CN218842080U - System for preparing reducing gas of shaft furnace by coke oven gas - Google Patents
System for preparing reducing gas of shaft furnace by coke oven gas Download PDFInfo
- Publication number
- CN218842080U CN218842080U CN202223604546.7U CN202223604546U CN218842080U CN 218842080 U CN218842080 U CN 218842080U CN 202223604546 U CN202223604546 U CN 202223604546U CN 218842080 U CN218842080 U CN 218842080U
- Authority
- CN
- China
- Prior art keywords
- gas
- furnace
- heat exchanger
- coke oven
- shaft furnace
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Industrial Gases (AREA)
Abstract
The utility model discloses a system for preparing shaft furnace reducing gas by coke oven gas, which comprises a shaft furnace; the furnace top gas treatment unit is connected with the shaft furnace and comprises a first heat exchanger, a washer and a desulfurization device which are sequentially connected, wherein the first heat exchanger is connected with the shaft furnace; the coke oven gas treatment unit comprises an adsorption refining device for treating the coke oven gas; reduction gas generationThe unit is connected with the shaft furnace and comprises a pressurizing device, a first heat exchanger and a dry reforming furnace, wherein the pressurizing device is connected with the first heat exchanger, the first heat exchanger is connected with the dry reforming furnace, and the dry reforming furnace is connected with a reducing gas inlet of the shaft furnace; wherein, the desulphurization device and the adsorption refining device are respectively connected with the pressurizing device. The utility model utilizes the adsorption purification technology to remove impurities in the coke oven gas, and the refined coke oven gas, the carbon-containing process gas and the oxygen are catalytically converted into reducing gas in the reformer after being mixed, and has the advantages of simple process, high-pressure operation, small equipment volume, energy conservation, CO 2 Low emission and the like.
Description
Technical Field
The utility model relates to a coke oven gas recycles technical field, especially relates to a system of coke oven gas preparation shaft furnace reducing gas.
Background
The third CO in the iron and steel industry 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 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.
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. Coke oven gas containing H 2 S、CS 2 、COS、NH 3 And impurities such as BTX (benzene, toluene, xylene, and the like), tar, naphthalene, and the like, which cause that the conventional gas-based shaft furnace process using natural gas as a gas source cannot operate, and a gas-based shaft furnace reducing gas process suitable for coke oven gas needs to be developed.
The existing 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 low, the equipment is huge, and the investment is high.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a system of coke oven gas preparation shaft furnace reducing gas utilizes the impurity among the adsorption and purification technique desorption coke oven gas, and refined coke oven gas, carbonaceous process gas, oxygen are converted into reducing gas by the catalysis in the reformer after mixing, but have simple process, high-pressure operation, equipment small, energy-conserving, CO 2 Low emission and the like.
The above implementation objective of the present invention is mainly realized by the following technical solutions:
a system for preparing shaft furnace reducing gas from coke oven gas comprises:
a shaft furnace;
the furnace top gas processing unit is connected with the shaft furnace and comprises a first heat exchanger, a scrubber and a desulfurization device which are sequentially connected, and the first heat exchanger is connected with a furnace top gas outlet of the shaft furnace;
the coke oven gas treatment unit comprises an adsorption refining device for treating the coke oven gas;
the reducing gas generating unit is connected with the shaft furnace and comprises a pressurizing device, a first heat exchanger and a dry reforming furnace, wherein an outlet of the pressurizing device is connected with an inlet of the first heat exchanger, an outlet of the first heat exchanger is connected with the dry reforming furnace, and the dry reforming furnace is connected with a reducing gas inlet of the shaft furnace;
wherein the outlet of the desulfurization device and the outlet of the adsorption refining device are respectively connected with the inlet of the pressurizing device.
In a preferred embodiment of the present invention, the top gas treatment unit further comprises a second heat exchanger, and the second heat exchanger is 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 processing unit further comprises a user pipeline connected to a gas user, the user pipeline being connected to the outlet of the desulfurization device.
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 pressurizing device is connected to the steam inlet pipe.
