Method for total sulfur removal from blast furnace gas

Abstract

The present application relates to a kind of blast furnace gas total sulfur removal methods, comprising the following steps: (1) blast furnace gas is passed into hydrolysis tower filled with catalyst, and COS and CS2 in blast furnace gas are converted into H2S by the action of the catalyst and hydrolysis reaction;(2) then the H2S formed by conversion is passed into dry adsorption tower filled with desulfurizer with blast furnace gas to carry out desulfurization treatment and realize total sulfur removal;The catalyst is modified carbon material active alumina loaded;The desulfurizer is modified porous ferric oxide.The present application can remove most of the sulfur in blast furnace gas, and through hydrolysis catalysis, not only COS and CS2 can be removed efficiently, and H2S produced by subsequent desulfurizer can be removed with high efficiency, to realize blast furnace gas total desulfurization.

Description

Technical Field

[0001] This invention relates to the field of desulfurization technology, specifically to a method for the complete removal of sulfur from blast furnace gas. Background Technology

[0002] Blast furnace gas mainly consists of nitrogen, hydrogen, carbon monoxide, carbon dioxide, and methane, and also contains small amounts of hydrogen sulfide, organic sulfur, and dust. The total sulfur content in blast furnace gas is 60–160 mg / Nm³. 3 It contains 20%–40% hydrogen sulfide and 60%–80% organic sulfur, with carbonyl sulfur (COS) being the main organic sulfur and trace amounts of CS2.

[0003] Carbonyl sulfide, also known as carbon oxysulfide or carbonyl sulfide, has the molecular formula COS or OCS. It has a simple, linear molecular structure, with oxygen, carbon, and sulfur atoms linked by double bonds. The compact, approximately ellipsoidal molecular structure contributes to its relatively stable chemical properties. However, it exhibits poor reactivity in chemical absorption, even causing solution degradation. In physical absorption, COS and CO2 have similar solubility, making selective separation difficult. Because COS is not easily dissociated or liquefied, it is difficult to remove using conventional desulfurization methods.

[0004] Conventional methods for removing COS involve hydrogenation or hydrolysis to convert it into H2S, which is then removed. COS and CS2 react with trace amounts of water vapor in the feed gas to form H2S under the action of a hydrolysis catalyst, as shown in the following reaction equation:

[0005] COS+H2O→H2S+CO2, CS2+2H2O→2H2S+CO2;

[0006] The above reaction is a first-order reversible exothermic reaction. A low-temperature environment favors the reaction proceeding to the right, increasing the equilibrium conversion rate. Therefore, industrially, while maintaining a certain rate, it is desirable to minimize the hydrolysis reaction temperature, as high temperatures can easily lead to oxygen poisoning of the hydrolysis catalyst. Room-temperature catalysts (operating temperatures 30–100℃) can only remove COS, while medium-temperature catalysts (operating temperatures 100–250℃) can remove both COS and CS2.

[0007] The main technical routes for controlling sulfur emissions from blast furnace gas include front-end control (removing sulfur from the blast furnace gas) and end-end control (installing desulfurization and denitrification devices at the user end after blast furnace gas combustion). Front-end control involves centralized treatment before user consumption, controlling the sulfur content in the gas to within acceptable limits after combustion. This method involves centralized equipment and lower investment compared to end-end control. If end-end control is used, both organic and inorganic sulfur are converted into SO2 after blast furnace gas combustion and emitted into the atmosphere with the flue gas. Therefore, desulfurization facilities need to be installed in the blast furnace gas-using section. Given the numerous and dispersed downstream users of blast furnace gas, end-end treatment equipment would require significant investment, be difficult to operate and manage, and have challenging desulfurization byproducts.

