CN222434398U - Comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas - Google Patents
Comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas Download PDFInfo
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- CN222434398U CN222434398U CN202421214405.0U CN202421214405U CN222434398U CN 222434398 U CN222434398 U CN 222434398U CN 202421214405 U CN202421214405 U CN 202421214405U CN 222434398 U CN222434398 U CN 222434398U
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 157
- 239000000571 coke Substances 0.000 title claims abstract description 28
- 230000002194 synthesizing effect Effects 0.000 title claims abstract description 15
- 238000001179 sorption measurement Methods 0.000 claims abstract description 55
- 238000002156 mixing Methods 0.000 claims abstract description 38
- 238000006057 reforming reaction Methods 0.000 claims abstract description 15
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 48
- 230000015572 biosynthetic process Effects 0.000 claims description 33
- 238000003786 synthesis reaction Methods 0.000 claims description 33
- 238000000926 separation method Methods 0.000 claims description 28
- 238000000746 purification Methods 0.000 claims description 26
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- 238000010926 purge Methods 0.000 claims description 6
- 230000003009 desulfurizing effect Effects 0.000 abstract description 6
- 238000004064 recycling Methods 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 206
- 239000000047 product Substances 0.000 description 49
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 14
- 229910000831 Steel Inorganic materials 0.000 description 14
- 239000010959 steel Substances 0.000 description 14
- 238000000034 method Methods 0.000 description 13
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 12
- 229910052799 carbon Inorganic materials 0.000 description 12
- 229910002091 carbon monoxide Inorganic materials 0.000 description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 9
- 229910052739 hydrogen Inorganic materials 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000002994 raw material Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 238000005261 decarburization Methods 0.000 description 4
- 238000005496 tempering Methods 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 238000010248 power generation Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002090 carbon oxide Inorganic materials 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
Abstract
The utility model discloses a comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas, which comprises a purifying and desulfurizing device, a CO 2 separating and purifying device, a first pressure swing adsorption device, a purifying and separating device, a methanation device, a second pressure swing adsorption device, a dry reforming reaction device, a third pressure swing adsorption device, a methanol synthesizing device, a rectifying device, a compressor, a first gas mixing device, a second gas mixing device and a blast furnace, wherein a blast furnace gas pipe network is sequentially communicated with the purifying and desulfurizing device and the CO 2 separating and purifying device through pipelines, a lean CO 2 gas outlet of the CO 2 separating and purifying device is communicated with an inlet of the first pressure swing adsorption device, a rich CO 2 gas outlet of the first pressure swing adsorption device is communicated with a gas inlet of the blast furnace through the second gas mixing device. The system reduces CO 2 emission and realizes the recycling and efficient utilization of each effective component of the gas.
Description
Technical Field
The utility model relates to the field of gas resource utilization, in particular to a comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas.
Background
The steel industry is a large household with CO 2 emission, carbon emission is about 15% of the whole country, and byproduct gas (blast furnace gas, converter gas and coke oven gas) is a main carbon discharge source. At present, the energy is utilized by means of power generation, combustion and the like, so that not only is the resource wasted, but also the environment is polluted. Therefore, the utilization rate of gas resources is improved, and the reduction of carbon emission becomes an urgent need for sustainable development of the steel industry.
The tempering co-production not only can make the byproduct gas of the steel mill be efficiently utilized, but also can promote the multi-element supply of chemical raw materials, and most importantly, can fix carbon elements discharged by the steel industry, thereby realizing the aim of reducing carbon. The development of toughening co-production in the steel industry focuses on separating and purifying effective components (H 2、CO、CO2、CH4 and the like) in byproduct gas of a steel mill as raw materials to synthesize chemical products such as methanol, ethanol, glycol, urea and the like. The methanol is widely used as chemical raw materials and green fuel, has large market capacity, separates and purifies CO 2 and H 2 from steel mill gas by tempering and coproduction, and synthesizes high-value methanol, which is an effective way for reducing carbon and enhancing efficiency.
The patent application of publication No. CN116397062A provides a near-zero carbon emission blast furnace long-flow tempering CO-production process and a system thereof, wherein blast furnace gas is subjected to pressure swing adsorption decarburization to separate desorption gas and decarburization gas, the desorption gas is subjected to liquefaction rectification to purify to obtain liquid carbon dioxide, one part of the decarburization gas is recycled to the blast furnace, and the other part of the decarburization gas is mixed with refined converter gas and coke oven gas converted from light hydrocarbon to separate CO+N 2、H2 material flow for synthesizing ethylene glycol. The process and the system thereof combine and solidify 'carbon' emission into a liquid carbon dioxide product through steel coke fusion and tempering, but do not directly fix CO 2 into high-value products, and increase the subsequent treatment procedures of CO 2.