In a preferred embodiment of the present invention, the dry reforming furnace includes a furnace body, an oxygen inlet and a mixed gas inlet are provided at an upper portion of the furnace body, the oxygen inlet is connected to an oxygen inlet pipe, and the mixed gas inlet is connected to an outlet of the first heat exchanger; and the lower part of the furnace body is provided with a reducing gas outlet which is connected with the reducing gas inlet of the shaft furnace.
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 dry reforming furnace is 0.1MPa to 3.0MPa, and the operating temperature thereof is 800 ℃ to 1100 ℃.
In a preferred embodiment of the present invention, the temperature of the top gas discharged from the top gas outlet of the shaft furnace is 300 to 500 ℃; after heat exchange is carried out by the first heat exchanger and the second heat exchanger, the temperature of the top gas is 30-50 ℃.
In a preferred embodiment of the present invention, the adsorption purification apparatus is filled with an adsorbent material for adsorbing impurities in the coke oven gas, and the adsorbent material has an adsorption capacity at 20 to 100 ℃ and is desorbed and regenerated at 160 to 350 ℃.
Compared with the prior art, technical scheme following beneficial effect has:
1. the utility model discloses a system for coke oven gas preparation shaft furnace reducing gas adopts molecular sieve absorption desorption sulphur and BTX (the mixture of benzene, toluene, xylol) wherein, and desorption gas utilizes the furnace roof gas heating, 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 system for preparing shaft furnace reducing gas from coke oven gas, which adopts a dry reforming furnace, a furnace body can be made of refractory materials, and can run under higher pressure and temperature, and compared with the traditional tube type reforming furnace, the system has no material limitation, the whole equipment volume is small, and the investment is low;
3. the utility model discloses a system for coke oven gas preparation shaft furnace is original gas adopts coke oven gas and carbon dioxide catalytic conversion to be richly contained H 2 Reducing CO, saving energy and reducing emission 2 ；
4. The utility model discloses a system for coke oven gas preparation shaft furnace is reducing gas has set up the heat exchanger, and the reducing gas of reborner output directly enters the shaft furnace, and the energy consumption is low, and the flow is succinct.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description 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 connection structure of a system for preparing reducing gas of a shaft furnace from coke oven gas.
The reference numbers indicate:
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 desulfurization unit; 30. a coke oven gas processing unit; 31. an adsorption refining device; 40. a reducing gas generation unit; 41. a pressurizing device; 42. dry reforming furnace; 421. a furnace body; 422. an oxygen inlet; 423. a mixed gas inlet; 424. a reducing gas outlet; 425. a catalyst layer; 50. steam enters the pipeline; 60. oxygen enters the pipeline; 70. a user conduit; A. top gas of the furnace; B. process gas; C. coke oven gas; D. mixing gas; E. reducing gas; F. steam; 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. The terms "vertical," "horizontal," "left," "right," and the like as used herein are for illustrative purposes 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 in the description of the invention herein 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.
A system for preparing shaft furnace reducing gas from coke oven gas comprises:
a shaft furnace 10;
the top gas treatment unit 20 is connected with the shaft furnace 10, the top gas treatment unit 20 comprises a first heat exchanger 21, a scrubber 23 and a desulphurization device 24 which are sequentially connected, and the first heat exchanger 21 is connected with the top gas outlet 11 of the shaft furnace 10;
a coke oven gas treatment unit 30 including an adsorption refining device 31 for treating the coke oven gas C;
a reducing gas generating unit 40 connected to the shaft furnace 10, the reducing gas generating unit 40 comprising a pressurizing device 41, a first heat exchanger 21, and a dry reforming furnace 42, an outlet of the pressurizing device 41 being connected to an inlet of the first heat exchanger 21, an outlet of the first heat exchanger 21 being connected to the dry reforming furnace 42, the dry reforming furnace 42 being connected to the reducing gas inlet 12 of the shaft furnace 10;
wherein, the outlet of the desulfurization device 24 and the outlet of the adsorption refining device 31 are respectively connected with the inlet of the pressurizing device 41.
The utility model discloses a roof gas processing unit 20, coke oven gas processing unit 30 and the reduction gas generation unit 40 that link to each other, with the roof gas A and the coke oven gas C of the shaft furnace 10 through handling catalytic conversion in dry reformer 42 reduction gas E, but have simple process, high-pressure operation, equipment are small, energy-conserving, CO 2 Low emission and the like.
