CN109316900B - Comprehensive utilization method of converter tail gas - Google Patents
Comprehensive utilization method of converter tail gas Download PDFInfo
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- CN109316900B CN109316900B CN201811347186.2A CN201811347186A CN109316900B CN 109316900 B CN109316900 B CN 109316900B CN 201811347186 A CN201811347186 A CN 201811347186A CN 109316900 B CN109316900 B CN 109316900B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/502—Carbon monoxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
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- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
The application discloses a comprehensive utilization method of converter tail gas, which comprises the following steps: after the converter tail gas is cooled, dedusted and deeply purified, different pressure swing adsorbents are sequentially used for CO2And CO purification and recovery, the obtained gas has high purity and high recovery rate, and CO2The method can be used for commodity sale, and the high-purity CO can be used for producing carbonyl compounds; the adsorbent used for deep purification contains activated carbon and iron, does not contain other impurity elements, and can be used for preparing steelmaking raw materials after adsorption, so that the waste of energy is reduced. The method of the invention fully utilizes the heat of the converter tail gas and the tail gas components, reduces the environmental pollution, increases the economic benefit, realizes the recycling and economic utilization of resources, and has the advantages of energy saving, environmental protection and simplicity.
Description
Technical Field
The invention relates to a comprehensive utilization method of converter tail gas.
Background
The converter tail gas contains rich carbon monoxide, and the carbon monoxide has a higher combustion value. At present, the measures generally adopted by metallurgical enterprises for treating pollution and improving economic benefits are to recycle the fuel to be used for furnace heating, power generation and the like, the added value of products is not high, and CO generated by combustion is low2The greenhouse level is further increased. Facing increasingly severe environment protection situation and emission reduction requirement, enterprises can treat work due to flue gasA large amount of scientific research funds and equipment are invested, and the economic benefit is further improved.
Enterprises need a method for economically and comprehensively utilizing converter tail gas in an environment-friendly way.
Disclosure of Invention
Aiming at the defects in the prior art, the invention aims to provide a comprehensive utilization method of converter tail gas, which is based on the characteristic that the composition of the converter tail gas is complex, and adopts the steps of firstly deeply purifying and then respectively separating high-purity CO2And CO, and the method makes full use of the heat and the tail gas components of the converter tail gas, reduces the environmental pollution, increases the economic benefit, realizes the recycling economic utilization of resources, and has the advantages of energy conservation, environmental protection and simplicity.
In order to achieve the above purposes, the technical scheme adopted by the invention is as follows:
a comprehensive utilization method of converter tail gas comprises the following steps:
s1, cooling and dedusting the converter tail gas to obtain a first mixed gas;
s2, deeply purifying the first mixed gas to remove CO in the converter tail gas2CO and N2An external gas to obtain a second mixed gas;
CO in the converter tail gas2CO and N2The other gases include: h2S、COS、CS2、PH3、AsH3HF, HCN, HCl, metal carbonyls, and O2；
S3, adopting a pressure swing adsorption method to adsorb CO in the second mixed gas2Separated from water for producing CO2The rest gas is third mixed gas;
s4, separating CO in the third mixed gas by adopting a pressure swing adsorption method, directly using the third mixed gas for preparing carbonyl compounds, and using the rest gas as fourth mixed gas;
s5, mixing the fourth mixed gas with the first mixed gas, and circularly performing the steps S2-S5.
In one embodiment of the above method, in step S2,the deep purification comprises the following steps: carrying out constant-temperature pressure swing adsorption on the first mixed gas by using a first adsorbent to remove CO in the tail gas of the converter2CO and N2Further using a catalyst to perform fine dearsenification on the other gases;
the first adsorbent is prepared by taking activated carbon as a carrier and loading sufficient iron or iron compound, so that the surface of the first adsorbent is alkaline and reductive to remove CO in the converter tail gas2CO and N2An external gas;
adsorbing CO in the converter tail gas2CO and N2And mixing the first adsorbent of the other gas with the steelmaking raw material to perform steelmaking to obtain converter tail gas, and repeating the steps S1-S5.
