Organic sulfur hydrolysis synergistic sulfur recovery catalyst as well as preparation method and application thereof

Abstract

The invention belongs to the technical field of sulfur recovery, and particularly relates to an organic sulfur hydrolysis synergistic sulfur recovery catalyst as well as a preparation method and application thereof. Comprising the following steps: (1) dissolving strontium salt; (2) adding transition metal salt; (3) adding a titanium source; (4) adding an alkali metal compound; (5) stirring reaction; (6) hydro-thermal treatment; and (7) centrifuging, washing, drying and roasting. The general formula of the prepared catalyst is SrTi (1-x) MxO3, in the formula, x is equal to 0.05-0.2, and M is a transition metal element. The prepared catalyst is high in material composition and structure adjustability, rich in surface acid-base sites, excellent in organic sulfur hydrolysis reaction activity and H2S selective oxidation activity, and capable of realizing efficient and synergistic proceeding of organic sulfur hydrolysis and H2S selective oxidation and removing sulfur-containing components in process gas in one step.

Description

Technical Field

[0001] The invention belongs to the technical field of sulfur recovery, and in particular relates to an organic sulfur hydrolysis synergistic sulfur recovery catalyst and a preparation method and application thereof. Background Art

[0002] With the rapid development of my country's economy, the contradiction between resource supply and demand and environmental pollution problems have become increasingly prominent. The scientific use of high-sulfur resources and the reduction of sulfur-containing pollutant emissions have received widespread attention from the society. In addition to inorganic sulfur (mainly H2S, SO2, etc.), industrial gases prepared from coal, oil and natural gas also contain various organic sulfides (mainly COS). In industrial production, sulfides in raw gas often cause corrosion loss of pipeline equipment and poisoning and deactivation of catalytic materials, especially catalytic materials. Most of them are very sensitive to sulfur elements, and even trace amounts of sulfur may cause serious effects. Therefore, in order to ensure the normal progress of industrial production, the raw gas must be deeply purified and finely desulfurized before use. In addition, sulfides discharged without effective treatment will not only endanger human health, but also have a serious impact on the atmospheric environment. At present, the desulfurization process technology commonly used in industry mainly treats inorganic H2S and SO2 gases, lacks effective treatment of COS, and the residual COS has become one of the main factors restricting the utilization and emission of sulfur-containing gases. Its efficient removal is the key to achieving fine desulfurization of industrial gases. Therefore, pollution control of organic sulfur gas is an issue that must be addressed by related industries.

[0003] At present, the pollution control technology for organic sulfur gas mainly involves a staged treatment process that first catalytically hydrolyzes organic sulfur into H2S and then removes H2S by catalytic oxidation. This process is complex and has a long operation flow, and fails to comprehensively consider the conversion reaction of organic sulfur hydrolysis and subsequent hydrolysis product H2S. Under the current global environmental protection trend of advocating energy conservation and emission reduction and emphasizing the coordinated control of multiple pollutants, it is imperative to develop a one-step desulfurization method for organic sulfur hydrolysis and sulfur recovery.

[0004] Chinese patent CN118237005A discloses a catalyst for catalyzing the hydrolysis of organic sulfur to generate hydrogen sulfide. The catalyst is composed of an alumina additive, a first metal oxide additive and a second potassium species additive, wherein the alumina carrier content is 70-96wt%, the first metal oxide additive content is 0.2-12wt%, and the second potassium species additive content is 3.8-18wt%. The catalyst can realize the efficient catalytic hydrolysis of carbon disulfide and / or sulfur oxide in industrial coal gas into hydrogen sulfide. However, it does not involve the subsequent treatment of H2S generated after catalytic hydrolysis.

[0005] Chinese patent CN117414809A discloses an organic sulfur hydrolysis catalyst, preparation method and application, wherein titanium-containing pseudo-boehmite is obtained by adding a water-soluble titanium-containing compound and a surfactant, and then the titanium-containing pseudo-boehmite is molded to obtain an organic sulfur hydrolysis catalyst. The catalyst can give full play to the hydrolysis effect of each titanium active site on organic sulfur, and achieve a higher organic sulfur hydrolysis rate under the condition of low titanium content. However, it also does not involve the subsequent treatment of H2S generated after catalytic hydrolysis.

[0006] Chinese patent CN109382105B discloses a hydrogen sulfide selective oxidation catalyst and its preparation method. The carrier used can ensure that the catalyst has a suitable pore structure, avoid Claus reverse reaction when the catalyst is selectively oxidized, and reduce the sensitivity of the catalyst to water vapor and oxygen content; the catalyst has the characteristics of high activity, insensitivity to water vapor and oxygen content in the process gas, high lateral pressure strength, and high H2S conversion rate. However, it does not consider the treatment of organic sulfur and does not involve the issue of how COS is converted into H2S.

[0007] Perovskite oxides have good catalytic activity, thermal stability and structural tunability in catalysis. The arrangement of their metal ions and oxygen ions can be adjusted by doping and synthesis methods to optimize the catalytic performance. Perovskite oxides usually have certain basic sites, especially when doped with transition metals. These basic sites can be enhanced by adjusting the valence state and coordination environment of the metal, thereby improving the catalytic activity for certain reactions (such as organic reactions or CO2 hydrogenation). The hydrolysis reaction of organic sulfur is a typical base-catalyzed process, in which the basic sites are usually regarded as the active core of the hydrolysis reaction. In the selective oxidation process of hydrogen sulfide, metal oxide systems are currently the most commonly used catalyst systems in the industrial field. As the active center of the oxidation reaction, transition metal oxides have unique electronic structures and tunable redox properties. The d orbital electrons of these metals can participate in the redox reaction, allowing them to switch between different oxidation states, thereby effectively adsorbing reactants and accelerating the migration process of oxygen. In addition, the structure of metal oxides can be optimized by doping or changing the synthesis conditions to improve their catalytic performance and selectivity. Therefore, combining the excellent catalytic properties of perovskite-type oxides with the needs of organic sulfur hydrolysis and subsequent treatment of hydrogen sulfide, developing a one-step catalyst that can efficiently catalyze organic sulfur hydrolysis and synergistically achieve sulfur recovery is of great significance for solving the current technical problems of organic sulfur pollution control in industrial gases. Summary of the invention

[0008] In view of the shortcomings of the prior art, the purpose of the present invention is to provide an organic sulfur hydrolysis and synergistic sulfur recovery catalyst, which has the dual functions of organic sulfur hydrolysis and sulfur recovery (selective oxidation), can remove organic sulfur in the gas in one step, and achieve the purpose of energy conservation, emission reduction and coordinated control of multiple pollutants.

[0009] Another object of the present invention is to provide a preparation method and application of an organic sulfur hydrolysis synergistic sulfur recovery catalyst.

[0010] The technical solution adopted by the present invention is as follows:

[0011] The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst adopts a hydrothermal method and uses an alkali metal compound as a precipitant to synthesize a perovskite-type composite oxide catalyst, and comprises the following steps:

[0012] (1) Dissolve strontium salt in deionized water and stir evenly;

[0013] (2) adding a transition metal salt to step (1) and continuing stirring;

[0014] (3) slowly adding a titanium precursor to step (2) under vigorous stirring;

[0015] (4) adding an alkali metal compound to step (3) and continuing stirring;

[0016] (5) stirring the mixed solution obtained in step (4) at room temperature to ensure sufficient reaction, thereby obtaining reaction solution 1;

[0017] (6) transferring the reaction solution 1 to a hydrothermal reactor and heating the reaction to obtain a reaction solution 2;

[0018] (7) After the heating reaction is completed, the reaction solution 2 is first centrifuged; then, the separated precipitate is washed with deionized water and ethanol to effectively remove impurities therein; then, the washed precipitate is dried at a temperature range of 80-120°C for 8-24h to obtain the reactant 1; finally, the reactant 1 is placed in a muffle furnace, heated to 400-800°C at a heating rate of 5°C per minute, and calcined at this temperature for 4-8h to obtain an organic sulfur hydrolysis synergistic sulfur recovery catalyst, the general formula of which is SrTi 1-x M x O3, wherein x=0.05-0.2, and M is a transition metal element.

[0019] In the step (1), the strontium salt is nitrate or acetate.

[0020] In the step (2), the transition metal salt is a nitrate or an acetate; the transition metal in the transition metal salt is one or more of Mn, Fe, Ce, Co or Cu.

[0021] In the step (3), the titanium precursor is tetraisopropyl titanate or tetrabutyl titanate.

[0022] In the step (4), the alkali metal compound is one or more of sodium hydroxide, potassium hydroxide, sodium carbonate or potassium carbonate.

[0023] In the step (5), the stirring time is 0.5-3h.

[0024] In the step (6), the heating reaction temperature is 100-200°C and the time is 12-48h.

[0025] In the step (7), the centrifugal speed is 4000 rpm and the time is 10 min / time.

[0026] The organic sulfur hydrolysis synergistic sulfur recovery catalyst is prepared by the preparation method of the organic sulfur hydrolysis synergistic sulfur recovery catalyst.

[0027] The application of the organic sulfur hydrolysis synergistic sulfur recovery catalyst is used to catalyze the hydrolysis of organic sulfur, realize the synergistic operation of organic sulfur hydrolysis and H2S selective oxidation, and remove sulfur-containing components in the process gas in one step.

[0028] Compared with the prior art, the present invention has the following beneficial effects:

[0029] (1) The organic sulfur hydrolysis synergistic sulfur recovery catalyst of the present invention realizes the dual functional synergy of organic sulfur hydrolysis and sulfur recovery (i.e., selective oxidation), and can remove organic sulfur components in industrial gas in one step. The catalyst not only has adjustable composition and structure, strong variability, and rich surface acidity and alkalinity, but also exhibits excellent organic sulfur hydrolysis reaction activity and H2S selective oxidation activity. Moreover, through efficient synergistic action, it can remove sulfur-containing components in process gas in one step, greatly simplifying the complex operation of multiple steps and multiple equipment in traditional treatment processes, and significantly improving treatment efficiency and resource utilization;

[0030] (2) The preparation method of the organic sulfur hydrolysis synergistic sulfur recovery catalyst described in the present invention is scientific, reasonable, simple and easy to implement, and easy to scale up for industrial production. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] Figure 1 X-ray diffraction patterns of the catalysts prepared in Examples 1-5;

[0032] Figure 2 X-ray diffraction patterns of the catalysts prepared in Examples 1 and 6-9;

[0033] Figure 3 The activity diagram of the catalyst prepared in Examples 1-9 in the COS catalytic hydrolysis reaction;

[0034] Figure 4 The selective oxidation activity diagram of H2S for the catalysts prepared in Examples 1-9;

[0035] Figure 5 The SO2 yield graph of the catalyst prepared in Examples 1-9 in the COS catalytic hydrolysis reaction;

[0036] Figure 6 This is a graph showing the S yield of the catalysts prepared in Examples 1-9 in the COS catalytic hydrolysis reaction. DETAILED DESCRIPTION

[0037] The present invention is further described below with reference to the embodiments, but they do not limit the implementation of the present invention.

[0038] The raw materials used in the examples and comparative examples are conventional commercially available raw materials unless otherwise specified, and the process methods used in the examples and comparative examples are conventional methods in the art unless otherwise specified.

[0039] Some of the raw materials used in the examples and comparative examples are described as follows:

[0040] Example 1

[0041] The SrTi 0.9 Mn 0.1 The preparation method of O3 comprises the following steps:

[0042] (1) Dissolve 4.232 g of strontium nitrate in 100 mL of deionized water and stir thoroughly;

[0043] (2) adding 0.465 mL of 50% manganese nitrate solution to step (1) and continuing stirring;

[0044] (3) Slowly add 5.32 mL of tetraisopropyl titanate to step (2) under vigorous stirring;

[0045] (4) Add 2.4 g of sodium hydroxide to step (3) and continue stirring;

[0046] (5) stirring the mixed solution obtained in step (4) at room temperature for 1 h to ensure sufficient reaction, thereby obtaining reaction solution 1;

[0047] (6) The reaction solution 1 was transferred to a 180 mL hydrothermal reactor and heated at 200 °C for 24 h to obtain a reaction solution 2;

[0048] (7) After the heating reaction is completed, the reaction solution 2 is first centrifuged at 4000 rpm for 10 min to separate the solid precipitate; then, the separated precipitate is washed with deionized water and ethanol to effectively remove impurities therein; then, the washed precipitate is dried at 120°C for 12 h to obtain the reactant 1; finally, the reactant 1 is placed in a muffle furnace, heated to 500°C at a heating rate of 5°C per minute, and calcined at this temperature for 4 h to obtain SrTi 0.9 Mn 0.1 O3, recorded as ST-Mn0.1.

[0049] Example 2

[0050] The difference from Example 1 is that the prepared organic sulfur hydrolysis synergistic sulfur recovery catalyst is SrTi 0.9 Fe 0.1 O3, in step (2) of the preparation method, the transition metal salt added is 0.808 g of ferric nitrate nonahydrate, and the prepared SrTi 0.9 Fe 0.1 O3 is denoted as ST-Fe0.1, and the rest is the same as in Example 1.

[0051] Example 3

[0052] The difference from Example 1 is that the prepared organic sulfur hydrolysis synergistic sulfur recovery catalyst is SrTi 0.9 Ce 0.1 O3, in step (2) of the preparation method, the transition metal salt added is 0.868 g of cerium nitrate hexahydrate, and the prepared SrTi 0.9 Ce 0.1 O3 is denoted as ST-Ce0.1, and the rest is the same as in Example 1.

[0053] Example 4

[0054] The difference from Example 1 is that the prepared organic sulfur hydrolysis synergistic sulfur recovery catalyst is SrTi 0.9 Co 0.1 O3, in step (2) of the preparation method, the transition metal salt added is 0.582 g of cobalt nitrate hexahydrate, and the prepared SrTi 0.9 Co 0.1 O3 is denoted as ST-Co0.1, and the rest is the same as in Example 1.

[0055] Example 5

[0056] The difference from Example 1 is that the prepared organic sulfur hydrolysis synergistic sulfur recovery catalyst is SrTi 0.9 Cu 0.1O3, in step (2) of the preparation method, the transition metal salt added is 0.483 g of copper nitrate trihydrate, and the prepared SrTi 0.9 Cu 0.1 O3 is denoted as ST-Cu0.1, and the rest is the same as in Example 1.

[0057] Example 6

[0058] The difference from Example 1 is that the prepared organic sulfur hydrolysis synergistic sulfur recovery catalyst is SrTi 0.95 Mn 0.05 O3, in step (2) of the preparation method thereof, the transition metal salt added is 0.233 mL of 50% manganese nitrate solution, and the prepared SrTi 0.95 Mn 0.05 O3 is denoted as ST-Mn0.05, and the rest is the same as in Example 1.

[0059] Example 7

[0060] The difference from Example 1 is that the prepared organic sulfur hydrolysis synergistic sulfur recovery catalyst is SrTi 0.8 Mn 0.2 O3, in step (2) of the preparation method, the transition metal salt added is 0.930 mL of 50% manganese nitrate solution, and the prepared SrTi 0.8 Mn 0.2 O3 is denoted as ST-Mn0.2, and the rest is the same as in Example 1.

[0061] Example 8

[0062] The SrTi 0.9 Mn 0.1 The preparation method of O3-400 comprises the following steps:

[0063] (1) Dissolve 2.056 g of strontium acetate in 100 mL of deionized water and stir thoroughly;

[0064] (2) adding 0.233 mL of 50% manganese nitrate solution to step (1) and continuing stirring;

[0065] (3) Slowly add 3.015 mL of tetrabutyl titanate to step (2) under vigorous stirring;

[0066] (4) Add 2.805 g potassium hydroxide and 0.69 g potassium carbonate to step (3) and continue stirring;

[0067] (5) stirring the mixed solution obtained in step (4) at room temperature for 0.5 h to ensure sufficient reaction, thereby obtaining reaction solution 1;

[0068] (6) The reaction solution 1 was transferred to a 180 mL hydrothermal reactor and heated at 100 °C for 12 h to obtain a reaction solution 2;

[0069] (7) After the heating reaction is completed, the reaction solution 2 is first centrifuged at 4000 rpm for 10 min to separate the solid precipitate; then, the separated precipitate is washed with deionized water and ethanol to effectively remove impurities therein; then, the washed precipitate is dried at 80°C for 8 h to obtain the reactant 1; finally, the reactant 1 is placed in a muffle furnace, heated to 400°C at a heating rate of 5°C per minute, and calcined at this temperature for 4 h to obtain SrTi 0.9 Mn 0.1 O3-400, recorded as ST-Mn-400.

[0070] Example 9

[0071] The SrTi 0.9 Mn 0.1 The preparation method of O3-800 comprises the following steps:

[0072] (1) Dissolve 2.056 g of strontium acetate in 100 mL of deionized water and stir thoroughly;

[0073] (2) adding 0.233 mL of 50% manganese nitrate solution to step (1) and continuing stirring;

[0074] (3) Slowly add 3.015 mL of tetrabutyl titanate to step (2) under vigorous stirring;

[0075] (4) Add 2 g of sodium hydroxide and 0.53 g of sodium carbonate to step (3) and continue stirring;

[0076] (5) stirring the mixed solution obtained in step (4) at room temperature for 3 h to ensure sufficient reaction, thereby obtaining reaction solution 1;

[0077] (6) The reaction solution 1 was transferred to a 180 mL hydrothermal reactor and heated at 200 °C for 48 h to obtain a reaction solution 2;

[0078] (7) After the heating reaction is completed, the reaction solution 2 is first centrifuged at 4000 rpm for 10 min to separate the solid precipitate; then, the separated precipitate is washed with deionized water and ethanol to effectively remove impurities therein; then, the washed precipitate is dried at 120°C for 24 h to obtain the reactant 1; finally, the reactant 1 is placed in a muffle furnace, heated to 800°C at a heating rate of 5°C per minute, and calcined at this temperature for 8 h to obtain SrTi 0.9 Mn 0.1O3-800, recorded as ST-Mn-800.

[0079] The X-ray diffraction patterns of the catalysts prepared in Examples 1-9 were tested using an X-ray diffractometer. The test results are as follows: Figure 1-2 As shown. Figure 1-2 It can be seen that the catalysts prepared in Examples 1-9 all have a perovskite structure, and all samples have typical perovskite structural characteristic diffraction peaks (JCPDS No. 74-1296).

[0080] The catalysts prepared in Examples 1-9 were respectively ground, tableted, and sieved, and the 50±10 mesh portion was taken to evaluate the activity of the catalyst in an organic sulfur hydrolysis and coordinated sulfur recovery evaluation device. Among them, the quartz fixed bed reaction tube has an outer diameter of 10 mm and an inner diameter of 6 mm. The reactor adopts electric heating and two-stage heating. The total length of the heating section is 350 mm, and the catalyst loading is 0.25 mL. The raw gas is mixed and then fed into the reactor for reaction. The gas composition and concentration after the reaction are analyzed using a gas chromatograph with a thermal conductivity detector (TCD) and a flame photometer detector (FPD+). The catalyst evaluation conditions are: raw gas composition (volume): 1000 ppm COS, 1000 ppm H2O, 1000 ppm O2, and the rest is N2. The gas volume space velocity is 6000h -1 The bed temperature is 100℃, 200℃ and 300℃ respectively. Each temperature point is maintained for 3h. The average value of the data in the last 1h is taken as the activity data of the temperature point. In this reaction, the activity of the catalyst in the COS catalytic hydrolysis reaction is expressed by the COS conversion rate, the catalyst's selective oxidation activity for H2S is expressed by the H2S conversion rate, the degree of side reactions is expressed by the SO2 yield, and the total activity of the organic sulfur hydrolysis and sulfur recovery reaction is expressed by the S yield. The calculation methods are as follows:

[0081] COS conversion rate (%) = (COS concentration in inlet gas - COS concentration in outlet gas) / COS concentration in inlet gas × 100%;

[0082] H2S conversion rate (%) = (COS concentration in inlet gas - COS concentration in outlet gas - H2S concentration in outlet gas) / (COS concentration in inlet gas - COS concentration in outlet gas) × 100%;

[0083] SO2 yield (%) = SO2 concentration in outlet gas / COS concentration in inlet gas × 100%;

[0084] S yield (%) = (COS concentration in intake air - COS concentration in outlet air - H2S concentration in outlet air - SO2 concentration in outlet air) / COS concentration in intake air × 100%.

[0085] The evaluation results are shown in Tables 1-9 and Figure 3-6 shown.

[0086] Table 1 ST-Mn0.1 evaluation results

[0087]

[0088] Table 2 ST-Fe0.1 evaluation results

[0089]

[0090] Table 3 ST-Ce0.1 evaluation results

[0091]

[0092] Table 4 ST-Co0.1 evaluation results

[0093]

[0094] Table 5 ST-Cu0.1 evaluation results

[0095]

[0096] Table 6 Evaluation results of ST-Mn0.05

[0097]

[0098] Table 7 ST-Mn0.2 evaluation results

[0099]

[0100]

[0101] Table 8 Evaluation results of ST-Mn-400

[0102]

[0103] Table 9 Evaluation results of ST-Mn-800

[0104]

[0105] From Table 1-9 and Figure 3-6It can be seen that at 300°C, the COS conversion rate of Examples 1-5 all reached 100%, the H2S conversion rate reached more than 88.5%, and the final total sulfur yield was higher than 88.5%, and except for Example 2, no by-product SO2 was produced. Comparison of Examples 1, 6, and 7 shows that the manganese content has a more obvious effect on the catalyst performance, and a moderate manganese content is conducive to the reaction. Comparison of Examples 1, 8, and 9 shows that the catalysts have organic sulfur hydrolysis and synergistic sulfur recovery catalytic performance within a wider range of synthesis conditions. This shows that the catalyst prepared by the present invention has excellent organic sulfur hydrolysis reaction activity and synergistic H2S selective oxidation activity, and can achieve efficient synergistic organic sulfur hydrolysis and H2S selective oxidation, and remove sulfur-containing components in the process gas in one step.

Claims

1. A method for preparing an organic sulfur hydrolysis synergistic sulfur recovery catalyst, characterized in that: The following steps are involved: (1) Dissolve strontium salt in deionized water and stir evenly; (2) adding a transition metal salt to step (1) and continuing stirring; (3) adding a titanium precursor to step (2) under stirring; (4) adding an alkali metal compound to step (3) and continuing stirring; (5) stirring the mixed solution obtained in step (4) at room temperature to obtain reaction solution 1; (6) transferring the reaction solution 1 to a hydrothermal reactor and heating the reaction to obtain a reaction solution 2; (7) After the heating reaction is completed, the reaction solution 2 is centrifuged, washed, dried, and calcined in sequence to obtain an organic sulfur hydrolysis synergistic sulfur recovery catalyst, the general formula of which is SrTi 1-x M x O3, wherein x=0.05-0.2, and M is a transition metal element.

2. The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 1, characterized in that: In the step (1), the strontium salt is nitrate or acetate.

3. The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 1, characterized in that: In the step (2), the transition metal salt is a nitrate or an acetate; the transition metal in the transition metal salt is one or more of Mn, Fe, Ce, Co or Cu.

4. The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 1, characterized in that: In the step (3), the titanium precursor is tetraisopropyl titanate or tetrabutyl titanate.

5. The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 1, characterized in that: In the step (4), the alkali metal compound is one or more of sodium hydroxide, potassium hydroxide, sodium carbonate or potassium carbonate.

6. The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 1, characterized in that: In the step (5), the stirring time is 0.5-3h.

7. The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 1, characterized in that: In the step (6), the heating reaction temperature is 100-200°C and the time is 12-48h.

8. The method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 1, characterized in that: In the step (7), the calcination temperature is 400-800°C and the calcination time is 4-8h.

9. An organic sulfur hydrolysis synergistic sulfur recovery catalyst, characterized in that: The catalyst is prepared by the method for preparing the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to any one of claims 1 to 8.

10. An application of the organic sulfur hydrolysis synergistic sulfur recovery catalyst according to claim 9, characterized in that: It is used to catalyze the hydrolysis of organic sulfur, realize the coordinated hydrolysis of organic sulfur and the selective oxidation of H2S, and remove the sulfur-containing components in the process gas in one step.

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