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 sponge iron and top gas a, the sponge 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 treated to generate process gas B which can be primarily utilized. The top gas treatment unit 20 comprises a first heat exchanger 21, a scrubber 23 and a desulphurization device 24 which are sequentially connected, the first heat exchanger 21 is connected with a top gas outlet 11 of the shaft furnace 10, the top gas A firstly passes through the first heat exchanger 21 to be cooled, the waste heat of the top gas A is recovered, then the top gas A enters the scrubber 23 to be dedusted, and then the top gas A enters the desulphurization device 24 to be subjected to removal of organic sulfur and inorganic sulfur; in this embodiment, the desulfurization unit 24 can adopt dry desulfurization or wet desulfurization, and the sulfur content of the top gas A after passing through the desulfurization unit 24 is less than or equal to 5ppmv. The process gas B generated after the heat exchange and purification of the top gas A and the coke oven gas C (COG) after adsorption and refining are mixed and enter the reducing gas generation unit 40.
The coke oven gas treatment unit 30 mainly performs adsorption refining treatment on 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 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 apparatuses 31 are provided, and at least 1 is provided, and the filler for adsorbing coke oven gas C in the adsorption/purification apparatus 31 may be a molecular sieve, preferably a hydrophobic material. The coke oven gas C passing through the adsorption refining device 31 is mixed with the process gas B generated by the top gas treatment unit 20 and enters the reducing gas generation unit 40.
The reducing gas generating unit 40 is mainly used for processing the process gas B and the refined coke oven gas C respectively generated by the top gas processing unit 20 and the coke oven gas processing unit 30 to generate the reducing gas E. Specifically, as shown in FIG. 1, the outlet of the desulfurizer 24 and the coke oven gas location in the top gas treatment unit 20The outlet of the adsorption purification device 31 in the treatment unit 30 is connected to the inlet of the pressurizing device 41 in the reducing gas generation unit 40, and the mixed gas D is pressurized to 0.1MPa to 2.0MPa in the pressurizing device 41; the mixed gas D is pressurized and then enters a first heat exchanger 21 through a pipeline, and is subjected to heat exchange treatment with the top gas A in the first heat exchanger 21, and the temperature of the mixed gas D after heat exchange is more than 300 ℃; the mixed gas D enters the dry reforming furnace 42 after passing through the first heat exchanger 21, the mixed gas D is mixed with oxygen G at the inlet of the dry reforming furnace 42 to generate partial oxidation reaction, and CH in the coke oven gas C in the mixed gas D 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 And CO in the process gas B in the mixed gas D 2 Is catalytically reformed into CO and H in the lower part of the dry reforming furnace 42 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 the dry reformer 42 2 And CO as a reducing gas E, into the shaft furnace 10.
In a possible embodiment of the present invention, as shown in fig. 1, 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, an outlet of the adsorption refining device 31 is connected with an inlet of the second heat exchanger 22, and an outlet of the second heat exchanger 22 is connected with an 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 one possible embodiment of the present invention, as shown in fig. 1, the top gas treatment unit 20 further includes a user pipe 70 connected to a gas user, and the user pipe 70 is connected to an outlet of the desulfurization unit 24.
The process gas B generated after the heat exchange and purification of the top gas A is divided into two parts, one part is delivered to plant gas users through a user pipeline 70 for the daily use of the gas users, and the other part is mixed with coke oven gas C (COG) after adsorption and refining and enters a reducing gas generation unit 40; in this embodiment, the ratio of the process gas B as the fuel gas is 10% to 50%.
In a possible embodiment of the invention, as shown in fig. 1, the inlet of the first heat exchanger 21 is connected to a steam inlet pipe 50, and the outlet of the pressurizing device 41 is connected to the steam inlet pipe 50. The addition of steam F to the mixed gas D via steam inlet line 50 prior to introduction of the mixed gas D into the dry reforming furnace 42 can be regulated by the addition of steam F to the mixed gas D as appropriate 2 The ratio to CO; in this example, H 2 The adjustable range of the ratio of/CO is 0.5-5.