[0008] Therefore, how to treat blast furnace gas at its source, reduce SO2 emissions from downstream users, and achieve front-end desulfurization control of blast furnace gas is the technical problem that this invention aims to solve. Summary of the Invention

[0009] To address the aforementioned technical problems, a method for complete sulfur removal from blast furnace gas is provided. This invention can remove the vast majority of sulfur from blast furnace gas. Through hydrolysis catalysis, not only can COS and CS2 be efficiently removed, but the subsequent desulfurization agent can also efficiently remove H2S generated from the conversion of COS and CS2, achieving complete desulfurization of blast furnace gas.

[0010] To achieve the above objectives, the present invention is implemented through the following technical solution:

[0011] A method for removing total sulfur from blast furnace gas includes the following steps:

[0012] (1) Blast furnace gas is introduced into a hydrolysis tower filled with catalyst, so that COS and CS2 in the blast furnace gas are hydrolyzed and converted into H2S under the action of the catalyst.

[0013] (2) Then the H2S formed by conversion is introduced together with the blast furnace gas into a dry adsorption tower filled with desulfurizing agent for desulfurization treatment to achieve complete sulfur removal;

[0014] The catalyst is activated alumina (γ-Al2O3) supported on modified carbon material; the desulfurizing agent is modified porous ferric oxide.

[0015] Furthermore, the catalyst is prepared by: stirring and reacting activated alumina, starch, urea, and water, mixing them evenly, drying them, and calcining them at 550°C for 3 hours to obtain the first product; mixing and reacting the first product with an aqueous solution of water-soluble carbonate, drying it, and calcining it again at 350°C for 3 hours to obtain activated alumina loaded with modified carbon material.

[0016] Furthermore, the mass ratio of the activated alumina, the starch, and the urea is 5:1:1; the mass ratio of the first product to the water-soluble carbonate is 1:0.1; the water-soluble carbonate is potassium carbonate and / or sodium carbonate; the stirring reaction time is 3 hours, and the mixing reaction time is 8 hours.

[0017] Furthermore, the desulfurizing agent is prepared by: stirring ferric hydroxide, starch, urea, and water, mixing them evenly, drying them, and calcining them at 300°C for 3 hours to obtain a second product; mixing the second product with an aqueous solution of water-soluble carbonate, drying it, and calcining it again at 350°C for 3 hours to obtain modified porous ferric oxide.

[0018] Furthermore, the mass ratio of the ferric hydroxide to the starch and the urea is 5:1:1; the mass ratio of the second product to the water-soluble carbonate is 1:0.1; the water-soluble carbonate is potassium carbonate and / or sodium carbonate; the stirring reaction time is 4 hours, and the mixing reaction time is 3 hours.

[0019] Furthermore, the conditions for the hydrolysis reaction are as follows: under anaerobic conditions, using nitrogen gas with a purity exceeding 4N as the equilibrium gas, at a gas flow rate of 80-100 mL / min, a hydrolysis temperature of 65-80℃, 5-15% water vapor, and a reaction space velocity of 5000-30000 h⁻¹. -1 .

[0020] Furthermore, the reaction conditions for the desulfurization treatment are as follows: under anaerobic conditions, using nitrogen gas with a purity exceeding 4N as the equilibrium gas, at a gas flow rate of 80-100 mL / min, a desulfurization temperature of 50-100℃, 5-15% water vapor, and a reaction space velocity of 5000-30000 h⁻¹. -1 .

[0021] Furthermore, the catalyst is packed in the hydrolysis tower at a rate of at least 3% of the tower height.

[0022] Furthermore, the amount of desulfurizing agent packed in the dry adsorption tower is at least 3% of the tower height. Generally, the amount of catalyst or desulfurizing agent packed is the volume that fills that height of the tower.