The patent application of publication No. CN116947619A provides a process and a system for preparing acetic acid by dry reforming and oxo synthesis of methane-rich gas, wherein methane-rich gas and CO 2 are used as raw materials, and acetic acid products are obtained by the processes of dry reforming reaction, CO 2 separation, CO separation, methanol synthesis, oxo synthesis and the like. The process and the system fully utilize the methane-rich gas to prepare the acetic acid, reduce the emission of greenhouse gas CO 2 in the traditional acetic acid preparation process, but the source of CO 2 raw material gas is unknown, the process flow is longer, and the steel mill gas is not effectively treated.
Disclosure of utility model
The utility model aims to provide a comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas by recycling and efficiently utilizing various components of gas.
The technical scheme includes that the device comprises a purification desulfurization device, a CO 2 separation and purification device, a first pressure swing adsorption device, a purification and separation device, a methanation device, a second pressure swing adsorption device, a dry reforming reaction device, a third pressure swing adsorption device, a methanol synthesis device, a rectification device, a compressor, a first gas mixing device, a second gas mixing device and a blast furnace, wherein a blast furnace gas pipe network is sequentially communicated with the purification desulfurization device and the CO 2 separation and purification device through pipelines, a lean CO 2 gas outlet of the CO 2 separation and purification device is communicated with an inlet of the first pressure swing adsorption device, a rich CO 2 gas outlet of the first pressure swing adsorption device is communicated with a gas inlet of the blast furnace through the second pressure swing adsorption device, a rich H 2 gas outlet of the second pressure swing adsorption device is communicated with an inlet of the second gas mixing device, a rich methane gas outlet of the first gas mixing device is communicated with an inlet of the second pressure swing adsorption device, a lean CO 2 gas outlet of the first pressure swing adsorption device is sequentially communicated with a gas inlet of the third pressure swing adsorption device, and a rich CO gas outlet of the third pressure swing adsorption device is sequentially communicated with a gas inlet of the third pressure swing adsorption device.
Furthermore, a third gas mixing device is arranged between the third pressure swing adsorption device and the methanol synthesis device, and a purge gas outlet of the methanol synthesis device is communicated with an inlet of the third gas mixing device.
Further, the tail gas outlet of the first pressure swing adsorption device is communicated with a gas pipe network.
The technical scheme has the beneficial effects that the method takes CO 2 in blast furnace gas and methane-rich gas obtained by methanation of coke oven gas as raw materials for dry reforming, and the obtained synthesis gas is synthesized into methanol products after partial CO is separated, so that the problem of large discharge of blast furnace gas CO 2 in steel plants is solved, and the high-value utilization is performed. The blast furnace gas separated CO, the synthetic gas separated CO and the hydrogen-rich gas generated by methanation of the coke oven gas are recycled, so that the recycling and high-efficiency utilization of each effective component of the steel mill gas is realized, the process flow is simple, and the blast furnace process is reduced from the source. The utility model reduces CO 2 emission, realizes the recycling and high-efficiency utilization of each effective component of the gas, improves the economic benefit of steel mills, and has important significance for realizing the double-carbon target.
Drawings
The utility model will be described in further detail with reference to the drawings and the detailed description.
Fig. 1 is a schematic diagram of the system architecture of the present utility model.
Detailed Description
As shown in FIG. 1, the comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas comprises a purifying and desulfurizing device, a CO 2 separating and purifying device, a first pressure swing adsorption device, a purifying and separating device, a methanation device, a second pressure swing adsorption device, a dry reforming reaction device, a third pressure swing adsorption device, a methanol synthesizing device, a rectifying device, a first gas mixing device, a second gas mixing device, a third gas mixing device, a blast furnace, a first compressor, a second compressor, a third compressor, a fourth compressor and a fifth compressor. The blast furnace gas pipeline is communicated with an inlet of the purification desulfurization device through a pipeline, an outlet of the purification desulfurization device is communicated with an inlet of the CO 2 separation purification device through a first compressor, a lean CO 2 gas outlet of the CO 2 separation purification device is communicated with an inlet of the first pressure swing adsorption device through a second compressor, a CO-rich gas outlet of the first pressure swing adsorption device is communicated with an inlet of the second gas mixing device, an outlet of the second gas mixing device is communicated with a gas inlet of the blast furnace, a CO-rich 2 gas outlet of the CO 2 separation purification device is communicated with the first gas mixing device, and a tail gas outlet of the first pressure swing adsorption device is communicated with a gas pipeline network. After the structure is adopted, the blast furnace gas is purified and desulfurized through a purifying and desulfurizing device, then is subjected to CO 2 separation and purification through a CO 2 separation and purifying device to obtain CO 2 -enriched product gas and CO 2 -enriched product gas, the CO 2 -enriched product gas is subjected to CO separation and purification through a first pressure swing adsorption device to obtain 1# CO-enriched product gas and carbon oxide-depleted tail gas, the 1# CO-enriched product gas is sent to a second gas mixing device to be mixed with the 2# CO-enriched product gas and H 2 -enriched gas and then is sent to a blast furnace to be used as gas, the CO 2 -enriched product gas is sent to the first gas mixing device, and the carbon oxide-depleted tail gas is sent to a gas pipe network.
The comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas is shown in fig. 1, wherein a coke oven gas pipe network is communicated with an inlet of a purification and separation device through a pipeline, an outlet of the purification and separation device is communicated with an inlet of a methanation device through a third compressor, an outlet of the methanation device is communicated with an inlet of a second pressure swing adsorption device, a methane-rich gas outlet of the second pressure swing adsorption device is communicated with an inlet of a first gas mixing device, an outlet of the first gas mixing device is communicated with an inlet of a dry reforming reaction device through a fourth compressor, an outlet of the dry reforming reaction device is communicated with an inlet of a third pressure swing adsorption device, a lean CO gas outlet of the third pressure swing adsorption device is communicated with an inlet of the third gas mixing device, an outlet of the third gas mixing device is communicated with an inlet of a methanol synthesis device through a fifth compressor, an outlet of the methanol synthesis device is communicated with an inlet of a rectifying device, a purge gas outlet of the methanol synthesis device is communicated with an inlet of the third gas mixing device, a rich H 2 gas outlet of the second pressure swing adsorption device is communicated with an inlet of the second gas mixing device, and a CO gas outlet of the third pressure swing adsorption device is communicated with an inlet of the second gas mixing device. After the structure is adopted, coke oven gas is purified and separated through a purifying and separating device, enters a methanation device for methanation reaction, enters a second pressure swing adsorption device for separation of gas to obtain methane-rich gas and H 2 -rich gas, the methane-rich gas and the CO 2 -rich product gas are mixed in a first gas mixing device and enter a dry reforming reaction device for dry reforming reaction to obtain synthesis gas, partial CO of the synthesis gas is separated through a third pressure swing adsorption device to obtain 2# CO-rich product gas and CO-lean product gas, the CO-lean product gas enters a methanol synthesis device for synthesis into crude methanol, the crude methanol enters a rectifying device for rectification to obtain a methanol product, methanol purge gas generated by the methanol synthesis device is returned to the third gas mixing device for mixing with the CO-lean product gas for methanol synthesis again, and the H 2 -rich gas 2# CO-rich product gas enters the second gas mixing device for mixing with the 1# CO-rich product gas and is sent into a blast furnace for use as gas.
As shown in fig. 1, the production process of the comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas comprises the following steps:
(1) Carrying out CO 2 separation and purification on blast furnace gas after purifying and desulfurizing to obtain CO 2 -rich product gas and CO 2 -lean product gas, carrying out CO separation and purification on the CO 2 -lean product gas to obtain No. 1 CO-rich product gas and carbon oxide-lean tail gas, and returning the carbon oxide-lean tail gas to a gas pipe network for combustion power generation;
The main composition of the blast furnace gas is （vol）：CO 20～30%、CO2 15～25%、CH4 0.4～1.5%、H21.5～3.5%、O2 0.2～1.0%、N2 46～60%. the blast furnace gas is purified and desulfurized until the sulfur content is less than 0.1ppm and the oxygen content is less than 300ppm. The CO 2 content in the CO 2 -enriched product gas is more than 85vol%, and the CO content in the 1# CO-enriched product gas is more than 85vol%.