In one possible embodiment of the present invention, the dry reforming furnace 42 includes a furnace body 421, the upper portion of the furnace body 421 is provided with an oxygen inlet 422 and a mixed gas inlet 423, the oxygen inlet 422 is connected to the oxygen inlet pipe 60, and the mixed gas inlet 423 is connected to the outlet of the first heat exchanger 21; the furnace body 421 is provided at a lower portion thereof with a reducing gas outlet 424, the reducing gas outlet 424 being connected to the reducing gas inlet 12 of the shaft furnace 10.
The utility model discloses a dry reforming furnace 42 compares with traditional shell and tube reforming furnace and does not have the material restriction, and whole equipment is small, invests in lowly.
Specifically, the pressurized mixed gas D is mixed with the water vapor F, preheated by the first heat exchanger 21, and enters through the mixed gas inlet 423 of the dry reforming furnace 42, and the oxygen G enters from the oxygen inlet 422; the mixed gas D and the oxygen G are mixed at the burner of the dry reforming furnace 42 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 a 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 dry reforming furnace 42 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 comes from the heat released by the oxidation of the upper part of the furnace body 421. The generated CO and H are rich 2 The reducing gas E flows out through a reducing gas outlet 424 at the bottom of the dry reforming furnace 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 a practical embodiment of the present invention, the furnace body 421 is provided with a catalyst layer 425 inside, and the catalyst in the catalyst layer 425 is a nickel-based catalyst or a carbon-based catalyst. The catalyst in the catalyst layer 425 provided inside the furnace body 421 can catalyze the catalytic reforming reaction inside the dry reforming furnace 42 to accelerate the reaction.
In one practical embodiment of the present invention, the operating pressure of the dry reforming furnace 42 is 0.1MPa to 3.0MPa, and the operating temperature thereof is 800 ℃ to 1100 ℃. In this embodiment, the furnace body 421 is made of refractory material and can operate at a high pressure and temperature.
In a possible embodiment of the present invention, the temperature of the top gas a discharged from the top gas outlet 11 of the shaft furnace 10 is 300 ℃ to 500 ℃; after heat exchange is carried out by the first heat exchanger 21 and the second heat exchanger 22, the temperature of the top gas A is 30-50 ℃. The waste heat of the top gas A is recovered through the first heat exchanger 21 and the second heat exchanger 22, and the energy conversion efficiency is greatly improved.
In one possible embodiment of the present invention, the adsorption refining device 31 is filled with an adsorbent material for adsorbing impurities in the coke oven gas C, and the adsorbent material has an adsorption capacity at 20 to 100 ℃ and is desorbed and regenerated at 160 to 350 ℃.
In this embodiment, the adsorbent material is a molecular sieve, preferably a hydrophobic adsorbent material, which can adsorb impurities such as inorganic sulfur, organic sulfur, tar, benzene, naphthalene, etc., has an 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 system for preparing the shaft furnace reducing gas by using the coke oven gas, the working process of the system for preparing the shaft furnace reducing gas by using the 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 material is fed from the upper feed inlet of the shaft furnace 10, and the reducing gas E flows from bottom to top in the shaft furnace 10 and undergoes a reduction reaction with the iron ore at a temperature of 930 ℃ to obtain sponge iron and top gas A. The top gas A is discharged from the top gas outlet 11 and enters the first heat exchanger 21, and exchanges heat with the mixed gas D of the dry reforming furnace 42, the temperature of the mixed gas D is raised to 350 ℃, and the mixed gas enters the dry reforming furnace 42. The top gas A enters a second heat exchanger 22 after heat exchange through a first heat exchanger 21, exchanges heat with desorption gas H of an adsorption refining device 31 of coke oven gas C, the desorption gas H is heated to 280 ℃, the top gas A enters a scrubber 23 after heat exchange, the top gas A enters a desulphurization device 24 after cooling and dedusting, process gas B generated after hydrogen sulfide and organic sulfur are removed is divided into two parts, and one part of the process gas B accounting for 30 percent of the total amount is conveyed to plant gas users through a user pipeline 70; the other part is mixed with the coke oven gas C after adsorption refining, the pressure is increased to 0.5MPa through a pressurizing device 41, the mixture enters a pipeline 50 through water vapor to be mixed with proper amount of water vapor F, and the mixture enters a mixed gas inlet 423 of a dry reforming furnace 42 after being preheated by a first heat exchanger 21.
