Regeneration method of hydrolysis catalyst for inactivated blast furnace gas

Abstract

The invention provides a regeneration method of a hydrolysis catalyst for inactivated blast furnace gas, and belongs to the technical field of catalyst regeneration. The method comprises the following steps: in a nitrogen-air mixed atmosphere, carrying out oxidation treatment on inactivated blast furnace gas by using a hydrolysis catalyst to obtain an oxidized catalyst; carrying out nitrogen blowing on the oxidized catalyst to obtain a desulfurized catalyst; cleaning the desulfurized catalyst by using an ethanol solution to obtain a cleaned catalyst; carrying out first roasting on the cleaned catalyst to obtain a roasted catalyst; dipping the roasted catalyst in an active metal salt solution, and drying to obtain a dipped catalyst; and washing the impregnated catalyst by using an inorganic alkaline solution, and then carrying out second roasting to obtain the regenerated hydrolysis catalyst for blast furnace gas. The inactivated hydrolysis catalyst for the blast furnace gas is regenerated, and the regenerated hydrolysis catalyst is high in activity, long in service life and capable of meeting the requirement for reutilization of the blast furnace gas.

Description

Technical Field

[0001] The invention relates to the technical field of catalyst regeneration, and in particular to a method for regenerating a deactivated blast furnace gas hydrolysis catalyst. Background Art

[0002] Blast furnace gas generally uses a hydrolysis catalyst to convert organic sulfur into H2S, and then removes H2S through a desulfurizer. The reaction principle is as follows: COS+H2O=CO2+H2S, CS2+2H2O=CO2+2H2S. Under the action of the hydrolysis catalyst, organic sulfur reacts with water vapor in the gas to generate hydrogen sulfide and carbon dioxide.

[0003] Hydrolysis catalysts are generally based on alumina, titanium oxide, etc. as carriers, loaded with metal oxides and alkaline salts as active components and additives. Blast furnace gas generally contains chlorine, SO2, NO X , HCN and other components, which will react with the active components of the hydrolysis catalyst, such as nickel oxide, molybdenum oxide and other metal oxides undergo sulfidation to become nickel sulfide, molybdenum sulfide, etc., potassium carbonate, sodium carbonate and potassium hydroxide and other alkaline activity enhancing components become potassium chloride, sodium chloride and lose alkalinity, and some active components are sulfated to become sulfites or sulfates, resulting in sulfation of the hydrolysis catalyst, making the hydrolysis catalyst inactive. At the same time, H2S produced by the hydrolysis of blast furnace gas will react with trace amounts of O2 in the gas to generate elemental S to block the micropores, and some C, high-boiling organic matter, dust and other substances will also block the micropores of the hydrolysis catalyst. The hydrolysis catalyst is severely poisoned during the hydrolysis of organic sulfur in blast furnace gas, resulting in a short service life of the hydrolysis catalyst. In the absence of dechlorination and other protective measures, the service life is about 3 to 6 months, and in the case of adding dechlorination protection measures, the service life is about 12 months. The frequent replacement of the hydrolysis catalyst produces a large amount of waste hydrolysis catalyst, which is difficult to handle. Summary of the invention

[0004] In view of this, the object of the present invention is to provide a method for regenerating deactivated blast furnace gas using a hydrolysis catalyst. The present invention regenerates the deactivated blast furnace gas using a hydrolysis catalyst, and the regenerated hydrolysis catalyst has high activity and long service life, and can meet the demand for reuse of blast furnace gas.

[0005] In order to achieve the above-mentioned object of the invention, the present invention provides the following technical solutions:

[0006] The present invention provides a method for regenerating a deactivated blast furnace gas using a hydrolysis catalyst, comprising the following steps:

[0007] In a nitrogen-air mixed atmosphere, deactivated blast furnace gas is oxidized using a hydrolysis catalyst to obtain an oxidized catalyst;

[0008] Blowing nitrogen through the oxidized catalyst to obtain a desulfurized catalyst;

[0009] washing the desulfurized catalyst with an ethanol solution to obtain a washed catalyst;

[0010] performing a first calcination on the cleaned catalyst to obtain a calcined catalyst;

[0011] The calcined catalyst is impregnated in an active metal salt solution and then dried to obtain an impregnated catalyst, wherein the active metal salt solution further comprises polyethylene glycol;

[0012] The impregnated catalyst is washed with an inorganic alkaline solution and then subjected to a second calcination to obtain a regenerated blast furnace gas hydrolysis catalyst.

[0013] Preferably, the oxidation treatment is carried out at a temperature of 100 to 150° C. and for a time of 6 to 12 hours.

[0014] Preferably, the volume percentage of air in the nitrogen-air mixed atmosphere is 3-5%.

[0015] Preferably, the nitrogen blowing temperature is 300-350°C and the air velocity is 100-200h -1 .

[0016] Preferably, the volume percentage of ethanol in the ethanol solution is 20-30%.

[0017] Preferably, the volume ratio of the ethanol solution to the desulfurized catalyst is 1.5 to 3:1.

[0018] Preferably, the temperature of the first calcination is 400-450°C, and the air velocity is 100-200h -1 , the first calcination is carried out in air.

[0019] Preferably, the active metal salt in the active metal salt solution includes lanthanum nitrate, cerium nitrate and nickel nitrate, the mass percentage of lanthanum nitrate in the active metal salt solution is 1-3%, the mass percentage of cerium nitrate is 1-5%, the mass percentage of nickel nitrate is 2-5%, and the mass percentage of polyethylene glycol is 1-5%.

[0020] Preferably, the mass fraction of the inorganic alkaline substance in the inorganic alkaline solution is 15-25%, and the inorganic alkaline substance solution includes potassium carbonate, sodium carbonate and ammonia water.

[0021] Preferably, the second calcination is performed at a temperature of 300 to 500° C. and for a time of 2 to 5 hours.

[0022] The invention provides a method for regenerating a deactivated blast furnace gas using a hydrolysis catalyst. The method comprises the following steps: in a nitrogen-air mixed atmosphere, subjecting the deactivated blast furnace gas to an oxidation treatment with a hydrolysis catalyst to obtain an oxidized catalyst; subjecting the oxidized catalyst to nitrogen blowing to obtain a desulfurized catalyst; cleaning the desulfurized catalyst with an ethanol solution to obtain a cleaned catalyst; subjecting the cleaned catalyst to a first roasting to obtain a roasted catalyst; impregnating the roasted catalyst in an active metal salt solution and then drying to obtain an impregnated catalyst, wherein the active metal salt solution further comprises polyethylene glycol; and washing the impregnated catalyst with an inorganic alkaline solution and then subjecting the second roasting to obtain a regenerated blast furnace gas hydrolysis catalyst.

[0023] Compared with the prior art, the present invention has the following beneficial effects:

[0024] During the oxidation treatment of the present invention, the deactivated blast furnace gas undergoes an oxidation reaction with the sulfides such as nickel sulfide and molybdenum sulfide in the hydrolysis catalyst to generate elemental S, and the metals such as nickel and molybdenum as active components are converted into oxides and retained in the micropores, and the sulfides are converted into oxides under the oxidation action of oxygen; nitrogen blowing can carry away the elemental S in the micropores of the oxidized catalyst along with the gas, so that the elemental S in the gas is cooled and collected; the desulfurized catalyst is cleaned with an ethanol solution, so that soluble chlorides, sulfates, sulfites (including potassium chloride, sodium chloride, potassium sulfate, potassium sulfite, etc.), tar and other organic substances in the desulfurized catalyst can be cleaned; the first roasting can activate the cleaned catalyst, restore the microporous structure of the catalyst, and partially C, ethyl acetate remaining in the cleaned catalyst Alcohols and the like will decompose to increase the number of micropores, and the micropore structure destroyed after deactivation will also be restored with the first calcination; the polyethylene glycol in the active metal salt solution acts as a dispersant, which is beneficial to the loading of the active metal salt, and the polyethylene glycol decomposes during the second calcination to increase the catalyst pores; during the washing process with the inorganic alkaline solution, the active metal salt in the active metal salt solution is converted into carbonate precipitates, which are immersed in the catalyst micropores, and the inorganic alkaline substances (including sodium carbonate, potassium carbonate and ammonia water) can restore the alkaline active sites of the catalyst; during the second calcination, the carbonate precipitates (including nickel carbonate, etc.) decompose to generate metal oxides with catalytic activity. At the same time, the residual ammonia, polyethylene glycol, etc. decompose to enhance the catalyst micropores and promote the recovery of the catalyst pore structure.

[0025] The data in the examples show that the deactivated hydrolysis catalyst can be returned to the factory for regeneration and reuse, and the activity of the regenerated hydrolysis catalyst can reach 95-98% of the activity of the new catalyst, and the service life can reach 85-95% of the new prepared hydrolysis catalyst, which can meet the demand for reuse of blast furnace gas.

[0026] Furthermore, the present invention limits the temperature of the oxidation treatment and the air content in the nitrogen-air mixed atmosphere to prevent excessive oxygen from entering the catalyst, causing S oxidation to generate sulfate and destroying the internal structure of the catalyst. DETAILED DESCRIPTION

[0027] The present invention provides a method for regenerating a deactivated blast furnace gas using a hydrolysis catalyst, comprising the following steps:

[0028] In a nitrogen-air mixed atmosphere, deactivated blast furnace gas is oxidized using a hydrolysis catalyst to obtain an oxidized catalyst;

[0029] Blowing nitrogen through the oxidized catalyst to obtain a desulfurized catalyst;

[0030] washing the desulfurized catalyst with an ethanol solution to obtain a washed catalyst;

[0031] performing a first calcination on the cleaned catalyst to obtain a calcined catalyst;

[0032] The calcined catalyst is impregnated in an active metal salt solution and then dried to obtain an impregnated catalyst, wherein the active metal salt solution further comprises polyethylene glycol;

[0033] The impregnated catalyst is washed with an inorganic alkaline solution and then subjected to a second calcination to obtain a regenerated blast furnace gas hydrolysis catalyst.

[0034] The invention uses a hydrolysis catalyst to oxidize deactivated blast furnace gas in a nitrogen-air mixed atmosphere to obtain an oxidized catalyst.

[0035] In the present invention, the deactivated blast furnace gas hydrolysis catalyst is preferably obtained by using the blast furnace gas hydrolysis catalyst.

[0036] In the present invention, the specific surface area of ​​the deactivated blast furnace gas hydrolysis catalyst is preferably 50 to 100 m 2 / g, specifically 50, 60, 70, 80, 90 or 100 m 2 / g.

[0037] In the present invention, the blast furnace gas hydrolysis catalyst preferably comprises a carrier, an active metal oxide component, an alkaline salt and an auxiliary agent.

[0038] In the present invention, the carrier preferably comprises alumina and titanium dioxide, the mass percentage of the carrier in the blast furnace gas hydrolysis catalyst is preferably 70-80%, and the mass percentage of alumina in the carrier is preferably 80-95%;

[0039] In the present invention, the mass percentage of the active metal oxide component in the blast furnace gas hydrolysis catalyst is preferably 2-5%, and the active metal oxide component preferably includes nickel oxide and molybdenum oxide.

[0040] In the present invention, the mass percentage of the alkaline salt in the blast furnace gas hydrolysis catalyst is preferably 10-20%, and the alkaline salt preferably includes potassium carbonate and sodium carbonate.

[0041] In the present invention, the auxiliary agent is preferably a rare earth metal.

[0042] In the present invention, the active site micropore size of the blast furnace gas hydrolysis catalyst is preferably Specifically, it can be 80, 100 or The specific surface area is preferably 200 to 250 m 2 / g, specifically 200, 210, 220, 230, 240 or 250 m 2 / g.

[0043] In the present invention, the temperature of the oxidation treatment is preferably 100-150°C, specifically 100, 110, 120, 130, 140 or 150°C, and the time is preferably 6-12h, specifically 6, 8, 10 or 12h; during the oxidation treatment, the deactivated blast furnace gas undergoes oxidation reaction with sulfides such as nickel sulfide and molybdenum sulfide in the hydrolysis catalyst to generate elemental S, and the active components such as nickel and molybdenum metals are converted into oxides and retained in the micropores, and the sulfides are oxidized by oxygen to generate oxides.

[0044] In the present invention, the volume percentage of air in the nitrogen-air mixed atmosphere is preferably 3-5%, specifically 3%, 4% or 5%.

[0045] The present invention limits the temperature of the oxidation treatment and the air content in the nitrogen-air mixed atmosphere to prevent excessive oxygen (oxygen content <1 vol%) from entering the catalyst, resulting in oxidation of S to generate sulfate and destroying the internal structure of the catalyst.

[0046] After obtaining the oxidized catalyst, the present invention blows nitrogen through the oxidized catalyst to obtain a desulfurized catalyst.

[0047] In the present invention, the temperature of the nitrogen blowing is preferably 300-350°C, specifically 300, 310, 320, 330, 340 or 350°C, and the air velocity is preferably 100-200h -1 , specifically 100, 150 or 200h -1 The nitrogen blowing can carry away the elemental S in the micropores of the oxidized catalyst along with the gas, so that the elemental S in the gas can be collected after cooling.

[0048] After obtaining the desulfurized catalyst, the present invention uses an ethanol solution to clean the desulfurized catalyst to obtain a cleaned catalyst.

[0049] In the present invention, the volume percentage of ethanol in the ethanol solution is preferably 20-30%, specifically 20%, 25% or 30%. The present invention uses the ethanol solution to clean the desulfurized catalyst, and can clean the soluble chlorides, sulfates, sulfites (including potassium chloride, sodium chloride, potassium sulfate, potassium sulfite, etc.), tar and other organic substances in the desulfurized catalyst.

[0050] In the present invention, the volume ratio of the ethanol solution to the desulfurized catalyst is preferably 1.5 to 3:1, specifically 1.5:1, 2:1, 2.5:1 or 3:1.

[0051] After obtaining the cleaned catalyst, the present invention performs a first calcination on the cleaned catalyst to obtain a calcined catalyst.

[0052] In the present invention, the temperature of the first calcination is preferably 400-450°C, specifically 400, 410, 420, 430, 440 or 450°C, and the space velocity is preferably 100-200h -1 , specifically 100, 150 or 200h -1 The time is preferably 2 to 5 hours, specifically 2, 3, 4 or 5 hours. The first calcination is preferably carried out in air. The first calcination can activate the cleaned catalyst and restore the microporous structure of the catalyst. Part of C, ethanol, etc. remaining in the cleaned catalyst will decompose to increase the number of micropores. The microporous structure destroyed after deactivation will also be restored as the first calcination proceeds.

[0053] After obtaining the calcined catalyst, the present invention immerses the calcined catalyst in an active metal salt solution and then dries it to obtain an impregnated catalyst, wherein the active metal salt solution further includes polyethylene glycol.

[0054] In the present invention, the active metal salt in the active metal salt solution preferably includes lanthanum nitrate, cerium nitrate and nickel nitrate, the mass percentage of lanthanum nitrate in the active metal salt solution is preferably 1-3%, specifically 1%, 1.5%, 2% or 3%, the mass percentage of cerium nitrate is preferably 1-5%, specifically 1%, 2%, 3%, 4% or 5%, the mass percentage of nickel nitrate is preferably 2-5%, specifically 2%, 3%, 4% or 5%, and the mass percentage of polyethylene glycol is preferably 1-5%, specifically 1%, 2%, 3%, 4% or 5%. In the present invention, the polyethylene glycol in the active metal salt solution is used as a dispersant to facilitate the loading of the active metal salt, and the polyethylene glycol is decomposed by heating during the second calcination, which can increase the pores of the catalyst.

[0055] In the present invention, the impregnation is preferably equal volume impregnation.

[0056] In the present invention, the drying is preferably oven drying, the temperature of the oven drying is preferably 120° C., and the time is preferably 2 hours.

[0057] After obtaining the impregnated catalyst, the present invention uses an inorganic alkaline solution to wash the impregnated catalyst and then performs a second calcination to obtain a regenerated blast furnace gas hydrolysis catalyst.

[0058] In the present invention, the mass fraction of the inorganic alkaline substance in the inorganic alkaline solution is preferably 15-25%, specifically 15%, 20%, 22% or 25%, and the inorganic alkaline substance solution preferably includes potassium carbonate, sodium carbonate and ammonia water; during the washing process of the inorganic alkaline solution, the active metal salt in the active metal salt solution is converted into carbonate precipitates and impregnated in the catalyst micropores, and the inorganic alkaline substance (including sodium carbonate, potassium carbonate and ammonia water) can restore the alkaline active sites of the catalyst.

[0059] In the present invention, drying is preferably performed after the washing and before the second roasting, and the drying temperature is preferably 120° C. and the drying time is preferably 2 hours.

[0060] In the present invention, the temperature of the second calcination is preferably 300-500°C, specifically 300, 400 or 500°C, and the time is preferably 2-5h, specifically 2, 3, 4 or 5h; during the second calcination, carbonate precipitates (including nickel carbonate, etc.) decompose to generate metal oxides with catalytic activity, and at the same time, residual ammonia, polyethylene glycol, etc. decompose to enhance the catalyst micropores and promote the recovery of the catalyst pore structure.

[0061] The technical solutions in the present invention will be described clearly and completely below in conjunction with the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, not all of them. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0062] Example 1

[0063] S1, take 5kg of deactivated blast furnace gas and use hydrolysis catalyst, space velocity 100h -1 , N2 is used as the carrier gas, and air is added to obtain a mixed atmosphere. The air content in the mixed atmosphere is 3 vol%, the temperature is 120°C, and the oxidation reaction is carried out by circulating ventilation for 6 hours to obtain the product S1.

[0064] S2, nitrogen, 300℃, space velocity 100h -1The elemental S deposited in the micropores of the product S1 is taken away with the gas, the elemental S in the gas is collected after cooling, and nitrogen is continuously passed for 24 hours to obtain the product S2.

[0065] S3. Wash 1 kg of product S2 with 1.5 kg of 20 vol% ethanol solution to obtain product S3.

[0066] S4, 400℃, air speed 100h -1 , pass air, and carry out the first calcination of product S3 for 4 hours to obtain product S4.

[0067] S5, prepare an active metal salt solution, wherein the mass percentage of lanthanum nitrate is 1%, the mass percentage of cerium nitrate is 2%, the mass percentage of nickel nitrate is 3%, and the mass percentage of polyethylene glycol 200 is 3%, and impregnate the product S4 by an equal volume impregnation method. After the impregnation is completed, dry at 120° C. for 2 hours to obtain the product S5.

[0068] S6. Prepare an inorganic alkaline solution, in which the mass percentage of potassium carbonate is 15%, the mass percentage of sodium carbonate is 5%, and the mass percentage of hydrogen peroxide is 2%. 5 L of the solution is used to wash the product S5, and then dry it at 120° C. for 2 h to obtain the product S6.

[0069] S7. The product S6 is subjected to a second calcination activation at 400° C. for 3 h to obtain a regenerated blast furnace gas hydrolysis catalyst.

[0070] Performance test of the hydrolysis catalyst of the regenerated blast furnace gas

[0071] 1. Laboratory activity test

[0072] According to HG / T 4350-2012 room temperature carbon oxysulfide catalyst activity test method, space velocity 2000h -1 , inlet COS content 200mg / Nm 3 , N2 is the carrier gas, and the test results of the catalyst activity at different temperatures are shown in Table 1.

[0073] Table 1 Laboratory activity test results

[0074] sample Temperature ℃ 50 55 60 65 70 80 Hydrolyzing Agent for Regenerating Blast Furnace Gas COS conversion % 90.2 93.5 97.2 99.1 99.9 99.9 New hydrolyzing agent COS conversion % 91.1 94.0 97.8 99.3 99.9 99.9

[0075] 2. On-site catalyst activity test

[0076] Side line test of a steel plant in Tangshan, blast furnace gas, COS content 100~150mg / Nm 3 , airspeed 1200h -1 The test results are shown in Table 2.

[0077] Table 2 Field activity test results

[0078] sample Temperature ℃ 50 55 60 65 70 80 Hydrolyzing Agent for Regenerating Blast Furnace Gas COS conversion rate % 87.2 90.3 95.2 98.2 99.9 99.9 New hydrolyzing agent COS conversion rate % 89.5 91.2 96.5 99.1 99.9 99.9

[0079] As can be seen from Tables 1 and 2, the activity of the regenerated blast furnace gas hydrolysis catalyst above 70°C reaches 99.9%.

[0080] 3. On-site catalyst life test

[0081] Side line test of a steel plant in Tangshan, blast furnace gas, COS content 100~150mg / Nm 3 , airspeed 1200h -1 , with a conversion rate of ≥90% as the export index requirement, according to the general design conditions, the hydrolysis inlet temperature is 60-90°C, and the results are shown in Table 3. It can be seen that in the field test, at normal operating temperature and operating space velocity, the cumulative service life of the regenerated blast furnace gas hydrolysis catalyst can reach more than 10 months, which is close to the 1-year (360-day) service life requirement of the new catalyst.

[0082] Table 3 On-site catalyst life test results

[0083] Temperature ℃ 60 70 80 90 Run time 132 days 91 days 51 days 38 days Cumulative running time 132 days 223 days 274 days 312 days

[0084] Example 2

[0085] S1, take 5kg of deactivated blast furnace gas and use hydrolysis catalyst, space velocity 100h -1 , N2 is used as the carrier gas, and air is added to obtain a mixed atmosphere. The air content in the mixed atmosphere is 5 vol%, the temperature is 100°C, and the circulation ventilation is carried out for 10 hours to carry out the oxidation reaction to obtain the product S1.

[0086] S2, nitrogen, 350℃, space velocity 100h -1 The elemental S deposited in the micropores of the product S1 is taken away with the gas, the elemental S in the gas is collected after cooling, and nitrogen is continuously passed for 12 hours to obtain the product S2.

[0087] S3. Wash 1 kg of product S2 with 2 kg of 25 vol% ethanol solution to obtain product S3.

[0088] S4, 450℃, air speed 100h -1 , pass air, and carry out the first roasting of product S3 for 3 hours to obtain product S4.

[0089] S5, prepare an active metal salt solution, wherein the mass percentage of lanthanum nitrate is 1.5%, the mass percentage of cerium nitrate is 1%, the mass percentage of nickel nitrate is 5%, and the mass percentage of polyethylene glycol 200 is 4%, and impregnate the product S4 by an equal volume impregnation method. After the impregnation is completed, dry at 120° C. for 2 hours to obtain the product S5.

[0090] S6. Prepare an inorganic alkaline solution, in which the mass percentage of potassium carbonate is 18%, the mass percentage of sodium carbonate is 5%, and the mass percentage of hydrogen peroxide is 1%. 5 L of the solution is used to wash the product S5, and then dry it at 120° C. for 2 h to obtain the product S6.

[0091] S7. The product S6 is subjected to a second calcination activation at 500° C. for 2 h to obtain a regenerated blast furnace gas hydrolysis catalyst.

[0092] The performance of the obtained regenerated blast furnace gas was tested using a hydrolysis catalyst

[0093] 1. Laboratory activity test

[0094] According to HG / T4350-2012 room temperature carbon oxysulfide catalyst activity test method, space velocity 2000h -1 , inlet COS content 200mg / Nm 3 , N2 is the carrier gas, and the test results of the catalyst activity at different temperatures are shown in Table 4.

[0095] Table 4 Laboratory activity test results

[0096] sample Temperature ℃ 50 55 60 65 70 80 Hydrolyzing Agent for Regenerating Blast Furnace Gas COS conversion % 89.5 92.9 96.9 99.0 99.9 99.9 New hydrolyzing agent COS conversion % 91.1 94.0 97.8 99.3 99.9 99.9

[0097] 2. On-site catalyst activity test

[0098] Side line test of a steel plant in Tangshan, blast furnace gas, COS content 100~150mg / Nm 3 , airspeed 1200h -1 The test results are shown in Table 5.

[0099] Table 5 Field activity test results

[0100] sample Temperature ℃ 50 55 60 65 70 80 Hydrolyzing Agent for Regenerating Blast Furnace Gas COS conversion rate % 86.5 90.1 94.8 97.6 99.9 99.9 New hydrolyzing agent COS conversion rate % 89.5 91.2 96.5 99.1 99.9 99.9

[0101] It can be seen from Tables 4 and 5 that the activity of the regenerated blast furnace gas hydrolysis catalyst above 70°C reaches 99.9%.

[0102] 3. On-site catalyst life test

[0103] Side line test of a steel plant in Tangshan, blast furnace gas, COS content 100~150mg / Nm 3 , airspeed 1200h -1 , with a conversion rate of ≥90% as the export index requirement, according to the general design conditions, the hydrolysis inlet temperature is 60-90°C, and the results are shown in Table 6. It can be seen that in the field test, at normal operating temperature and operating space velocity, the cumulative service life of the regenerated blast furnace gas hydrolysis catalyst can reach more than 10 months, which is close to the 1-year (360-day) service life requirement of the new catalyst.

[0104] Table 6 On-site catalyst life test results

[0105] Temperature ℃ 60 70 80 90 Run time 145 days 102 days 58 days 31 days Cumulative running time 145 days 247 days 305 days 336 days

[0106] The above description is only a preferred embodiment of the present invention and does not limit the present invention in any form. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principle of the present invention, and these improvements and modifications should also be regarded as the protection scope of the present invention.

Claims

1. A method for regenerating a deactivated blast furnace gas using a hydrolysis catalyst, characterized in that: The following steps are involved: In a nitrogen-air mixed atmosphere, deactivated blast furnace gas is oxidized using a hydrolysis catalyst to obtain an oxidized catalyst; Blowing nitrogen through the oxidized catalyst to obtain a desulfurized catalyst; washing the desulfurized catalyst with an ethanol solution to obtain a washed catalyst; performing a first calcination on the cleaned catalyst to obtain a calcined catalyst; The calcined catalyst is impregnated in an active metal salt solution and then dried to obtain an impregnated catalyst, wherein the active metal salt solution further comprises polyethylene glycol; The impregnated catalyst is washed with an inorganic alkaline solution and then subjected to a second calcination to obtain a regenerated blast furnace gas hydrolysis catalyst.

2. The regeneration method according to claim 1, characterized in that: The temperature of the oxidation treatment is 100-150° C., and the time is 6-12 hours.

3. The regeneration method according to claim 1 or 2, characterized in that: The volume percentage of air in the nitrogen-air mixed atmosphere is 3-5%.

4. The regeneration method according to claim 1, characterized in that: The nitrogen blowing temperature is 300-350°C, and the air velocity is 100-200h -1 .

5. The regeneration method according to claim 1, characterized in that: The volume percentage of ethanol in the ethanol solution is 20-30%.

6. The regeneration method according to claim 1 or 5, characterized in that: The volume ratio of the ethanol solution to the desulfurized catalyst is 1.5 to 3:

1.

7. The regeneration method according to claim 1, characterized in that: The temperature of the first calcination is 400-450°C, and the air velocity is 100-200h -1 , the first calcination is carried out in air.

8. The regeneration method according to claim 1, characterized in that: The active metal salt in the active metal salt solution comprises lanthanum nitrate, cerium nitrate and nickel nitrate. The mass percentage of lanthanum nitrate in the active metal salt solution is 1-3%, the mass percentage of cerium nitrate is 1-5%, the mass percentage of nickel nitrate is 2-5%, and the mass percentage of polyethylene glycol is 1-5%.

9. The regeneration method according to claim 1, characterized in that: The mass fraction of the inorganic alkaline substance in the inorganic alkaline solution is 15-25%, and the inorganic alkaline substance solution comprises potassium carbonate, sodium carbonate and ammonia water.

10. The regeneration method according to claim 1, characterized in that: The second calcination is carried out at a temperature of 300 to 500° C. and for a time of 2 to 5 hours.