[0023] Beneficial technical effects:

[0024] This invention provides a catalyst for hydrolyzing organic sulfur in blast furnace gas by co-modifying activated alumina with starch and urea and loading it with potassium as the active ingredient. It also provides a desulfurizing agent for adsorbing inorganic sulfur generated from the conversion of organic sulfur by co-modifying ferric oxide with starch and urea and loading it with potassium as the active ingredient. Applying these catalysts to the removal of both organic and inorganic sulfur from blast furnace gas can achieve the goal of total sulfur removal, addressing the problem of excessive sulfur dioxide in actual production at its source. The catalyst of this invention can achieve both adsorption and catalysis of organic sulfur, while the desulfurizing agent can remove inorganic sulfur. It boasts advantages such as simple preparation method and low cost, and can be widely used in actual factories for the removal of organic sulfur, especially carbonyl sulfur and H2S. Attached Figure Description

[0025] Figure 1 This is a schematic diagram of the process route of the present invention. Detailed Implementation

[0026] The technical solutions of the present invention will be clearly and completely described below with reference to the embodiments and accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The following description of at least one exemplary embodiment is merely illustrative and is in no way intended to limit the present invention or its application or use. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are within the scope of protection of the present invention.

[0027] Unless otherwise specifically stated, the numerical values ​​set forth in these embodiments do not limit the scope of the invention. Techniques and methods known to those skilled in the art may not be discussed in detail, but where appropriate, such techniques and methods should be considered part of the specification. In all examples shown and discussed herein, any specific values ​​should be interpreted as merely exemplary and not as limitations. Therefore, other examples of exemplary embodiments may have different values.

[0028] Furthermore, it should be noted that the use of terms such as "first" and "second" to define intermediate products is merely for the purpose of distinguishing intermediate products generated in each step. Unless otherwise stated, the above terms have no special meaning and therefore should not be construed as limiting the scope of protection of this invention.

[0029] Experimental methods not specifically described in the following examples are generally determined according to national standards; if no corresponding national standard exists, they are performed according to generally accepted international standards or the standards proposed by relevant enterprises. Unless otherwise stated, all parts are parts by weight, and all percentages are weight percentages.

[0030] The process flow diagram of the blast furnace gas total sulfur removal method of the present invention is shown below. Figure 1 As shown, in actual industrial production, the blast furnace gas is processed sequentially through dust removal, TRT treatment, catalytic hydrolysis, and dry adsorption to obtain clean blast furnace gas; or the blast furnace gas is processed sequentially through dust removal, catalytic hydrolysis, TRT treatment, and dry adsorption to obtain clean blast furnace gas.

[0031] The following experimental procedure uses a mixed gas with a total sulfur content of 160 mg / L, containing 24% H2S, 70% COS, and 6% CS2 to simulate blast furnace gas.

[0032] Example 1

[0033] A method for removing total sulfur from blast furnace gas includes the following steps:

[0034] Simulated blast furnace gas: total sulfur content is 160 mg / L, including 24% H2S, 70% COS, and 6% CS2;

[0035] (1) Simulated blast furnace gas is introduced into a hydrolysis tower filled with a catalyst, so that COS and CS2 in the blast furnace gas are hydrolyzed into H2S under the action of the catalyst. The conditions for the hydrolysis reaction are: under anaerobic conditions, with nitrogen gas of 99.999% purity as the equilibrium gas, a gas flow rate of 100 mL / min, a hydrolysis temperature of 70℃, 15% water vapor, and a reaction space velocity of 5000 h⁻¹. -1 The catalyst is loaded into the hydrolysis tower at a rate of 8% of the tower height.

[0036] (2) The H2S formed by the conversion is then introduced along with the blast furnace gas into a dry adsorption tower filled with desulfurizing agent for desulfurization treatment. The reaction conditions for the desulfurization treatment are: under anaerobic conditions, with nitrogen gas of 99.999% purity as the balance gas, a gas flow rate of 100 mL / min, a desulfurization temperature of 70℃, 15% water vapor, and a reaction space velocity of 5000 h⁻¹. -1 The desulfurizing agent is loaded into the dry adsorption tower at a rate of 8% of the tower height to achieve complete sulfur removal.