Wherein, the desulphurization device 24 of the top gas A adopts dry desulphurization to remove hydrogen sulfide and organic sulfur, and the content of the removed sulfur is 1ppmv. The primarily purified coke oven gas C is 60000Nm 3 H, total sulfur content 300mg/Nm 3 Containing tar oil 20mg/Nm 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, and 5 purification columns operate and 1 purification column is reserved. When the adsorption of the refining tower reaches a certain saturation level, about 5000Nm 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 and the process gas B are mixed, pressurized by a pressurizing device 41, mixed with the steam F entering a pipeline 50, and then enter a first heat exchanger 21 for preheating, wherein the preheating temperature is 350 ℃. The preheated mixed gas D enters the dry reforming furnace 42 from the mixed gas inlet 423, the oxygen G enters the dry reforming furnace 42 from the oxygen inlet 422, the mixed gas D and the oxygen G generate oxidation reaction and catalytic reforming reaction in the dry reforming furnace 42 to generate a reducing gas E, and the temperature of the reducing gas E obtained by the reaction is 930 ℃ phi (H) 2 ) Phi (CO) is about 1.3, phi (H) 2 )+φ(CO)>80 percent of the reducing gas E enters the shaft furnace 10 from a reducing gas inlet 12 at the lower part of the shaft furnace 10 to react with the iron ore in the furnace to produce the sponge iron, and the sponge iron with the temperature of 500 ℃ is output from the lower part of the shaft furnace 10.
The above-mentioned embodiments, which further illustrate the objects, technical solutions and advantages of the present invention in detail, it should be understood that the above-mentioned embodiments are only examples 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 (10)
1. A system for preparing shaft furnace reducing gas from coke oven gas is characterized by comprising the following components:
a shaft furnace;
the furnace top gas treatment unit is connected with the shaft furnace and comprises a first heat exchanger, a scrubber and a desulfurization device which are sequentially connected, wherein the first heat exchanger is connected with a furnace top gas outlet of the shaft furnace;
the coke oven gas treatment unit comprises an adsorption refining device for treating the coke oven gas;
the reducing gas generating unit is connected with the shaft furnace and comprises a pressurizing device, a first heat exchanger and a dry reforming furnace, wherein an outlet of the pressurizing device is connected with an inlet of the first heat exchanger, an outlet of the first heat exchanger is connected with the dry reforming furnace, and the dry reforming furnace is connected with a reducing gas inlet of the shaft furnace;
wherein, the outlet of the desulphurization device and the outlet of the adsorption refining device are respectively connected with the inlet of the pressurizing device.
2. The system of claim 1, wherein the top gas processing unit further comprises a second heat exchanger connected between the first heat exchanger and the scrubber.
3. The system for preparing reducing gas of the shaft furnace from coke oven gas according to claim 2, 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.
4. The system for preparing reducing gas of the shaft furnace from coke oven gas according to claim 1, wherein the top gas processing unit further comprises a user pipeline connected with a gas user, and the user pipeline is connected with an outlet of the desulfurization device.
5. The system for preparing reducing gas of the shaft furnace from coke oven gas as claimed in claim 1, wherein an inlet of the first heat exchanger is connected with a steam inlet pipeline, and an outlet of the pressurizing device is connected with the steam inlet pipeline.
6. The system for preparing reducing gas of the shaft furnace from coke oven gas as claimed in claim 5, wherein the dry reforming furnace comprises a furnace body, the upper part of the furnace body is provided with an oxygen inlet and a mixed gas inlet, the oxygen inlet is connected with an oxygen inlet pipeline, and the mixed gas inlet is connected with an outlet of the first heat exchanger; and the lower part of the furnace body is provided with a reducing gas outlet which is connected with the reducing gas inlet of the shaft furnace.
