CN108840311B - Hydrogen sulfide liquid-phase oxidation removal method using eutectic solvent as medium - Google Patents
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- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
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Abstract
The invention discloses a eutectic solutionA method for removing hydrogen sulfide by liquid phase oxidation with an agent as a medium belongs to the field of chemical separation. The invention takes one or a mixture of more of amide derivatives and glycol derivatives as a hydrogen bond donor, imidazole salt, quaternary ammonium salt or choline as a hydrogen bond acceptor, and mixes the two or more of amide derivatives and glycol derivatives according to a certain molar ratio to obtain a plurality of functional eutectic solvents, wherein the eutectic solvents have stable physicochemical properties, are cheap and easy to prepare, and have H resistance2The S gas has the characteristics of excellent solubility, easy recovery and the like. The eutectic solvent designed by the invention can be used for H in various sulfur-containing gas sources2S gas, to H efficiently2Selective capture of S gas and ordinary-temp liquid-phase oxidation of enriched H2S is quickly converted into high-purity sulfur, the eutectic solvent can be regenerated and reused after being dried, and the whole process has the advantages of high desulfurization efficiency, mild operation conditions, low energy consumption, no discharge of VOCs and the like, and is novel green and efficient H2S oxidation removal method.
Description
Technical Field
The invention belongs to the field of chemical separation, relates to a method for removing hydrogen sulfide and recycling the hydrogen sulfide, and particularly relates to a method for converting hydrogen sulfide into sulfur through room-temperature high-efficiency liquid-phase oxidation after the hydrogen sulfide is enriched in a eutectic solvent.
Background
Hydrogen sulfide (H)2S) is a highly corrosive and combustible extremely toxic gas, which is widely existed in gas fuels such as natural gas, refinery gas, synthetic gas and the like, and also in industrial and agricultural gases such as coal bed gas, methane and the like. H2The presence of S not only seriously threatens the environment and personal safety, but also causes corrosion of equipment and pipelines, catalyst poisoning and the like in the process of gas transportation and utilization. How to treat highly toxic and highly corrosive H2The safe and reliable storage and the green and efficient resource utilization of S gas are one of the most challenging subjects, and the development of an efficient hydrogen sulfide separation technology is to reduce H in the atmosphere2S concentration is the most effective strategy. Currently, the industry currently traps and removes H2The method of S mainly comprises a dry method and a wet method. Common dry desulfurization methods include membrane separation, solid adsorption-catalytic oxidation, gas-phase Claus, and the like. Compared with the dry method, the wet method removes H2S is always the main technical flow of industrial processes, most typical alcohol amine method, and the application process thereofThere are also a number of bottleneck problems: (1) trapping and removing H2The energy consumption in the S process is high; (2) most alcohol amine absorbents are volatile, and Volatile Substances (VOCs) can be generated and discharged into the atmosphere in the using process to form secondary pollution; (3) organic amines are susceptible to degradation or oxidation resulting in reduced desulfurization efficiency. Thus, green and efficient H was developed2The S trapping method has extremely important scientific and practical significance.