[0037] The catalyst mentioned in step 1 is activated alumina supported on modified carbon material. The preparation method is as follows: activated alumina microspheres (γ-Al2O3), starch, and urea are weighed and mixed in a mass ratio of 5:1:1. Deionized water is added and the mixture is stirred at a speed of at least 500 rpm for 3 hours. After mixing evenly, the mixture is dried at 80°C and calcined at 550°C for 3 hours to obtain the first product. The first product is mixed with an aqueous solution of potassium carbonate and reacted for 8 hours, wherein the mass ratio of the first product to the potassium carbonate is 1:0.1. The mixture is then dried at 80°C and calcined again at 350°C for 3 hours to obtain activated alumina supported on modified carbon material.

[0038] The desulfurizing agent mentioned in step 2 is modified porous ferric oxide. The preparation method is as follows: ferric hydroxide, starch, and urea are weighed and mixed in a mass ratio of 5:1:1. Deionized water is added and the mixture is stirred at a speed of at least 500 rpm for 4 hours. After mixing evenly, the mixture is dried at 80°C and calcined at 300°C for 3 hours to obtain the second product. The second product is mixed with an aqueous solution of potassium carbonate and reacted for 3 hours. Then, it is dried at 80°C and calcined again at 350°C for 3 hours to obtain modified porous ferric oxide.

[0039] Example 2

[0040] A method for removing total sulfur from blast furnace gas includes the following steps:

[0041] Simulated blast furnace gas: Total sulfur content is 160 mg / L, including 24% inorganic sulfur (H2S), 70% organic sulfur (COS), and 6% organic sulfur (CS2).

[0042] (1) Simulated blast furnace gas is introduced into a hydrolysis tower filled with a catalyst, so that COS and CS2 in the blast furnace gas are hydrolyzed into H2S under the action of the catalyst. The hydrolysis reaction conditions are: under anaerobic conditions, with nitrogen gas of 99.999% purity as the equilibrium gas, a gas flow rate of 100 mL / min, a hydrolysis temperature of 70℃, 15% water vapor, and a reaction space velocity of 10000 h⁻¹. -1 The catalyst is packed in the hydrolysis tower at a rate of 6% of the tower height.

[0043] (2) Then, the converted H2S is introduced along with the blast furnace gas into a dry adsorption tower filled with desulfurizing agent for desulfurization treatment. The reaction conditions for the desulfurization treatment are: under anaerobic conditions, with nitrogen gas of 99.999% purity as the balance gas, a gas flow rate of 100 mL / min, a desulfurization temperature of 70℃, 15% water vapor, and a reaction space velocity of 10000 h⁻¹. -1 The desulfurizing agent is loaded into the dry adsorption tower at a rate of 6% of the tower height, achieving complete sulfur removal.

[0044] The catalyst mentioned in step 1 is activated alumina supported on modified carbon material, prepared in the same way as in Example 1.

[0045] The desulfurizing agent mentioned in step 2 is modified porous ferric oxide, prepared using the same method as in Example 1.

[0046] Example 3

[0047] A method for removing total sulfur from blast furnace gas includes the following steps:

[0048] Simulated blast furnace gas: total sulfur content is 160 mg / L, including 24% H2S, 70% COS, and 6% CS2;

[0049] (1) Simulated blast furnace gas is introduced into a hydrolysis tower filled with a catalyst, so that COS and CS2 in the blast furnace gas are hydrolyzed into H2S under the action of the catalyst. The conditions for the hydrolysis reaction are: under anaerobic conditions, with nitrogen gas of 99.999% purity as the equilibrium gas, a gas flow rate of 100 mL / min, a hydrolysis temperature of 70℃, 15% water vapor, and a reaction space velocity of 30000 h⁻¹. -1 The catalyst is loaded into the hydrolysis tower at a rate of 10% of the tower height.