(2) Purifying and separating coke oven gas, performing methanation reaction, and separating gas to obtain methane-rich gas and H 2 -rich gas;
The main composition of the coke oven gas is (vol) H 2 50～65%、CO 4～10%、CO2 1～6%、CH4 15～23%,O2～1%、N2 -8%. The coke oven gas is purified and separated until the sulfur content is less than 0.1ppm and the oxygen content is less than 300ppm. The methanation reaction mainly comprises CO+3H 2→CH4+H2O,CO2+4H2→CH4+2H2 O, wherein the methanation reaction condition is that the reaction temperature is 500-700 ℃ and the pressure is 1-4 MPa. The separation adopts one or a combination of more of pressure swing adsorption separation, membrane separation and cryogenic separation. The content of CH 4 in the methane-rich gas is more than 85vol%, and the main composition of the H 2 -rich gas is (vol): H 2＞80%、CO＜10ppm、CO2＜20ppm、CH4 0.5～3%、O2 <10ppm.
(3) The CO-rich 2 product gas and methane-rich gas are subjected to dry reforming reaction to obtain synthesis gas, and partial CO is separated from the synthesis gas to obtain a 2# CO-rich product gas and a CO-lean product gas;
The dry reforming reaction mainly comprises CO 2+CH4→2CO+2H2, wherein the reaction condition of the dry reforming reaction is that the reaction temperature is 600-1200 ℃ and the pressure is 0.1-4 MPa, the catalyst adopted in the dry reforming reaction comprises one or a combination of a plurality of platinum-based catalyst, rhodium-based catalyst, palladium-based catalyst, ruthenium-based catalyst, nickel-based catalyst and copper-based catalyst, the CO 2 -enriched product gas is methane-enriched gas=1:0.5-5, and the CO/H 2 =0.2-5:1 volume ratio in the synthesis gas. The CO content in the 2# CO-rich product gas is more than 90vol%, and the molar ratio of hydrogen to carbon in the CO-lean product gas is H/C=2-2.8:1.
(4) Methanol synthesis is carried out on the lean CO product gas to obtain a methanol product, and the methanol purge gas generated by the methanol synthesis is returned to be mixed with the lean CO product gas for methanol synthesis again;
The main reaction of the methanol synthesis is that CO+2H2H 2 - & gt CH3OH, the reaction condition of the methanol synthesis is that the temperature is 200-300 ℃, the pressure is 2-8 MPa, and the purity of the methanol product is more than 98%.
(5) And mixing the No. 1 CO-rich product gas, the No. 2 CO-rich product gas and the H 2 -rich gas, and then spraying back to the blast furnace for recycling.
The specific production example is that the comprehensive utilization system for synthesizing the methanol by using the blast furnace gas and the coke oven gas is adopted for production.
Blast furnace gas and coke oven gas of a certain iron and steel company are used as raw materials:
the main composition of the blast furnace gas is CO 26%, CO 2 20%、CH4 0.75%、H2 2.1%、O2 0.43%、N2 49.2.2%, the temperature is 40 ℃ and the pressure is 6000Pa (A), and the flow is 111000Nm 3/h;
the main composition of the coke oven gas is H 2 60%、CO 6%、CO2 2%、CH4 22%、O2 0.72%、N2 7.6.6%, the temperature is 40 ℃ and the pressure is 6000Pa (A), and the flow rate is 275000Nm 3/H;
the scale of the device is 40 ten thousand tons of methanol produced annually, and the operation time of the device is 8000 h/year.
As shown in fig. 1, the method comprises the following steps:
(1) Separating and purifying CO 2 and CO by using blast furnace gas:
the method comprises the steps of purifying and desulfurizing blast furnace gas with the flow rate of 111000Nm 3/h to remove sulfur and oxygen in the gas until the sulfur content is less than 0.1ppm and the oxygen content is less than 300ppm, feeding the blast furnace gas into a CO 2 separation and purification device to circularly absorb organic amine, enabling the blast furnace gas in the device to be in countercurrent contact with N-methyldiethanolamine (MEDA-CO 2), absorbing CO 2 through mass transfer and chemical reaction, reducing pressure, heating and desorbing to obtain CO 2 -rich product gas with the flow rate of 24000Nm 3/h、CO2 concentration of 91.1%, and then conveying the CO 2 -rich product gas to a first gas mixing device to be mixed with methane-rich gas. And the adsorption gas generated by the CO 2 separation and purification device enters a first pressure swing adsorption device to perform pressure swing adsorption purification on CO, so as to obtain a No. 1 CO-rich product gas with the flow rate of 30000Nm 3/h and the CO concentration of 96.2%.
(2) Methanation of coke oven gas to obtain methane-rich gas and H 2 -rich gas:
The method comprises the steps of purifying and separating coke oven gas with flow rate of 275000Nm 3/H, removing sulfur in the gas to be less than 0.1ppm and oxygen content to be less than 300ppm, then introducing the coke oven gas into a methanation device for reaction, converting CO, CO 2 and H 2 in the device into methane under the catalysis of 650 ℃ and 2.0MPa, introducing the coke oven gas into a second pressure swing adsorption device for hydrogen extraction and gas separation, and obtaining methane-rich gas with flow rate of 70000Nm 3/h、CH4 concentration of 88.26% and H-rich 2 gas with flow rate of 205000Nm 3/h、H2 concentration of 81.05%.
(3) The dry reforming reaction yields synthesis gas:
Methane-rich gas with flow rate of 70000Nm 3/h、CH4 and concentration of 88.26% and CO 2 -rich product gas with flow rate of 24000Nm 3/h、CO2 and concentration of 91.1% are mixed, and then dry reforming reaction is carried out through a nickel-based catalyst under the conditions of 800 ℃ and 1.0MPa, so as to obtain synthetic gas with flow rate of 170000Nm 3/H and concentration of 49.0% and 49.0% of CO and H 2 respectively. The synthesis gas was sent to a third pressure swing adsorption unit for pressure swing adsorption extraction of a portion of the CO to obtain a 2# CO-enriched product gas having a flow rate of 48000Nm 3/H and a CO concentration of 90.45%, and a CO-depleted product gas having a flow rate of 120000Nm 3/H and CO and H 2 concentrations of 33.0% and 66.0%, respectively.
(4) Methanol synthesis:
The low-CO product gas with the flow rate of 120000Nm 3/H and the concentration of CO and H 2 of 33.0 percent and 66.0 percent is respectively subjected to methanol synthesis by a copper-based catalyst at the temperature of 250 ℃ and the pressure of 6MPa to prepare crude methanol, and the synthesized crude methanol is conveyed to a rectifying device by a pump to separate water to prepare a methanol product (the purity is 99 percent) with the yield of 40 ten thousand tons/year. The methanol purge gas generated by the methanol synthesis device is returned to the methanol synthesis device.
(5) Back-spraying blast furnace:
The gas mixture was mixed with a flow rate of 30000Nm 3/H, a CO concentration of 96.2% in the CO-rich product gas # 1, a flow rate of 48000Nm 3/H, a CO concentration of 90.45% in the CO-rich product gas # 2, and a flow rate of 205000Nm 3/h、H2% in the H-rich 2, and a concentration of 81.05% in the CO-rich product gas, and was returned to the blast furnace.
(6) Tail gas treatment:
The carbon-poor oxide tail gas of the blast furnace gas from which CO and CO 2 are removed is returned to a gas pipe network for each process of steel production and fuel gas use of a power generation device.
Claims (3)
1. A comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas is characterized by comprising a purification desulfurization device, a CO 2 separation and purification device, a first pressure swing adsorption device, a purification separation device, a methanation device, a second pressure swing adsorption device, a dry reforming reaction device, a third pressure swing adsorption device, a methanol synthesis device, a rectification device, a compressor, a first gas mixing device, a second gas mixing device and a blast furnace, wherein a blast furnace gas pipe network is sequentially communicated with the purification desulfurization device and the CO 2 separation and purification device through a pipeline, a lean CO 2 gas outlet of the CO 2 separation and purification device is communicated with an inlet of the first pressure swing adsorption device, a rich CO 2 gas outlet of the first pressure swing adsorption device is communicated with a gas inlet of the blast furnace through the second pressure swing adsorption device, a rich H 2 gas outlet of the second pressure swing adsorption device is communicated with an inlet of the second gas mixing device, a rich methane gas outlet of the first gas mixing device is communicated with an inlet of the first gas mixing device, a rich CO gas outlet of the third pressure swing adsorption device is sequentially communicated with a gas inlet of the third pressure swing adsorption device, and a rich CO gas outlet of the third pressure swing adsorption device is sequentially communicated with the third pressure swing adsorption device.
2. The comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas, which is disclosed in claim 1, is characterized in that a third gas mixing device is further arranged between the third pressure swing adsorption device and the methanol synthesis device, and a purge gas outlet of the methanol synthesis device is communicated with an inlet of the third gas mixing device.
3. The comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas according to claim 1 or 2, wherein the tail gas outlet of the first pressure swing adsorption device is communicated with a gas pipe network.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202421214405.0U CN222434398U (en) | 2024-05-30 | 2024-05-30 | Comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas |
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| CN202421214405.0U CN222434398U (en) | 2024-05-30 | 2024-05-30 | Comprehensive utilization system for synthesizing methanol from blast furnace gas and coke oven gas |
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