Eutectic solvents (DESS) as a new class of green solvents, usually composed of a stoichiometric combination of hydrogen bond acceptors and hydrogen bond donors, have properties very similar to ionic liquids, especially in the field of gas separation, whether in H2Whether S or SO2In terms of removal, the DESS all showed excellent absorption and regeneration performance, while with respect to H2In situ conversion studies after S trapping progress relatively slowly if H can be trapped2S and SO2By the Claus process (the Claus method is a method using SO)2H is to be2The classical process of S oxidation into elemental sulfur) can realize the maximum recovery of elemental sulfur, and the produced sulfur can be widely used for manufacturing dyes, pesticides, matches, gunpowder, rubber and the like. Early gas phase Claus process used metal oxides as catalysts (reaction temperature)>180 ℃), but the generated sulfur is easy to be condensed on the surface of the solid catalyst to deactivate the catalyst and is often accompanied by 3-5% of H2The S gas remains in the Claus process tail gas and requires an additional purification process to treat the Claus tail gas, while the liquid-phase Claus processes reported in U.S. Pat. Nos. 5733516A, 592860A and 7381393B2 can effectively overcome the problems of the gas-phase Claus process and realize the H conversion under relatively mild conditions2And (4) complete conversion of S. The novel liquid-phase Claus process usually uses polyethylene glycol ether as a reaction medium, but the volatilization problem of an organic solvent is still difficult to overcome, VOCs which are harmful to the environment are generated, and a plurality of problems are brought to the actual operation process. Therefore, the existing Claus process needs to be further improved in green color. Considering that the traditional Claus process needs to ensure higher H in the system2S concentration and in excess of SO2The reaction can be fully carried out under the condition of (1), so that the Claus process is carried out at low H2S contentThe application of the gas treatment field of (2) is limited. Therefore, how to reduce the concentration of H2S enrichment is the key to efficient performance of a liquid-phase Claus process. The applicant of the present patent provides in Chinese patent CN105521696A6 the use of dissolved SO2To absorb H by means of Ionic Liquids (ILs)2Method of S, corresponding H2S can be converted into SO with the conversion rate of 96 percent2The reaction produces sulfur, but the process is still limited by H2Low solubility of S in ILs. In contrast, DESS is for H2S has better absorption and enrichment capacity, and the Claus process is used for treating low H2The S content gas provides a first opportunity. At present, numerous published patents (CN101961598A, CN101993378A, CN103159632A, US2009291872A1 and WO2009142663A1) are only reports H2Novel process for reversible trapping of S in absorbent, and no DESs for trapping H2S and related methods for in situ conversion thereof are reported, and particularly, the application of DESS to a liquid phase oxidation process is obviously more attractive by replacing the traditional volatile organic solvent with DESs.
Disclosure of Invention
The purpose of the invention is as follows: the invention aims to provide a hydrogen sulfide liquid-phase oxidation removal method taking a eutectic solvent as a medium, aiming at the defects of the prior art.
In order to achieve the above purpose, the invention adopts the following technical scheme:
a liquid-phase oxidizing process for removing hydrogen sulfide from the eutectic solvent features that one or two of amide derivative and glycol derivative are used as hydrogen bond donor and one of imidazole salt, quaternary ammonium salt and choline is used as hydrogen bond acceptor to proportionally combine the eutectic solvent to obtain H2S and H to be trapped2S is converted into sulfur by a room temperature liquid phase oxidation method, and the method comprises the following specific steps:
(1) firstly, mixing a hydrogen bond donor and a hydrogen bond acceptor according to a certain molar ratio, stirring at a proper temperature to enable the hydrogen bond donor and the hydrogen bond acceptor to be eutectic, cooling to room temperature to obtain a liquid, namely a eutectic solvent, wherein the mass percentage of water in the prepared eutectic solvent is less than 0.5%;
(2) reacting the eutectic solvent with hydrogen2S-shaped suckerFeeding the mixture into the top of a tower collecting device, and absorbing H containing a certain volume fraction entering from the bottom of the tower in a countercurrent manner2S gas to be treated, to make H2S is enriched in the eutectic solvent to form H2The rich S solution is used for subsequent oxidation;
(3) from SO of the above eutectic solvent2The SO with a certain volume fraction entering from the top of the absorption tower is absorbed in a countercurrent way2Gas to be treated, SO2SO formed by enrichment in eutectic solvent2The rich solution is used for subsequent oxidation;
(4) h obtained in the step is2S and SO2The rich solutions are respectively pumped to a liquid phase oxidation reaction tower, mixed in a static mixer at the top of the tower and then enter the liquid phase oxidation reaction tower to react to obtain eutectic solvent emulsion containing sulfur;
(5) discharging the emulsion of the eutectic solvent containing sulfur from the bottom of the liquid phase oxidation reaction tower, feeding the emulsion into a filtering, washing and drying integrated machine to filter out the eutectic solvent, separating and drying to obtain a sulfur finished product, drying and regenerating the filtered eutectic solvent by a drying unit to ensure that the mass percentage of water in the eutectic solvent is less than 0.5%, and feeding the eutectic solvent into H again2S absorption tower and SO2Absorption tower, excess H in tail gas of liquid phase oxidation reaction tower2S then re-enters H2And (5) an S absorption tower.