[0050] (2) The H2S formed by the conversion is then introduced along with the blast furnace gas into a dry adsorption tower filled with desulfurizing agent for desulfurization treatment. The reaction conditions for the desulfurization treatment are: under anaerobic conditions, with nitrogen gas of 99.999% purity as the balance gas, a gas flow rate of 100 mL / min, a desulfurization temperature of 70℃, 15% water vapor, and a reaction space velocity of 30000 h⁻¹. -1 The desulfurizing agent is loaded into the dry adsorption tower at a rate of 10% of the tower height to achieve complete sulfur removal.

[0051] The catalyst mentioned in step 1 is activated alumina supported on modified carbon material, prepared in the same way as in Example 1.

[0052] The desulfurizing agent mentioned in step 2 is modified porous ferric oxide, prepared using the same method as in Example 1.

[0053] Comparative Example 1

[0054] The blast furnace gas desulfurization method in this comparative example is the same as that in Example 1, except that the catalyst in the hydrolysis tower is activated alumina pellets.

[0055] Comparative Example 2

[0056] The blast furnace gas desulfurization method in this comparative example is the same as that in Example 1, except that the catalyst in the hydrolysis tower is the first product in Example 1.

[0057] Comparative Example 3

[0058] The blast furnace gas desulfurization method in this comparative example is the same as that in Example 1, except that the catalyst in the hydrolysis tower is: activated alumina balls and starch are mixed with water at a mass ratio of 5:1 and stirred for 3 hours, dried at 80°C, and calcined at 550°C for 3 hours; then it is mixed with potassium carbonate at a mass ratio of 1:0.1 in water and reacted for 8 hours, dried at 80°C, and calcined at 350°C for 3 hours to obtain the catalyst of this comparative example.

[0059] Comparative Example 4

[0060] The blast furnace gas desulfurization method in this comparative example is the same as that in Example 1, except that the catalyst in the hydrolysis tower is: activated alumina balls and urea are mixed in water at a mass ratio of 5:1 and stirred for 3 hours, dried at 80°C, and calcined at 550°C for 3 hours; then it is mixed with potassium carbonate in water at a mass ratio of 1:0.1 and reacted for 8 hours, dried at 80°C, and calcined at 350°C for 3 hours to obtain the catalyst of this comparative example.

[0061] Comparative Example 5

[0062] The blast furnace gas desulfurization method in this comparative example is the same as that in Example 1, except that the desulfurizing agent in the dry adsorption tower is the product of ferric hydroxide calcined at 350°C for 3 hours.

[0063] Comparative Example 6

[0064] The blast furnace gas desulfurization method in this comparative example is the same as that in Example 1, except that the desulfurizing agent in the dry adsorption tower is the second product.

[0065] Comparative Example 7

[0066] The desulfurization method for blast furnace gas in this comparative example is the same as that in Example 1, except that the desulfurizing agent in the dry adsorption tower is: iron hydroxide and starch are mixed with water at a mass ratio of 5:1 and stirred for 4 hours, dried at 80°C, and calcined at 300°C for 3 hours; then it is mixed with potassium carbonate at a mass ratio of 1:0.1 in water and reacted for 3 hours, dried at 80°C, and calcined at 350°C for 3 hours to obtain the desulfurizing agent of this comparative example.

[0067] Comparative Example 8

[0068] The desulfurization method for blast furnace gas in this comparative example is the same as that in Example 1, except that the desulfurizing agent in the dry adsorption tower is: ferric hydroxide and urea are mixed with water at a mass ratio of 5:1 and stirred for 4 hours, dried at 80°C, and calcined at 300°C for 3 hours; then it is mixed with potassium carbonate at a mass ratio of 1:0.1 in water and reacted for 3 hours, dried at 80°C, and calcined at 350°C for 3 hours to obtain the desulfurizing agent of this comparative example.