7. The system for preparing reducing gas of the shaft furnace from coke oven gas as claimed in claim 6, 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.
8. The system for preparing reducing gas of the shaft furnace from coke oven gas as claimed in claim 1, wherein the operating pressure of the dry reforming furnace is 0.1MPa to 3.0MPa, and the operating temperature is 800 ℃ to 1100 ℃.
9. The system for preparing shaft furnace reducing gas from coke oven gas according to claim 2, wherein the temperature of the top gas discharged from the top gas outlet of the shaft furnace is 300 ℃ to 500 ℃; after heat exchange is carried out by the first heat exchanger and the second heat exchanger, the temperature of the top gas is 30-50 ℃.
10. The system for preparing shaft furnace reducing gas from coke oven gas according to claim 1, wherein the adsorption refining device is filled with an adsorbent material for adsorbing impurities in the coke oven gas, and the adsorbent material has an adsorption capacity at 20-100 ℃ and is desorbed and regenerated at 160-350 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223604546.7U CN218842080U (en) | 2022-12-30 | 2022-12-30 | System for preparing reducing gas of shaft furnace by coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223604546.7U CN218842080U (en) | 2022-12-30 | 2022-12-30 | System for preparing reducing gas of shaft furnace by coke oven gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218842080U true CN218842080U (en) | 2023-04-11 |
Family
ID=87300242
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223604546.7U Active CN218842080U (en) | 2022-12-30 | 2022-12-30 | System for preparing reducing gas of shaft furnace by coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218842080U (en) |
-
2022
- 2022-12-30 CN CN202223604546.7U patent/CN218842080U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5796672B2 (en) | How to operate a blast furnace or steelworks | |
| WO2011108546A1 (en) | Blast furnace operation method, iron mill operation method, and method for utilizing a gas containing carbon oxides | |
| CN106103747A (en) | For the method operating top gas recirculation blast furnace installation | |
| CN101239702B (en) | High temperature coke oven crude gas hydrogen generating system device and technique | |
| EP2657215A1 (en) | Method and device for producing methanol | |
| CN111847381B (en) | Method and device for preparing hydrogen from industrial waste gas | |
| CN103805728B (en) | Method and device for producing reduced iron through synthetic gas prepared from high-nitrogen content retort gas | |
| CN203513711U (en) | System for producing gas-base direct reduction iron from coke-oven gas | |
| CN218842080U (en) | System for preparing reducing gas of shaft furnace by coke oven gas | |
| CN213772106U (en) | Gas-based shaft furnace reducing gas preparation system | |
| CN103952184A (en) | Method and system for preparing reducing gas used for shaft furnace through catalytic coal gasification | |
| CN213772103U (en) | System for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide | |
| CN218811560U (en) | Decarbonization and process gas recycling system for reducing gas of coke oven gas preparation shaft furnace | |
| CN218811562U (en) | System for preparing reducing gas by coke oven gas coupling shaft furnace conversion | |
| CN218853934U (en) | Carbon dioxide adjustable system for preparing reducing gas of shaft furnace by coke oven gas | |
| CN218893633U (en) | Temperature regulating system for preparing shaft furnace reducing gas from coke oven gas | |
| CN114774611A (en) | Hydrogen rich gas CO2Method for producing iron by oxidation conversion and hydrogen-based shaft furnace direct reduction | |
| CN213772104U (en) | Shaft furnace reducing gas preparation and self desorption system | |
| CN213895742U (en) | Shaft furnace reducing gas preparation and desorption gas self-heating system | |
| CN213895743U (en) | Shaft furnace reducing gas preparation and oxygen spraying temperature rising system | |
| CN213895741U (en) | Shaft furnace reducing gas preparation and humidification carbon elimination system | |
| CN114574648B (en) | System and method for preparing reducing gas of gas-based shaft furnace | |
| CN112408322A (en) | System and method for preparing ethanol and ethylene glycol synthesis gas through coke oven gas carbon supplementing conversion | |
| CN213772105U (en) | Shaft furnace reducing gas preparation and dry desulphurization system | |
| CN114574647B (en) | System and method for preparing shaft furnace reducing gas by coupling coke oven gas with carbon dioxide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |