CN114250088B - Composite solvent for removing carbonyl sulfide in blast furnace gas and application thereof - Google Patents
Composite solvent for removing carbonyl sulfide in blast furnace gas and application thereof Download PDFInfo
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- CN114250088B CN114250088B CN202111106681.6A CN202111106681A CN114250088B CN 114250088 B CN114250088 B CN 114250088B CN 202111106681 A CN202111106681 A CN 202111106681A CN 114250088 B CN114250088 B CN 114250088B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/14—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic
- C10K1/143—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors organic containing amino groups
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Abstract
The invention provides a compound solvent for removing carbonyl sulfide in blast furnace gas and application thereof, comprising 89-98.9 wt% of organic alcohol amine compound, 0.1-1 wt% of stabilizer, 0.5-5 wt% of activator and 0.5-5 wt% of accelerator. The compound solvent provided by the invention can be applied to a pre-desulfurization process of blast furnace gas, can be used for efficiently removing carbonyl sulfide in the blast furnace gas, has a removal rate of up to 90%, can be recycled, has no secondary pollutant emission, greatly reduces the running cost, and has high economic benefit.
Description
Technical Field
The invention belongs to the technical field of blast furnace gas desulfurization, and particularly relates to a compound solvent for removing carbonyl sulfide in blast furnace gas and application thereof.
Background
The blast furnace gas is a byproduct combustible gas with low heat value containing carbon monoxide, carbon dioxide, nitrogen and hydrogen in the iron-making process of iron and steel enterprises, has high yield and wide application, and can be used as fuel of blast furnace hot blast stoves, steel rolling heating furnaces and self-contained electric boilers of steel plants. The raw blast furnace gas also contains a large amount of dust and sulfides, which are mainly classified into organic sulfur and inorganic sulfur, and the organic sulfur content is about 70-85% higher than that of the inorganic sulfur. The main components of the organic sulfur include carbonyl sulfide (COS), carbon disulfide (CS 2), thioether, mercaptan and the like, wherein COS accounts for about 60-85% of the total sulfur; the main component of inorganic sulfur is mainly hydrogen sulfide, and also comprises a small amount of sulfur dioxide and the like. The sulfur dioxide emission in the untreated blast furnace gas exceeds the standard, and the SO 2 content in the discharged flue gas is usually more than 50mg/Nm 3, and sometimes even more than 200mg/Nm 3.
At present, the blast furnace gas desulfurization of iron and steel enterprises basically adopts end treatment, namely, the blast furnace gas is sent to a hot blast stove, a heating furnace and other subsequent devices after dust removal, purification and TRT power generation, and organic sulfur is converted into inorganic sulfur (SO 2) after combustion, and then desulfurization treatment is carried out, which is also called as a post desulfurization process. However, the sulfur content after the end treatment does not reach the national latest ultra-clean emission requirements (less than 50mg/Nm 3, less than 35mg/Nm 3 in some areas, and the latest environmental policy requirements to the end of 2025 steel industry all reach less than 35mg/Nm 3). At present, main technologies of terminal treatment include an SDS (sodium dodecyl sulfate), a circulating fluidized bed semi-dry method, an activated carbon method and the like, desulfurization facilities (a hot blast stove, a heating furnace, a gas boiler and the like) are required to be arranged at multiple points, the occupied area is large, equipment maintenance points are large, and H 2 S contained in blast furnace gas is severely corroded TRT facilities and conveying pipelines due to terminal desulfurization, the service life of a generator is shortened, and the early investment cost and the later maintenance cost are relatively high.
Therefore, the sulfide in the blast furnace gas is directly removed before the blast furnace gas is combusted, and the combustion is carried out after sulfur removal, so that the content of sulfur dioxide in the combusted flue gas can reach the national ultra-low emission requirement, and a post-desulfurization process is not needed, and the method is called as a pre-desulfurization process and also called as source management. The front desulfurization process is simple, the occupied area is small, the operation cost is low, no refractory byproducts are generated, the purified coal gas is directly supplied to each production unit at the downstream to be used as energy for combustion, the national ultra-low emission requirement can be directly met, the direct emission is avoided, the solid waste is not generated, the service life of a coal gas pipeline can be prolonged due to the reduction of corrosion, the economic benefit and the social benefit are greatly improved, and the desulfurization cost is greatly reduced.
The sulfur in the blast furnace gas is mainly COS, and the desulfurization of the blast furnace gas is mainly performed by removing COS. Because the carbonyl sulfide has stable property, the carbonyl sulfide is difficult to directly react with other compounds in the oxygen-free environment of blast furnace gas, is not easy to dissociate or liquefy, and is difficult to remove.
There are many techniques currently employed for desulfurizing gases, most commonly by contacting an acid gas stream with an organic solvent (or aqueous solution of an organic solvent) in a gas purification unit. In general, there are two general different gas cleaning solvents.
The first is a physical solvent, relying on physical absorption. Typical physical solvents are sulfolane and its derivatives, linear amides, pyrrolidones, methanol and polyvinyl alcohol dialkyl ether mixtures.
The second is a chemical solvent, which is a compound that causes the acid gas to be easily removed by a chemical reaction. For example, the most common chemical solvents in industry are alcohol amines, which can be recycled because the salts produced are easily decomposed or easily stripped by steam. Preferred amines for removal of acidic components from gas streams are Monoethanolamine (MEA), diethanolamine (DEA), triethanolamine (TEA), diisopropanolamine (DIPA), aminoethoxyethanol (AEE), methyldiethanolamine (MDEA) and MDEA with various activators added.
Generally, the above solvents have high efficiency for removing H 2 S and CO 2, but have many difficulties for organic sulfur, especially carbonyl sulfide. Physical solvents can remove organic sulfur to very low levels, but their regeneration is expensive and not suitable for industrial large scale use. In the chemical solvent, the hydrolysis rate of various alcohol amine to COS is not high, the hydrolysis process is very slow, the removal rate is very low, and the thiol compound is only subjected to physical dissolution to remove the thiol, and the removal effect on organic sulfur is very poor because the hydrolysis degree of the thiol in the alcohol amine aqueous solution is very low. After the amine method treatment, catalytic hydrolysis or alkali washing and catalytic oxidation are often adopted to remove mercaptan, and then fixed bed dry method refined desulfurization is adopted, so that the total steps of desulfurization are numerous, the total flow is long, and the equipment is numerous, the investment is large and the total consumption index is high.
Therefore, in order to remove carbonyl sulfide in the blast furnace gas at the front end, the invention provides the compound solvent which can remove carbonyl sulfide in the blast furnace gas efficiently and deeply, does not need to add additional equipment, can be recycled and has high economic benefit.
Disclosure of Invention
Aiming at the problems existing in the prior art, the invention aims to provide a compound solvent for removing carbonyl sulfide in blast furnace gas, which can effectively promote the reaction of alcohol amine compounds for removing organic sulfur, in particular to promote the removal of alcohol amine compounds for removing carbonyl sulfide, and the removal rate of the alcohol amine compounds for removing carbonyl sulfide can be up to more than 90 percent.
In one aspect, the invention provides a composite solvent for removing carbonyl sulfide in blast furnace gas, which comprises 89-98.9 wt% of organic alcohol amine compound, 0.1-1 wt% of stabilizer, 0.5-5 wt% of activator and 0.5-5 wt% of accelerator.
Further, the primary alcohol amine compound has 3 to 8 carbon atoms, and the tertiary alcohol amine compound has 3 to 6 carbon atoms.
Further, the primary alcohol amine compound is 2-amino-2-methyl-1-propanol (AMP) and/or 2-amino-1, 3-butanediol, and the proportion of the primary alcohol amine compound in the organic alcohol amine compound is 10-30wt%.
Further, the tertiary alcohol amine compound is Methyl Diethanolamine (MDEA), and the tertiary alcohol amine compound accounts for 70-90wt% of the organic alcohol amine compound.
Preferably, the primary alcohol amine compound is present in an amount of 15 to 25wt% in the organic alcohol amine compound, and the tertiary alcohol amine compound is present in an amount of 75 to 85wt% in the organic alcohol amine compound.
Further preferably, the primary alcohol amine compound is 20wt% in the organic alcohol amine compound and the tertiary alcohol amine compound is 80wt% in the organic alcohol amine compound.
Preferably, the stabilizer is a polyether polyol and/or a polyethylene glycol alkyl ether.
Preferably, the polyether polyol is polyoxyethylene propylene glycol ether, polyoxyethylene glycerol ether, oxypropylene propylene glycol ether or polyoxypropylene glycerol ether, and the molecular weight of the polyether polyol is 800-4000.
Preferably, the carbon number of the alkyl group in the polyethylene glycol alkyl ether is 10-16, and the molecular weight of the polyethylene glycol alkyl ether is 400-4000.
Further preferably, the alkyl group in the polyethylene glycol alkyl ether has 12 carbon atoms.
Preferably, the activator is formyl morpholine and derivatives thereof.
Further preferably, the activator is N-formyl morpholine.
Preferably, the accelerator is hydroxyethylpiperazine.
Preferably, the pH of the complex solvent is 11-12.
In another aspect, the invention provides application of the compound solvent in removing carbonyl sulfide of blast furnace gas, and the compound solvent is used by adding water to dilute the concentration to 30-50 wt%.
Preferably, the compound solvent is used by diluting the concentration to 40wt% with water.
Further, the compound solvent is used after the hydrogen chloride is removed from the blast furnace gas, and the hydrogen chloride content in the blast furnace gas is lower than 5mg/m 3.
Further, the complex solvent is used in a pre-blast furnace gas desulfurization process.
Further, the volume gas-liquid ratio of the blast furnace gas to the composite solvent is 400-600.
Further preferably, the ratio of the volume gas to liquid of the blast furnace gas to the complex solvent is 500.
Further, the temperature of the blast furnace gas is not higher than 40 ℃ and the pressure is 10-20kPa.
The principle of removing carbonyl sulfide in blast furnace gas by the composite solvent provided by the invention is as follows: the compound solvent diluted by water is in gas-liquid reverse contact with blast furnace gas in a desulfurizing tower, and the mass transfer process of gas phase to liquid phase can be accelerated due to the existence of an accelerator, so that carbonyl sulfide in the gas is accelerated to diffuse into the liquid phase; the alcohol amine compound in the compound solvent can physically dissolve part of carbonyl sulfide, and then the carbonyl sulfide and the alcohol amine compound are subjected to hydrolysis reaction rapidly under the action of an activating agent to generate hydrogen sulfide and carbon dioxide, and the hydrogen sulfide and the carbon dioxide are further reacted with the alcohol amine compound in a desulfurizing tower to generate amine salt, so that the carbonyl sulfide in blast furnace gas is efficiently removed.
The mechanism of the reaction of carbonyl sulfide and alcohol amine compound is as follows:
Namely the total reaction is: COS+H 2O＝H2S+CO2
Wherein at least one of R 1,R2,R3 contains a hydroxyl group.
The mechanism of the reaction of hydrogen sulfide and alcohol amine compound to generate amine salt is as follows:
The mechanism of the reaction of carbon dioxide and alcohol amine compounds to produce amine salts is as follows:
the reaction of the hydrogen sulfide, the carbon dioxide and the alcohol amine compound to generate amine salt is reversible reaction, the reaction is carried out rightward under the low temperature condition, and the reaction is carried out leftward after heating.
The solution absorbing sulfide in the desulfurizing tower is called rich solution, the rich solution enters a regenerating tower and is heated and regenerated to obtain lean solution and acid gas, and the regenerated lean solution enters the desulfurizing tower for recycling, so that the compound solvent can be effectively recycled, and the running cost is reduced.
The beneficial effects of the invention are as follows:
1. The composite solvent provided by the invention can effectively remove organic sulfur (carbonyl sulfide) in blast furnace gas, the removal rate can be up to 90% or more, and the composite solvent has good selective absorption to inorganic sulfur (hydrogen sulfide), can be recycled, has no secondary pollutant emission, greatly reduces the operation cost, and has high economic benefit;
2. The composite solvent has high carbonyl sulfide removal efficiency, the hydrolysis reaction of the carbonyl sulfide after the contact of the carbonyl sulfide and the composite solvent is extremely fast, more than 90 percent of the carbonyl sulfide in the blast furnace gas can be effectively removed after the gas-liquid contact for 15-30 seconds, and the clean gas with the total sulfur content lower than the national ultra-low emission standard is generated and is directly supplied to each production unit at the downstream from the equipment outlet;
3. the compound solvent can be used at normal temperature (not higher than 40 ℃) and ultra-low pressure (10-20 kPa), has low equipment requirement, can be widely applied to a desulfurization process before blast furnace gas, and reduces the emission content of sulfur from the source.
Detailed Description
The following are specific examples of the present invention, and the technical solutions of the present invention are further described, but the scope of the present invention is not limited to these examples. All changes and equivalents that do not depart from the gist of the invention are intended to be within the scope of the invention.
Desulfurization performance was tested on a test apparatus with a specific complex solvent. Before the blast furnace gas enters the desulfurizing tower, the blast furnace gas is subjected to HCl removal treatment, so that the HCl content in the blast furnace gas is ensured to be lower than 5mg/m 3. In the test, the content of COS and H 2 S is measured at the inlet of the blast furnace gas of the desulfurizing tower (namely the raw gas), and the content of COS and H 2 S is measured at the outlet of the blast furnace gas of the desulfurizing tower (namely the purified gas) after the gas and the liquid are contacted for 15-30 seconds. The average was taken three times for each test condition. The specific test conditions are as follows:
Example 1:
Mother liquor: 9.9% by weight of 2-amino-2-methyl-1-propanol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyethylene glycol dodecyl ether (molecular weight 400), 0.5% by weight of N-formyl morpholine and 0.5% by weight of hydroxyethylpiperazine. Adding water to dilute the concentration of the mother solution to 30wt%, adding the diluted mother solution into a desulfurizing tower, controlling the gas-liquid ratio to be 400 (v/v), controlling the temperature to be 40 ℃ and controlling the air pressure to be 10kPa. The data obtained from the test are shown in Table 1.
Example 2:
Mother liquor: 9.9% by weight of 2-amino-2-methyl-1-propanol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyethylene glycol dodecyl ether (molecular weight 400), 0.5% by weight of N-formyl morpholine and 0.5% by weight of hydroxyethylpiperazine. Adding water to dilute the concentration of the mother solution to 30wt%, adding the diluted mother solution into a desulfurizing tower, controlling the gas-liquid ratio to be 500 (v/v), controlling the temperature to be 40 ℃ and controlling the air pressure to be 10kPa. The data obtained from the test are shown in Table 1.
Example 3:
Mother liquor: 9.9% by weight of 2-amino-2-methyl-1-propanol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyethylene glycol dodecyl ether (molecular weight 400), 0.5% by weight of N-formyl morpholine and 0.5% by weight of hydroxyethylpiperazine. Adding water to dilute the concentration of the mother solution to 30wt%, adding the diluted mother solution into a desulfurizing tower, controlling the gas-liquid ratio to be 600 (v/v), controlling the temperature to be 40 ℃ and controlling the air pressure to be 10kPa. The data obtained from the test are shown in Table 1.
Example 4:
Mother liquor: 9.9% by weight of 2-amino-2-methyl-1-propanol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyethylene glycol dodecyl ether (molecular weight 800), 0.5% by weight of N-formyl morpholine and 0.5% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 40℃and the air pressure was 10kPa. The data obtained from the test are shown in Table 1.
Example 5:
mother liquor: 9.9% by weight of 2-amino-2-methyl-1-propanol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyethylene glycol dodecyl ether (molecular weight 800), 0.5% by weight of N-formyl morpholine and 0.5% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 50wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 40℃and the air pressure was 10kPa. The data obtained from the test are shown in Table 1.
Example 6:
Mother liquor: 9.9% by weight of 2-amino-2-methyl-1-propanol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyethylene glycol dodecyl ether (molecular weight 4000), 0.5% by weight of N-formylmorpholine and 0.5% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 40℃and the air pressure was 10kPa. The data obtained from the test are shown in Table 1.
Example 7:
Mother liquor: 19.5% by weight of 2-amino-2-methyl-1-propanol, 78% by weight of methyldiethanolamine, 0.5% by weight of polyoxyethylene glycerol ether (molecular weight 800), 1% by weight of N-formylmorpholine and 1% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 40℃and the air pressure was 10kPa. The data obtained from the test are shown in Table 1.
Example 8:
Mother liquor: 23.2% by weight of 2-amino-2-methyl-1-propanol, 69.8% by weight of methyldiethanolamine, 1% by weight of polyoxyethylene glycerol ether (molecular weight 800), 3% by weight of N-formylmorpholine and 3% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 40℃and the air pressure was 10kPa. The data obtained from the test are shown in Table 1.
Example 9:
Mother liquor: 26.7% by weight of 2-amino-2-methyl-1-propanol, 62.3% by weight of methyldiethanolamine, 1% by weight of polyoxyethylene glycerol ether (molecular weight 800), 5% by weight of N-formylmorpholine and 5% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 40℃and the air pressure was 10kPa. The data obtained from the test are shown in Table 1.
Example 10:
Mother liquor: 9.9% by weight of 2-amino-1, 3-butanediol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyoxypropylene glycerol ether (molecular weight 2000), 0.5% by weight of formylmorpholine and 0.5% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 30℃and the air pressure was 20kPa. The data obtained from the test are shown in Table 1.
Example 11:
Mother liquor: 26.7% by weight of 2-amino-1, 3-butanediol, 62.3% by weight of methyl diethanolamine, 1% by weight of polyoxypropylene glycerol ether (molecular weight 2000), 5% by weight of formylmorpholine and 5% by weight of hydroxyethyl piperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 30℃and the air pressure was 20kPa. The data obtained from the test are shown in Table 1.
Example 12:
Mother liquor: 9.9% by weight of 2-amino-1, 3-butanediol, 89% by weight of methyldiethanolamine, 0.1% by weight of polyoxypropylene glycerol ether (molecular weight 4000), 0.5% by weight of formylmorpholine and 0.5% by weight of hydroxyethylpiperazine. After the mother liquor concentration was diluted to 40wt% by adding water, it was fed into a desulfurizing tower, the gas-liquid ratio was controlled to 500 (v/v), the temperature was 30℃and the air pressure was 20kPa. The data obtained from the test are shown in Table 1.
Table 1: COS and H 2 S content in raw material gas and purified gas and removal rate thereof
As can be seen from the data in Table 1, the removal rate of carbonyl sulfide in blast furnace gas by the composite solvent provided by the application is very high, and can reach more than 90% under most conditions, and meanwhile, the removal rate of hydrogen sulfide can also reach more than 70%, the total sulfur content of the purified gas is lower than the national ultra-low emission standard (35 mg/Nm 3), and the purified gas can be directly supplied to each production unit at the downstream from the equipment outlet without secondary treatment.
The foregoing describes in detail preferred embodiments of the present invention. It should be understood that numerous modifications and variations can be made in accordance with the concepts of the invention without requiring creative effort by one of ordinary skill in the art. Therefore, all technical solutions which can be obtained by logic analysis, reasoning or limited experiments based on the prior art by the person skilled in the art according to the inventive concept shall be within the scope of protection defined by the claims.
Claims (5)
1. The application of the compound solvent in the pre-blast furnace gas desulfurization process is characterized in that the application comprises the step of carrying out gas-liquid reverse contact on the compound solvent diluted by water and the blast furnace gas in a desulfurizing tower;
the compound solvent comprises 89-98.9wt% of an organic alcohol amine compound, 0.1-1wt% of a stabilizer, 0.5-5wt% of an activating agent and 0.5-5wt% of an accelerator, wherein the organic alcohol amine compound comprises a primary alcohol amine compound and a tertiary alcohol amine compound;
The primary alcohol amine compound is 2-amino-2-methyl-1-propanol and/or 2-amino-1, 3-butanediol, and the proportion of the primary alcohol amine compound in the organic alcohol amine compound is 10-30wt%;
The tertiary alcohol amine compound is methyl diethanolamine, and the proportion of the tertiary alcohol amine compound in the organic alcohol amine compound is 70-90wt%;
The stabilizer is polyether polyol, wherein the polyether polyol is polyoxyethylene propylene glycol ether, polyoxyethylene glycerol ether, oxypropylene propylene glycol ether or polyoxypropylene glycerol ether, and the molecular weight of the polyether polyol is 800-4000; and/or the stabilizer is polyethylene glycol alkyl ether, wherein the carbon number of an alkyl group in the polyethylene glycol alkyl ether is 10-16, and the molecular weight of the polyethylene glycol alkyl ether is 400-4000;
the activator is formyl morpholine and derivatives thereof;
the accelerator is hydroxyethyl piperazine;
when the compound solvent is used, water is added to dilute the concentration to 30-50wt%;
the blast furnace gas is contacted with the compound solvent diluted by water after hydrogen chloride is removed, and the hydrogen chloride content in the blast furnace gas after hydrogen chloride is removed is lower than 5mg/m 3;
The volume gas-liquid ratio of the blast furnace gas after hydrogen chloride removal to the composite solvent diluted by water is 400-600;
the temperature of the blast furnace gas after hydrogen chloride removal is not higher than 40 ℃ and the pressure is 10-20kPa.
2. The use according to claim 1, wherein the primary alcohol amine compound comprises 20wt% of the organic alcohol amine compound and the tertiary alcohol amine compound comprises 80wt% of the organic alcohol amine compound.
3. The use according to claim 1, wherein the number of carbon atoms in the alkyl group in the polyethylene glycol alkyl ether is 12.
4. Use according to claim 1, wherein the compound solvent is diluted to a concentration of 40wt% with water when in use.
5. The use according to claim 1, wherein the ratio of the volume gas to liquid of the blast furnace gas after removal of hydrogen chloride to the complex solvent diluted with water is 500.
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| CN1421264A (en) * | 2002-12-11 | 2003-06-04 | 南化集团研究院 | Absorbing liquid for eliminating sulfide from gas mixture |
| CN106540515A (en) * | 2015-09-18 | 2017-03-29 | 中国石油化工股份有限公司 | A kind of accelerator for removing cos and mercaptan simultaneously |
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| EA025250B1 (en) * | 2010-12-06 | 2016-12-30 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Process for removing mercaptans from a gas stream |
| CN103495340B (en) * | 2013-10-15 | 2015-11-18 | 北京博源恒升高科技有限公司 | The method of SOx in compound alcamines solution removal gas |
| KR20170067782A (en) * | 2014-10-10 | 2017-06-16 | 다우 글로벌 테크놀로지스 엘엘씨 | Aqueous solution of 2-dimethylamino-2-hydroxymethyl-1,3-propanediol useful for acid gas removal from gaseous mixtures |
| BR112017012849A2 (en) * | 2014-12-18 | 2018-01-09 | Hexion Inc | method for sequestering a sulfur-containing compound from a sulfur-containing gas stream, multicomponent sequestering system, and treated stream. |
| CN106881021B (en) * | 2017-04-27 | 2019-10-11 | 河北精致科技有限公司 | After a kind of processing can direct emission tail gas of sulphur purification process |
| CN108325338A (en) * | 2018-03-28 | 2018-07-27 | 东北石油大学 | A kind of preparation method for removing the ionic liquid compounding agent of carbonyl sulfur |
| CN109865400A (en) * | 2018-10-16 | 2019-06-11 | 上海赛思特新能源科技有限公司 | Laminated desulfurizer and preparation method thereof |
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|---|---|---|---|---|
| CN1421264A (en) * | 2002-12-11 | 2003-06-04 | 南化集团研究院 | Absorbing liquid for eliminating sulfide from gas mixture |
| CN106540515A (en) * | 2015-09-18 | 2017-03-29 | 中国石油化工股份有限公司 | A kind of accelerator for removing cos and mercaptan simultaneously |
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