The activated carbon in the first adsorbent is used for adsorbing gas, and the iron or iron compound is used for enabling CO in converter tail gas2CO and N2The first adsorbent can be directly used as one part of steelmaking raw materials for steelmaking without regeneration after adsorption, so that the raw material assembly is convenient, the steelmaking recycling is realized, no new equipment is added, no new pollution is generated, and the energy consumption is very low compared with other purification methods.
In another embodiment, in step S2, the deep purification further includes the steps of: adsorbing CO in the converter tail gas2CO and N2Heating the first adsorbent of the other gas to 200-250 ℃ to desorb CO in the converter tail gas2CO and N2And (c) an external gas.
In this embodiment, in step S2, the heating is performed by using the heat of the converter off-gas in step S1. One specific implementation is as follows: the method comprises the steps that a high-heat-conduction material (such as corrosion-resistant metal alloy) is used on the peripheral side wall of the first adsorbent placing position of an adsorption tower where a first adsorbent is located, a heating cavity is arranged outside the side wall which uses the high-heat-conduction material, converter tail gas is introduced into the heating cavity, and heat of the converter tail gas is conducted to the first adsorbent.
In the above method, in step S2, the first adsorbent is loaded with 20% to 30% by weight of iron or iron compound. The ratio is such that CO2Is as small as possible and is capable of removing other gases. The detection shows that the content of sulfur, phosphorus and arsenic in the gas treated by the step is lower than 1ppm and the content of CO is lower than 1ppm2The loss was the lowest.
In the above method, in step S2, the adsorption is performed under the conditions of a pressure of 0.8 to 1.2MPa and a temperature of normal temperature; the aperture of the first adsorbent is 2-4nm, and the ratio of the gas flow of the first mixed gas to the amount of the first adsorbent is (5-10) sccm:1 g.
In the above method, in step S3, the pressure swing adsorption process is performed using a second adsorbent,
the second adsorbent is prepared by taking active carbon as a carrier and loading 40-60% of nitrate and 40-60% of chloride by weight percentage;
the nitrate is preferably calcium nitrate and the chloride is preferably potassium chloride.
In the above method, in step S3, the pressure swing adsorption method is performed at normal temperature, with an adsorption pressure of 3atm to 6atm and a desorption pressure of 0.1 to 1 atm;
the aperture of the second adsorbent is 1.0-1.5nm, and the ratio of the gas flow of the second mixed gas to the using amount of the second adsorbent is (3-7) sccm:1 g.
In the above method, in step S4, the pressure swing adsorption process is performed using a third adsorbent,
the third adsorbent is PU-1 copper-based adsorbent (Beijing McPioneer technologies, Inc.), the adsorption temperature of the pressure swing adsorption method is 70-90 ℃, preferably 80 ℃, and the adsorption pressure of the pressure swing adsorption method is 10 MPa; the ratio of the gas flow of the third mixed gas to the amount of the third adsorbent is (15-20) sccm:1 g.
The comprehensive utilization method of the converter tail gas has the following beneficial effects:
1. based on the characteristic of complex composition of converter tail gas, the method firstly adopts deep purification to remove compounds such as sulfur, phosphorus, arsenic and the like, and then a pressure swing adsorption method is used for separating high-purity CO respectively2And CO, high purity CO2Can be used for commodity sale, and the high-purity CO can be used for producing carbonyl compounds.
2. The adsorbent used for deep purification contains activated carbon, iron and compounds thereof, does not contain other impurity elements, and can be used for preparing steelmaking raw materials after adsorption, thereby reducing the waste of energy.
3. The adsorbent used for deep purification can be desorbed after adsorption, and heating during desorption can be carried out by utilizing the heat of the converter tail gas before temperature reduction.
4. The method has reasonable parameter setting, high operation efficiency of the whole system and CO2And the purity and recovery rate of CO are high.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the application and together with the description serve to explain the application and not to limit the application. In the drawings:
FIG. 1 is a process flow of a comprehensive utilization method of converter tail gas.
