device for treating the coke oven gas;
a reducing gas generation unit comprising a first generation line and a second line; wherein the first production line is provided with a first pressurizing device, the first heat exchanger and a reforming furnace, the outlet of the reforming furnace is connected with the reducing gas inlet, and the inlet of the first pressurizing device is connected with the outlet of the adsorption refining device; one end of the second pipeline is connected with an outlet of the desulfurization and decarburization device of the top gas treatment unit, and the other end of the second pipeline is connected with the reducing gas inlet.
2. The carbon dioxide tunable system for preparing the reducing gas of the shaft furnace from coke oven gas as claimed in claim 1, wherein the reducing gas generation unit further comprises a carbon dioxide injection line connected between an outlet of the desulfurization and decarbonization device and an inlet of the first heat exchanger of the reducing gas generation unit.
3. The carbon dioxide tunable system for preparing shaft furnace reducing gas from coke oven gas according to claim 1, wherein the top gas treatment unit further comprises a second heat exchanger connected between the first heat exchanger and the scrubber.
4. The system for adjusting carbon dioxide in reducing gas of a coke oven gas preparation shaft furnace according to claim 3, wherein an outlet of the adsorption refining device is connected with an inlet of the second heat exchanger, and an outlet of the second heat exchanger is connected with an inlet of the adsorption refining device.
5. The carbon dioxide tunable system for a reducing gas of a coke oven gas preparation shaft furnace according to claim 1 or 3, characterized in that the top gas treatment unit further comprises a second pressurizing device connected between the scrubber and the desulfurization and decarbonization device.
6. The system for adjusting carbon dioxide in reducing gas of a shaft furnace for preparing coke oven gas according to claim 5, wherein an outlet of the desulfurization and decarburization device of the top gas treatment unit is further connected with a process gas output pipeline for delivering the process gas to a gas user.
7. The system of claim 1, wherein an inlet of the first heat exchanger is connected to a steam inlet pipe, and an outlet of the first pressurizing device is connected to the steam inlet pipe.
8. The system of claim 7, wherein the reformer comprises a furnace body, the upper part of the furnace body is provided with an oxygen inlet and a coke oven gas inlet, the oxygen inlet is connected with an oxygen inlet pipe, and the coke oven gas inlet is connected with an outlet of the first heat exchanger; the lower part of the furnace body is provided with a reducing gas outlet which is connected with the reducing gas inlet.
9. The system of claim 8, wherein a catalyst layer is arranged inside the furnace body, and the catalyst in the catalyst layer is a nickel-based catalyst or a carbon-based catalyst.
10. The carbon dioxide adjustable system for preparing shaft furnace reducing gas from coke oven gas as claimed in claim 1, characterized in that the operating pressure of the reforming furnace is 0.1 MPa-3.0 MPa, and the operating temperature is 800 ℃ to 1100 ℃.
11. The carbon dioxide adjustable system for preparing the reducing gas of the shaft furnace from the coke oven gas as claimed in claim 1, wherein the pressure of the reducing gas injected into the reducing gas inlet is 0.08MPa to 2.0MPa, and the temperature of the reducing gas is 850 ℃ to 1100 ℃.
12. The system as claimed in claim 1, wherein the adsorption refining device is filled with hydrophobic adsorption material.
13. The system of claim 12, wherein the hydrophobic adsorption material is a molecular sieve material having an adsorption capacity at 20-100 ℃ and capable of desorption regeneration at 160-350 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223598997.4U CN218853934U (en) | 2022-12-30 | 2022-12-30 | Carbon dioxide adjustable system for preparing reducing gas of shaft furnace by coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223598997.4U CN218853934U (en) | 2022-12-30 | 2022-12-30 | Carbon dioxide adjustable system for preparing reducing gas of shaft furnace by coke oven gas |
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| CN218853934U true CN218853934U (en) | 2023-04-14 |
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| CN202223598997.4U Active CN218853934U (en) | 2022-12-30 | 2022-12-30 | Carbon dioxide adjustable system for preparing reducing gas of shaft furnace by coke oven gas |
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