Preferably, the molar ratio of the hydrogen bond donor to the hydrogen bond acceptor is (1-5) to (1-5), and the stirring temperature is between room temperature and 150 ℃.
Preferably, the hydrogen bond donor amide and the derivative thereof are one of acetamide, urea, 1, 3-dimethyl urea, 2-imidazolidone and 2-pyrrolidone; the hydrogen bond donor diol derivative is one of ethylene glycol, diethylene glycol, triethylene glycol, tetraethylene glycol, polyethylene glycol, 1, 3-butanediol, 1, 4-butanediol and glycerol; the hydrogen bond receptor choline is one of betaine (Beta) and choline chloride (ChCl); the hydrogen bond acceptor quaternary ammonium salt is tetraethylammonium chloride (N)2222Cl), triethylbutylammonium chloride (N)2224Cl), tetrabutylammonium chloride (N)4444Cl); the hydrogen bond receptor imidazole salt is 1-ethyl-3-methylimidazole chloride (EmimCl) or 1-butyl chloride-3-methylimidazole (BmimCl), 1-hexyl-3-methylimidazole chloride (HmimCl), 1-ethyl-3-methylimidazole thiocyanate (EmimSCN), 1-butyl-3-methylimidazole thiocyanate (bmimsccn), 1-hexyl-3-methylimidazole thiocyanate (hmimsccn).
Preferably, said H2The operation temperature of the S absorption tower is room temperature, the operation pressure is 1.0Mpa, and the operation liquid-gas ratio is 8-10 Kg/Nm3Introduced into a reaction vessel containing H2S the gas to be treated is H2One of natural gas, coke oven gas and hydrodesulfurization gas with the S volume fraction of 0.8-1.8%.
Preferably, said SO2The operation temperature of the absorption tower is room temperature, the operation pressure is 0.1Mpa, and the operation liquid-gas ratio is 40-50 Kg/Nm3Introduced with SO-containing gas2The gas to be treated is SO20.2% by volume of coal-fired flue gas.
Preferably, the operation temperature of the top of the liquid phase oxidation reaction tower is normal temperature, the operation temperature of the bottom of the liquid phase oxidation reaction tower is 60-80 ℃, the operation pressure is 1.0Mpa, and H is2S relative to SO2In stoichiometric excess of 0 to 15%.
Preferably, said H2S absorption tower and SO2The absorption tower is a mellapak250Y packed tower.
Has the advantages that:
compared with the prior art, the invention has the beneficial effects that:
(1) the DESs screened by the invention have stable physical and chemical properties, are cheap and easy to prepare, can be recycled, and can simultaneously carry out H treatment2S and SO2Has excellent solubility, and the developed H2The S normal temperature liquid phase oxidation method has the advantages of low operation temperature, low energy consumption, no subsequent tail gas treatment, no VOCs emission and capability of obtaining high-purity sulfur.
(2) The invention relates to a medium H using DESs2The S liquid phase oxidation method is suitable for various sulfur-containing gas sources (natural gas, coke oven gas, hydrodesulfurization gas, industrial waste gas, industrial raw material gas and the like), and can effectively realize the H gas oxidation2And (4) removing S, and simultaneously obtaining high-purity sulfur.
Drawings
FIG. 1 is a schematic of the process of the present invention;
1 is SO2Absorption column, 2 is H2And the S absorption tower, 3 is a liquid-phase oxidation reaction tower, 4 is a filtering, separating and drying integrated machine, and 5 is a drying unit.
Detailed Description
The invention is further described with reference to specific examples.
Example 1: taking 1-ethyl-3-methylimidazole-2-imidazolidinone chloride (molar ratio of 1:2) as an example of the preparation of the eutectic solvent, the preparation method comprises the steps of mixing a hydrogen bond donor 2-imidazolidinone and a hydrogen bond acceptor 1-ethyl-3-methylimidazole chloride according to the molar ratio of 1:2, stirring at 80 ℃ to enable the two to be eutectic, and cooling to room temperature to obtain a liquid, namely the eutectic solvent. The preparation of the eutectic solvents used in the following examples is similar.
Example 2: the method for removing hydrogen sulfide by liquid phase oxidation with eutectic solvent as medium is shown in figure 1, and is implemented by subjecting H2Natural gas with S volume fraction of 0.8% from H2The bottom of the S absorption tower 1 is input, and the eutectic solvent chlorinated 1-ethyl-3-methylimidazole-2-imidazolidinone (molar ratio is 1:2) is input from the top of the absorption tower 1. H2The operation temperature of the S absorption tower 1 is room temperature, the operation pressure is 1.0MPa, and the operation liquid-gas ratio is 10Kg/Nm3. Adding SO2From SO with a volume fraction of 0.2% of coal-fired flue gas2The bottom of the absorption tower 2 is fed with the eutectic solvent chlorinated 1-ethyl-3-methylimidazole-2-imidazolidinone (molar ratio of 1:2) from the top of the absorption tower 2. SO (SO)2The operation temperature of the absorption tower 2 is room temperature, the operation pressure is 0.1MPa, and the operation liquid-gas ratio is 50Kg/Nm3. The packing used for absorption columns 1 and 2 was mellapak 250Y. Respectively contain H2S and SO2The rich solution enters a liquid phase oxidation reaction tower 3 after being mixed in a static mixer, the operation temperature at the top of the tower is room temperature, the operation temperature at the bottom of the tower is 60 ℃, the operation pressure is 1.0MPa, wherein H is2S relative to SO2In a stoichiometric excess of 12%. The emulsion of eutectic solvent chloridized 1-ethyl-3-methylimidazole-2-imidazolidinone (molar ratio is 1:2) containing sulfur enters a filtering, washing and drying integrated machine 4 from the bottom of a reaction tower 3 to be filtered and removed of the eutectic solvent, and the mixture is separated,Drying to obtain a sulfur finished product, drying and regenerating the eutectic solvent chlorinated 1-ethyl-3-methylimidazole-2-imidazolidinone (molar ratio of 1:2) by a drying unit 5 to ensure that the mass percentage of water in the eutectic solvent is less than 0.5%, and then sending the eutectic solvent chlorinated 1-ethyl-3-methylimidazole-2-imidazolidinone into absorption towers 1 and 2 for recycling. H in natural gas washed by eutectic solvent chlorinated 1-ethyl-3-methylimidazole-2-imidazolidinone (molar ratio of 1:2)2S and SO in coal-fired flue gas2The content of (b) is determined by a dynamic flue gas analyzer. The analysis result showed that H2The S removal rate is more than or equal to 99.2 percent, and H is obtained after natural gas purification2The S content is reduced to 30mg/m3The loss rate of natural gas is less than 1.0 percent, and SO in the purified tail gas2The content of (A) is less than 10mg/m3Based on SO2The recovery rate of sulfur is more than or equal to 98.0 percent.
Example 3: the process is similar to example 2, see FIG. 1, and H2Coke oven gas with 3% S volume fraction from H2The bottom of the S absorption tower 1 is input, and the eutectic solvent chlorinated 1-butyl-3-methylimidazole-2-pyrrolidone (molar ratio is 1:2) is input from the top of the absorption tower 1. H2The operation temperature of the S absorption tower 1 is room temperature, the operation pressure is 1.0MPa, and the operation liquid-gas ratio is 8Kg/Nm3. Adding SO2From SO with a volume fraction of 0.2% of coal-fired flue gas2The bottom of the absorption tower 2 is fed with low cosolvent chlorinated 1-butyl-3-methylimidazole-2-pyrrolidone (molar ratio is 1:2) from the top of the absorption tower 1. SO (SO)2The operation temperature of the absorption tower 2 is room temperature, the operation pressure is 0.1MPa, and the operation liquid-gas ratio is 40Kg/Nm3. The packing used for absorption columns 1 and 2 was mellapak 250Y. Respectively contain H2S and SO2The rich solution enters a liquid phase oxidation reaction tower 3 after being mixed in a static mixer, the operation temperature at the top of the tower is room temperature, the operation temperature at the bottom of the tower is 80 ℃, the operation pressure is 1.0MPa, wherein H is2S relative to SO2In a stoichiometric excess of 8%. The emulsion of eutectic solvent chloridized 1-butyl-3-methylimidazole-2-pyrrolidone (molar ratio is 1:2) containing sulfur enters a filtering, washing and drying integrated machine 4 from the bottom of a reaction tower 3 to be filtered to remove the eutectic solvent, and the sulfur finished product is obtained by separation and drying, wherein the eutectic solvent chloridized 1-butyl-3-methylimidazole-2-pyrrolidone (molar ratio is 1:2) is dried and regenerated by a drying unit 5 to ensure that the water in the eutectic solvent chloridized 1-butyl-3-methylimidazole-2-pyrrolidone (molar ratio is 1:2) contains water by mass percentageThe amount is less than 0.5 percent, and then the waste gas is sent into the absorption towers 1 and 2 for reuse. H in natural gas after low cosolvent washing of 1-butyl-3-methylimidazole-2-pyrrolidone (molar ratio of 1:2)2S and SO in coal-fired flue gas2The content is determined by a dynamic flue gas analyzer. The analysis result showed that H2The removal rate of S is more than or equal to 99.0 percent, and the content of hydrogen sulfide is reduced to 45mg/m after the coke oven gas is purified3The loss rate of the coke oven gas is less than 1.3 percent, and the SO in the tail gas is purified2The content of (A) is less than 10mg/m3Based on SO2The recovery rate of sulfur is more than or equal to 98.0 percent.
Example 4: the process is similar to example 2, see FIG. 1, and H2Hydrodesulfurization of 1.8% S by volume from H2The bottom of the S absorption tower 1 is input, and the eutectic solvent chlorinated 1-hexyl-3-methylimidazole-acetamide (molar ratio is 1:1) is input from the top of the absorption tower 1. H2The operation temperature of the S absorption tower 1 is room temperature, the operation pressure is 1.0MPa, and the operation liquid-gas ratio is 10Kg/Nm3. Adding SO2From SO with a volume fraction of 0.2% of coal-fired flue gas2The bottom of the absorption tower 2 is fed with a eutectic solvent, namely 1-hexyl-3-methylimidazole-acetamide chloride (molar ratio is 1:1), and the top of the absorption tower 1 is fed with the eutectic solvent. SO (SO)2The operation temperature of the absorption tower 2 is room temperature, the operation pressure is 0.1MPa, and the operation liquid-gas ratio is 50Kg/Nm3. The packing used for absorption columns 1 and 2 was mellapak 250Y. Respectively contain H2S and SO2The rich solution enters a liquid phase oxidation reaction tower 3 after being mixed in a static mixer, the operation temperature at the top of the tower is room temperature, the operation temperature at the bottom of the tower is 60 ℃, the operation pressure is 1.0MPa, wherein H is2S relative to SO2In stoichiometric excess of 5%. The emulsion of sulfur-containing eutectic solvent chlorinated 1-hexyl-3-methylimidazole-acetamide (molar ratio is 1:1) enters a filtering, washing and drying integrated machine 4 from the bottom of a reaction tower 3 to be filtered and removed of the eutectic solvent, and sulfur finished products are obtained by separation and drying, wherein the eutectic solvent is triethyl butyl ammonium chloride (N)2224Cl) -malonic acid (mol ratio of 2:1) is dried and regenerated by a drying unit 5 to ensure that the water content is less than 0.5 percent by mass, and then the obtained product is sent into absorption towers 1 and 2 for reuse. H in natural gas washed by eutectic solvent chlorinated 1-hexyl-3-methylimidazole-acetamide (molar ratio of 1:1)2S and fuelSO in coal flue gas2The content is determined by a dynamic flue gas analyzer. The analysis result showed that H2S removal rate is more than or equal to 99.0%, and H is obtained after coke oven gas purification2The S content is reduced to 40mg/m3The loss rate of the coke oven gas is less than 1.0 percent, and the SO in the tail gas is purified2The content of (A) is less than 15mg/m3Based on SO2The recovery rate of sulfur is more than or equal to 98.0 percent.