Detailed Description
In order to more clearly explain the overall concept of the present application, the following detailed description is given by way of example in conjunction with the accompanying drawings.
Example 1 comprehensive utilization method of converter off-gas
Influence of first and second mixed gas flow on the result
As shown in fig. 1, the method for comprehensively utilizing converter off-gas provided by this embodiment includes the following steps:
s1, converting the converter tail gas (average heating value is 7500 kJ/m) in the steel-making production3The gas composition (volume fraction) is: 70% CO, CO210% of N210% of O20.5% of H2S is 1.0%, COS0.5% of CS20.2% pH31.5% of AsH32.0 percent of HF, 0.3 percent of HCN, 0.75 percent of HCl and 0.5 percent of carbonyl metal are subjected to temperature reduction and dust removal (dry method) to obtain a first mixed gas;
s2, deeply purifying the first mixed gas to remove CO in the converter tail gas2CO and N2An external gas to obtain a second mixed gas;
the deep purification comprises the following steps: the first mixed gas is adsorbed by a first adsorbent at constant temperature (normal temperature) and pressure swing (0.8MPa adsorption, unadsorbed gas in a 0.01MPa release tower), and CO in the converter tail gas is removed2CO and N2Further using a catalyst to perform fine dearsenification on the other gases;
the first adsorbent is prepared by taking active carbon as a carrier and loading 20 wt% of iron, so that the surface of the first adsorbent is alkaline and reductive to remove CO in the converter tail gas2CO and N2An external gas; the aperture of the first adsorbent is 3nm, and the gas flow rate of the first mixed gas and the dosage of the first adsorbent are respectively (2, 4, 8, 12) sccm:1 g.
Adsorbing CO in the converter tail gas2CO and N2And mixing the first adsorbent of the other gas with the steelmaking raw material to perform steelmaking to obtain converter tail gas, and repeating the steps S1-S5 on the converter tail gas.
S3, adopting a pressure swing adsorption method to adsorb CO in the second mixed gas2Separating with water, detecting CO after desorption2And for producing CO2The rest gas is third mixed gas;
the pressure swing adsorption method is carried out by using a second adsorbent, wherein the second adsorbent takes activated carbon as a carrier and is loaded with 50 weight percent of calcium nitrate and 50 weight percent of potassium chloride;
the pressure swing adsorption method has the temperature of normal temperature, the adsorption pressure of 3.5atm and the desorption pressure of 0.5 atm;
the aperture of the second adsorbent is 1.0nm, and the ratio of the gas flow of the second mixed gas to the using amount of the second adsorbent is 5sccm:1 g;
s4, separating CO in the third mixed gas by adopting a pressure swing adsorption method, detecting the purity and recovery rate of the desorbed CO, and directly using the CO for preparing carbonyl compounds (oxalic acid, methanol or formamide), wherein the rest gas is a fourth mixed gas;
the pressure swing adsorption method is carried out by using a third adsorbent, the third adsorbent is a PU-1 copper-based adsorbent (Beijing Pidao McCustoms Co., Ltd.), the operation is carried out according to the specification of the adsorbent, the adsorption temperature of the pressure swing adsorption method is 80 ℃, and the adsorption pressure of the pressure swing adsorption method is 10 MPa;
the gas flow rate of the third mixed gas and the dosage of the third adsorbent are in proportion
18sccm:1g；
S5, mixing the fourth mixed gas with the first mixed gas, and circularly performing the steps S2-S5.
The results are shown in table 1 and show that: the flow rate of the first mixed gas is too low, CO2Low recovery rate, high flow rate of the first mixed gas, and high CO content2The purity is reduced but the purity and recovery of CO is not greatly affected.
TABLE 1 influence of the first mixture gas flow on the results
Influence of the second and the second mixed gas flow on the result
The method is carried out according to the method of the first step, and the difference is that:
the ratio of the gas flow of the first mixed gas to the dosage of the first adsorbent is 8sccm:1 g;
the ratio of the gas flow rate of the second mixed gas to the amount of the second adsorbent is (1, 5, 10) sccm:1 g.
The results are shown in table 2 and show that: the second mixed gas has too low a flow rate, CO2Purity is reduced, theOver-high flow of mixed gas, CO2The recovery rate is reduced but the purity and recovery rate of CO are not greatly affected.
TABLE 2 Effect of second mixture gas flow on results
Influence of the third and fourth mixed gas flow rates on the results
The method is carried out according to the method of the first step, and the difference is that:
the ratio of the gas flow of the first mixed gas to the dosage of the first adsorbent is 8sccm:1 g;
the ratio of the gas flow rate of the third mixed gas to the amount of the third adsorbent used was (9, 18, 27) sccm:1 g.
The results are shown in table 3 and show that: the flow of the third mixed gas is too low, the purity of CO is reduced, the flow of the third mixed gas is too high, and the recovery rate of CO is reduced.
TABLE 3 influence of third mixture gas flow on the results
Example 2 comprehensive utilization method of converter tail gas
The comprehensive utilization method of the converter tail gas provided by the embodiment comprises the following steps:
s1, converting the converter tail gas (average heating value is 8000 kJ/m) of steel-making production3CO 50%, CO220% of N220% of O22.0% of H21.5% of S, 0.9% of COS and CS20.6% pH31.0% of AsH32.0%, HF 0.5%, HCN 0.5%, HCl 0.6%, and metal carbonyls 0.4%. ) Obtaining a first mixed gas through temperature reduction and dust removal (dry method);
s2, deeply purifying the first mixed gas to remove CO in the converter tail gas2CO and N2An external gas to obtain a second mixed gas;
the deep purification comprises the following steps: carrying out temperature-changing (normal temperature adsorption, 220 ℃ desorption) pressure-changing (1.2MPa adsorption, 0.01MPa desorption) adsorption on the first mixed gas by using a first adsorbent to remove CO in the converter tail gas2CO and N2Other gases (when the content of S, P, AS in the gas in the monitoring adsorption tower is lower than 1ppm, the adsorption is stopped, the desorption is carried out), and then a catalyst is further used for fine dearsenification;
the first adsorbent is prepared by taking active carbon as a carrier and loading 30 wt% of iron, so that the surface of the first adsorbent is alkaline and reductive to remove CO in the converter tail gas2CO and N2An external gas; the aperture of the first adsorbent is 2nm, and the ratio of the gas flow of the first mixed gas to the consumption of the first adsorbent is 10sccm:1 g;
the desorption temperature is realized by heating, and specifically, the heat of the converter tail gas in the step S1 is used for: the method comprises the steps that a high-heat-conduction material (such as corrosion-resistant stainless steel or nickel-based alloy) is used on the peripheral side wall of the first adsorbent placing position of an adsorption tower where a first adsorbent is located, a heating cavity is arranged outside the side wall using the high-heat-conduction material, converter tail gas is introduced into the heating cavity, and heat of the converter tail gas is conducted to the first adsorbent.
S3, adopting a pressure swing adsorption method to adsorb CO in the second mixed gas2Separating with water, detecting CO after desorption2Purity and recovery of for CO production2The rest gas is third mixed gas;
the pressure swing adsorption method is carried out by using a second adsorbent, wherein the second adsorbent takes active carbon as a carrier and is loaded with 40 weight percent of calcium nitrate and 60 weight percent of potassium chloride;
the pressure swing adsorption method has the temperature of normal temperature, the adsorption pressure of 5.5atm and the desorption pressure of 0.1 atm;
the aperture of the second adsorbent is 1.0nm, and the ratio of the gas flow of the second mixed gas to the using amount of the second adsorbent is 7sccm:1 g;
s4, separating CO in the third mixed gas by adopting a pressure swing adsorption method, detecting the purity and recovery rate of the desorbed CO, and directly using the CO for preparing carbonyl compounds (oxalic acid, methanol or formamide), wherein the rest gas is a fourth mixed gas;
the pressure swing adsorption method is carried out by using a third adsorbent, wherein the third adsorbent is a PU-1 copper-based adsorbent (McCuk, Beijing, McMc.), the adsorption temperature of the pressure swing adsorption method is 70 ℃ according to the specification of the adsorbent, and the adsorption pressure of the pressure swing adsorption method is 10 MPa;
the gas flow rate of the third mixed gas and the dosage of the third adsorbent are in a ratio of 20sccm:1 g;
s5, mixing the fourth mixed gas with the first mixed gas, and circularly performing the steps S2-S5.
Second, result in
CO obtained in this example2The purity is 96 percent, and the recovery rate is 96 percent; the purity of the obtained CO is 98%, and the recovery rate is 97%.
Comparative example 1 first sorbent composition change to CO2Effect of recovery
The method in the first step of the embodiment 2 is carried out, and the difference is that:
in step S2, the first adsorbent is prepared by using activated carbon as a carrier and loading 35 wt% of iron, so that the surface of the first adsorbent is alkaline and reducing.
Second, result in
CO obtained in this comparative example2The purity is 96 percent, and the recovery rate is 85 percent; the purity of the obtained CO was 98% and the recovery was 97%.
The results show that too high an iron content in the first adsorbent reduces CO2The recovery rate of (1).
Comparative example 2 Effect of variation of composition of first adsorbent on gas recovery
The method in the first step of the embodiment 2 is carried out, and the difference is that:
in step S2, the first adsorbent is supported by activated carbon as a carrier and loaded with 15 wt% of iron, so that the surface of the first adsorbent is alkaline and reducing.
Second, result in
After the first mixed gas is adsorbed by the first adsorbent in step S2, the S, P, As content failed to achieve the target of less than 1ppm, 10ppm, 12ppm and 20ppm, respectively.
Comparative example 3 Effect of composition change of second adsorbent on gas recovery
The method in the first step of the embodiment 2 is carried out, and the difference is that:
in step S3, the pressure swing adsorption method is performed using a second adsorbent, which is loaded with 35 wt% of calcium nitrate and 65 wt% of potassium chloride, and uses activated carbon as a carrier.
Second, result in
CO obtained in this comparative example2The purity is 98 percent, and the recovery rate is 85 percent; the purity of the obtained CO was 90% and the recovery was 95%.
The results show that a change in the composition of the second adsorbent results in a significant reduction in CO2And thus the purity of the CO.
Comparative example 4 Effect of changes in composition of second adsorbent on gas recovery
The method in the first step of the embodiment 2 is carried out, and the difference is that:
in step S3, the pressure swing adsorption process was performed using a second adsorbent, which was loaded with 50 wt% of different nitrates and 50 wt% of different chlorides, using activated carbon as a carrier, as shown in table 4.
Second, result in
As shown in table 4. The results show that a change in the composition of the second adsorbent results in a significant reduction in CO2And thus the purity of the CO.
TABLE 4 influence of second adsorbent composition change on gas recovery
| Difference in composition of second adsorbent | CO2Purity% | CO2Percent recovery rate% | Purity of CO% | CO recovery rate% |
| 50% calcium nitrate + 50% potassium chloride | 98 | 96 | 98 | 98 |
| 50% copper nitrate + 50% potassium chloride | 97 | 88 | 90 | 96 |
| 50% Zinc nitrate + 50% Potassium chloride | 95 | 85 | 88 | 96 |
| 50% ferric nitrate and 50% potassium chloride | 97 | 80 | 83 | 98 |
| 50% magnesium nitrate + 50% potassium chloride | 96 | 90 | 88 | 96 |
| 50% calcium nitrate + 50% sodium chloride | 95 | 92 | 89 | 95 |
| 50% calcium nitrate + 50% calcium chloride | 96 | 85 | 86 | 97 |
| 50% calcium nitrate + 50% copper chloride | 96 | 87 | 83 | 99 |
| 50% of calcium nitrate and 50% of zinc chloride | 96 | 86 | 84 | 97 |
| 50% calcium nitrate + 50% ferric chloride | 95 | 80 | 82 | 95 |
| 50% of calcium nitrate and 50% of magnesium chloride | 94 | 85 | 83 | 96 |
Those not described in detail in this specification are within the skill of the art. The above description is only an example of the present application and is not intended to limit the present application. Various modifications and changes may occur to those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application should be included in the scope of the claims of the present application.
Claims (7)
1. A comprehensive utilization method of converter tail gas is characterized by comprising the following steps:
s1, cooling and dedusting the converter tail gas to obtain a first mixed gas;
s2, deeply purifying the first mixed gas to remove CO in the converter tail gas2CO and N2And (c) obtaining a second mixed gas comprising: carrying out constant-temperature pressure swing adsorption on the first mixed gas by using a first adsorbent to remove CO in the tail gas of the converter2CO and N2Further using a catalyst to perform fine dearsenification on the other gases;
wherein the first adsorbent is prepared by taking activated carbon as a carrier and loading 20-30 wt% of iron or iron compound to make the surface of the first adsorbent alkaline or reductive;
s3, adopting a pressure swing adsorption method to adsorb CO in the second mixed gas2Separated from water for producing CO2The rest gas is third mixed gas;
s4, separating CO in the third mixed gas by adopting a pressure swing adsorption method, directly using the third mixed gas for preparing carbonyl compounds, and using the rest gas as fourth mixed gas;
s5, mixing the fourth mixed gas with the first mixed gas, and circularly performing the steps S2-S5;
in step S3, the pressure swing adsorption method is performed using a second adsorbent, which is loaded with 40-60 wt% of nitrate and 40-60 wt% of chloride, and uses activated carbon as a carrier; the nitrate is calcium nitrate and the chloride is potassium chloride.
2. The method of claim 1, wherein: step S2 further includes: adsorbing CO in the converter tail gas2CO and N2Heating the first adsorbent of the other gas to 200-250 ℃ to desorb CO in the converter tail gas2CO and N2And (c) an external gas.
3. The method of claim 2, wherein: in step S2, the heating is performed by using the heat of the converter off-gas in step S1.
4. The method of any one of claims 2-3, wherein: in step S2, the adsorption is performed under the conditions of a pressure of 0.8 to 1.2MPa and a temperature of normal temperature, the pore diameter of the first adsorbent is 2 to 4nm, and the ratio of the gas flow rate of the first mixed gas to the amount of the first adsorbent is (5 to 10) sccm:1 g.
5. The method of claim 1, wherein: in step S3, the pressure swing adsorption method is at normal temperature, the adsorption pressure is 3atm-6atm, and the desorption pressure is 0.1-1 atm;
the aperture of the second adsorbent is 1.0-1.5nm, and the ratio of the gas flow of the second mixed gas to the using amount of the second adsorbent is (3-7) sccm:1 g.
6. The method of any one of claims 1-3, wherein: in step S4, the pressure swing adsorption process is performed using a third adsorbent, which is a PU-1 copper-based adsorbent; the adsorption temperature of the pressure swing adsorption method is 70-90 ℃, and the adsorption pressure of the pressure swing adsorption method is 10 MPa; the ratio of the gas flow of the third mixed gas to the amount of the third adsorbent is (15-20) sccm:1 g.
7. The method of any one of claims 1 to 3, wherein the composition of gases in the converter off-gas is: 50-70% of CO, CO210-20% of N210-20% of O20.5-2.0%, H21.0-1.5% of S, 0.5-0.9% of COS, and CS20.2-0.6% pH30.8-1.5%, AsH31.5-2.0 percent of HF, 0.3-0.5 percent of HCN, 0.4-0.78 percent of HCl and 0.3-0.5 percent of carbonyl metal.
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