[0069] The conversion rates of organic sulfur (COS and CS2) in the simulated blast furnace gas subjected to catalytic hydrolysis were detected and calculated, and the specific results are shown in Table 1; the inorganic sulfur removal rate in the simulated blast furnace gas subjected to further dry adsorption was detected and calculated, and the specific results are shown in Table 1.

[0070] Table 1 Organic sulfur conversion rate and inorganic sulfur removal rate

[0071]

[0072] Table 1 shows that Comparative Examples 1-4 compare the catalysts for hydrolyzing organic sulfur. Comparative Example 1 used unmodified raw material activated alumina spheres as its catalyst; Comparative Example 2 used activated alumina co-modified with starch and urea; Comparative Example 3 used potassium-loaded activated alumina modified with starch; and Comparative Example 4 used potassium-loaded activated alumina modified with urea. It can be seen that the raw material alumina spheres in Comparative Example 1 achieved a conversion rate of approximately 55% for organic sulfur in the short term, but this rate decreased to less than 5% in the later stages as the treatment time increased. Comparative Example 2 used activated alumina co-modified with starch and urea as its catalyst. The starch and urea adhered to the alumina surface, creating pores during calcination and increasing the specific surface area of ​​the alumina, which could improve the organic sulfur conversion rate to some extent. Comparative Examples 3 and 4 used potassium-loaded activated alumina modified with starch or urea, respectively. The loaded potassium provided alkaline active sites, improving the organic sulfur conversion rate compared to Comparative Example 2.

[0073] Therefore, this invention uses urea and starch to jointly modify activated alumina and load it with potassium as the active ingredient, which helps the catalyst achieve an organic sulfur conversion rate of over 93% in a short time and prolongs the catalytic effect of the catalyst to achieve an organic sulfur conversion rate of over 70% over a long period of time.

[0074] Comparative Examples 5-8 compare desulfurizing agents for adsorbing inorganic sulfur. Comparative Example 5 used ferric oxide (calcined ferric hydroxide), Comparative Example 6 used ferric oxide co-modified with starch and urea, Comparative Example 7 used starch-modified ferric oxide loaded with potassium, and Comparative Example 8 used urea-modified ferric oxide loaded with potassium. It is evident that the ferric oxide in Comparative Example 1 has a certain removal effect on inorganic sulfur in the short term, but the removal effect is poor. With prolonged treatment time, ferric oxide basically has no removal effect on inorganic sulfur. Comparative Example 6 uses starch and urea to modify ferric oxide. The starch and urea adhere to the surface of ferric oxide, and during calcination, pores are generated, increasing the specific surface area of ​​ferric oxide, which can improve the adsorption effect of inorganic sulfur to a certain extent. Comparative Examples 7 and 8 use starch and urea to modify ferric oxide and load potassium, respectively. The loaded potassium provides alkaline active sites, improving the inorganic sulfur removal rate compared to Comparative Example 6. Therefore, this invention uses urea and starch to jointly modify ferric oxide and load it with the active ingredient potassium, which helps the desulfurizer achieve an inorganic sulfur removal rate of over 90% in a short time and prolongs the adsorption effect of the desulfurizer so that it can achieve an inorganic sulfur removal rate of over 70% over a long period of time.

[0075] In Example 1, the space velocity was the normal industrial production space velocity. Under reaction conditions of 70°C, it achieved a 99.9% organic sulfur conversion rate and over 90% inorganic sulfur removal rate within a short period of 5 minutes. In Example 1, the outlet hydrogen sulfide concentration was below 15 mg / L at 5 minutes. As blast furnace gas was continuously introduced, the organic sulfur concentration increased. After prolonged treatment of organic sulfur by the catalyst in the hydrolysis tower, the conversion rate of organic sulfur decreased to some extent, but after 195 minutes, it still achieved over 80% organic sulfur conversion and over 70% inorganic sulfur removal. Examples 2 and 3 used more stringent space velocities; increasing the space velocity would adversely affect the catalyst and desulfurizing agent. However, the catalyst of this invention still achieved a conversion rate of over 70% after prolonged treatment of organic sulfur, and the desulfurizing agent of this invention still achieved a removal rate of over 60% for inorganic sulfur.

[0076] The above description is merely a preferred embodiment of the present invention. In the above embodiments, when filling the catalyst and desulfurizing agent, multiple layers of catalyst bed and desulfurizing agent bed can be laid to ensure sufficient contact and reaction between the gas and the catalyst and desulfurizing agent. However, the scope of protection of the present invention is not limited thereto. Any equivalent substitutions or modifications made by those skilled in the art within the technical scope disclosed in the present invention, based on the technical solution and inventive concept of the present invention, should be covered within the scope of protection of the present invention.

Claims

1. A method for total sulfur removal from blast furnace gas, characterized in that, Includes the following steps: (1) Blast furnace gas is introduced into a hydrolysis tower filled with catalyst, so that COS and CS2 in the blast furnace gas are hydrolyzed and converted into H2S under the action of the catalyst. (2) Then the H2S formed by conversion is introduced together with the blast furnace gas into a dry adsorption tower filled with desulfurizing agent for desulfurization treatment to achieve complete sulfur removal; The catalyst is activated alumina supported on modified carbon material; The desulfurizing agent is modified porous ferric oxide; The catalyst is prepared by: stirring activated alumina, starch, urea, and water, mixing them evenly, drying them, and calcining them at 550°C for 3 hours to obtain a first product; mixing the first product with an aqueous solution of water-soluble carbonate, drying it, and calcining it again at 350°C for 3 hours to obtain activated alumina loaded with modified carbon material; the mass ratio of activated alumina, starch, and urea is 5:1:1; the mass ratio of the first product to the water-soluble carbonate is 1:0.1; the water-soluble carbonate is potassium carbonate and / or sodium carbonate; the stirring reaction time is 3 hours, and the mixing reaction time is 8 hours; The desulfurizing agent is prepared by: stirring and reacting ferric hydroxide, starch, urea, and water, mixing them evenly, drying them, and calcining them at 300°C for 3 hours to obtain a second product; mixing and reacting the second product with an aqueous solution of a water-soluble carbonate, drying it, and calcining it again at 350°C for 3 hours to obtain modified porous ferric oxide; the water-soluble carbonate is potassium carbonate and / or sodium carbonate.

2. The method for total sulfur removal from blast furnace gas according to claim 1, characterized in that, The mass ratio of the ferric hydroxide to the starch and the urea is 5:1:1; the mass ratio of the second product to the water-soluble carbonate is 1:0.1; the stirring reaction time is 4 hours, and the mixing reaction time is 3 hours.

3. A method for total sulfur removal from blast furnace gas according to any one of claims 1-2, characterized in that, The conditions for the hydrolysis reaction are as follows: under anaerobic conditions, using nitrogen gas with a purity exceeding 4N as the equilibrium gas, a gas flow rate of 80-100 mL / min, a hydrolysis temperature of 65-80℃, 5-15% water vapor, and a reaction space velocity of 5000-30000 h⁻¹. -1 .

4. A method for total sulfur removal from blast furnace gas according to any one of claims 1-2, characterized in that, The desulfurization reaction conditions are as follows: under anaerobic conditions, using nitrogen gas with a purity exceeding 4N as the equilibrium gas, a gas flow rate of 80-100 mL / min, a desulfurization temperature of 50-100℃, 5-15% water vapor, and a reaction space velocity of 5000-30000 h⁻¹. -1 .

5. A method for total sulfur removal from blast furnace gas according to any one of claims 1-2, characterized in that, The catalyst is packed in the hydrolysis tower at a rate of at least 3% of the tower's height. The amount of desulfurizing agent packed in the dry adsorption tower is at least 3% of the tower height.

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