The above eutectic solvent and other typical eutectic solvents, their specific ratio, H2The S removal rate and sulfur recovery rate are shown in the following table:
the foregoing shows and describes the general principles, essential features, and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are described in the specification and illustrated only to explain the principles of the invention, and that various changes and modifications may be made therein without departing from the spirit and scope of the invention. The scope of the invention is defined by the appended claims, the description and their equivalents.
Claims (6)
1. A hydrogen sulfide liquid phase oxidation removal method taking a eutectic solvent as a medium is characterized in that: the amide derivative is used as a hydrogen bond donor, the imidazole salt is used as a hydrogen bond acceptor, or the amide derivative and the glycol derivative are used as the hydrogen bond donor, the quaternary ammonium salt is used as the hydrogen bond acceptor, the eutectic solvent is combined in proportion, and H is treated2S and H to be trapped2S is converted into sulfur by a room temperature liquid phase oxidation method, and the molar ratio of the hydrogen bond donor to the hydrogen bond acceptor is (1-5) to (1-5);
the amide derivative is one of urea, 1, 3-dimethyl urea, 2-imidazolidinone and 2-pyrrolidone;
the imidazole salt is one of 1-ethyl-3-methylimidazole chloride, 1-butyl-3-methylimidazole chloride, 1-hexyl-3-methylimidazole chloride, 1-ethyl-3-methylimidazole thiocyanate, 1-butyl-3-methylimidazole thiocyanate and 1-hexyl-3-methylimidazole thiocyanate;
the diol derivative is one of ethylene glycol, diethylene glycol, triethylene glycol, tetraethylene glycol, polyethylene glycol, 1, 3-butanediol, 1, 4-butanediol and glycerol;
the quaternary ammonium salt is one of tetraethylammonium chloride, triethylbutylammonium chloride and tetrabutylammonium chloride;
the method comprises the following specific steps:
(1) firstly, mixing a hydrogen bond donor and a hydrogen bond acceptor according to a certain molar ratio, stirring at a proper temperature to enable the hydrogen bond donor and the hydrogen bond acceptor to be eutectic, cooling to room temperature to obtain a liquid, namely a eutectic solvent, wherein the mass percentage of water in the prepared eutectic solvent is less than 0.5%;
(2) reacting the eutectic solvent with hydrogen2The S absorption tower (1) enters from the top and countercurrent absorbs H with a certain volume fraction entering from the bottom2S is a gas to be treated to make H2S is enriched in the eutectic solvent to form H2The rich S solution is used for subsequent oxidation;
(3) from SO of the above eutectic solvent2The absorption tower (2) enters from the top and countercurrent absorbs SO with a certain volume fraction entering from the bottom of the tower2To treat the gas to make SO2SO formed by enrichment in eutectic solvent2The rich solution is used for subsequent oxidation;
(4) h obtained in the step is2S and SO2The rich solutions are respectively pumped to a liquid phase oxidation reaction tower (3), mixed in a static mixer at the top of the tower and then enter the liquid phase oxidation reaction tower (3), and then react to obtain eutectic solvent emulsion containing sulfur;
(5) discharging the emulsion of the eutectic solvent containing sulfur from the bottom of the liquid phase oxidation reaction tower (3), sending the emulsion into a filtering, washing and drying integrated machine (4) to filter out the eutectic solvent, separating and drying to obtain a sulfur finished product, and drying and regenerating the filtered eutectic solvent by a drying unit (5) to obtain the sulfur finished productWater content in percentage by mass<0.5% of the total amount of hydrogen and hydrogen2S absorption tower (1) and SO2Excessive H in tail gas of the absorption tower (2) and the liquid phase oxidation reaction tower (3)2S then re-enters H2S absorption tower (1).
2. The liquid-phase oxidation removal method of hydrogen sulfide using eutectic solvent as medium according to claim 1, wherein the stirring temperature is from room temperature to 150 ℃.
3. The method for removing hydrogen sulfide by liquid phase oxidation using eutectic solvent as medium according to claim 1, wherein said H is2The operation temperature of the S absorption tower (1) is room temperature, the operation pressure is 1.0MPa, and the operation liquid-gas ratio is 8-10 Kg/Nm3Introduced into a reaction vessel containing H2S the gas to be treated is H2One of natural gas, coke oven gas and hydrodesulfurization gas with the S volume fraction of 0.8-1.8%.
4. The method for removing hydrogen sulfide by liquid phase oxidation using eutectic solvent as medium according to claim 1, wherein said SO2The operation temperature of the absorption tower (2) is room temperature, the operation pressure is 0.1MPa, and the operation liquid-gas ratio is 40-50 Kg/Nm3Introduced with SO-containing gas2The gas to be treated is coal-fired flue gas with H2S volume fraction of 0.2%.
5. The method for removing hydrogen sulfide by liquid phase oxidation using eutectic solvent as medium according to claim 1, wherein the operation temperature of the top of the liquid phase oxidation reaction tower (3) is normal temperature, the operation temperature of the bottom of the tower is 60-80 ℃, the operation pressure is 1.0MPa, and H is H2S relative to SO2In stoichiometric excess of 0 to 15%.
6. The method for removing hydrogen sulfide by liquid phase oxidation using eutectic solvent as medium according to claim 1, wherein said H is2S absorption tower (1) and SO2The absorption column (2) is a packed column with a packings of melapak 250Y.
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| CN110128235B (en) * | 2019-05-15 | 2020-12-11 | 北京化工大学 | Eutectic solvent, preparation method thereof and application of eutectic solvent as extractant |
| CN110172365A (en) * | 2019-06-14 | 2019-08-27 | 山东管理学院 | The removal methods of the preparation of hydrogen sulfide absorption liquid, regeneration method and hydrogen sulfide |
| CN110180330A (en) * | 2019-06-25 | 2019-08-30 | 中国石油大学(华东) | For removing the New Absorbent and its preparation method and application of sulfide in exhaust gas |
| CN110448996A (en) * | 2019-08-21 | 2019-11-15 | 浙江工业大学 | A method of being based on Emim [Cl] eutectic solvent capture sulfur dioxide |
| CN110756002A (en) * | 2019-10-23 | 2020-02-07 | 中国石油化工股份有限公司 | Absorption liquid and method for recovering sulfur from gas containing hydrogen sulfide and sulfur dioxide |
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| US8852540B2 (en) * | 2011-06-22 | 2014-10-07 | Yeda Research And Development Co. Ltd. | Apparatus and method for removing sulfur dioxide from flue gases |
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| CN105521696B (en) * | 2015-11-26 | 2018-01-23 | 南京大学 | A kind of normal temperature liquid phase Claus techniques using ionic liquid as medium |
| CN106823744A (en) * | 2017-02-20 | 2017-06-13 | 中国科学院过程工程研究所 | A kind of preparation method of high selectivity desulphurization system and its desulfurizing agent |
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| CN107670464A (en) * | 2017-10-25 | 2018-02-09 | 北京化工大学 | A kind of process regenerated with eutectic solvent absorbing sulfur dioxide in flue and use hydrogen sulfide |
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