CN110127602B - Method for decomposing hydrogen sulfide by using catalyst - Google Patents
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- CN110127602B CN110127602B CN201810136034.1A CN201810136034A CN110127602B CN 110127602 B CN110127602 B CN 110127602B CN 201810136034 A CN201810136034 A CN 201810136034A CN 110127602 B CN110127602 B CN 110127602B
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- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0495—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by dissociation of hydrogen sulfide into the elements
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/04—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of inorganic compounds, e.g. ammonia
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Abstract
The invention relates to the field of hydrogen sulfide decomposition, and discloses a method for decomposing hydrogen sulfide by using a catalyst, which comprises the following steps: introducing a feed gas containing hydrogen sulfide into a low-temperature plasma reactor and contacting the feed gas with a decomposition catalyst in the low-temperature plasma reactor under a dielectric barrier discharge condition to perform a decomposition reaction, the decomposition catalyst containing a carrier, an active metal component supported on the carrier, and an auxiliary agent, and the auxiliary agent being at least one element selected from the group consisting of K, Na, N, and P; based on the total weight of the decomposition catalyst, the content of the carrier is 40-90 wt%, the content of the active metal component is 1-50 wt% calculated by oxide, and the content of the auxiliary agent is 0.01-10 wt% calculated by oxide. Compared with the method provided by the prior art, the method for improving the hydrogen sulfide conversion rate has higher hydrogen sulfide conversion rate.
Description
Technical Field
The invention relates to the field of hydrogen sulfide decomposition, in particular to a method for decomposing hydrogen sulfide by using a catalyst.
Background
Hydrogen sulfide (H)2S) is a highly toxic and malodorous acidic gas, which not only can cause corrosion of materials such as metal, but also can easily cause catalyst poisoning and inactivation in chemical production; in addition, hydrogen sulfide can also harm human health and cause environmental pollution. Therefore, in the case of performing a detoxification treatment of a large amount of hydrogen sulfide gas generated in industrial fields such as petroleum, natural gas, coal, and mineral processing, a solution is urgently needed in view of process requirements, equipment maintenance, environmental requirements, and the like.
Currently, the hydrogen sulfide is treated by the Claus process, which partially oxidizes hydrogen sulfide to produce sulfur and water. Although the method solves the problem of harmlessness of hydrogen sulfide, a large amount of hydrogen resources are lost.
With the increase of the processing amount of high-sulfur crude oil in China, the amount of the hydrogen sulfide-containing acidic tail gas which is a byproduct of an oil refining hydrofining unit is increased year by year, and the amount of hydrogen required by hydrofining is increased; in addition, hydrogen is used as a main raw material in chemical process such as oil hydrocracking, low-carbon alcohol synthesis, synthetic ammonia and the like, and the demand amount is also considerable. Therefore, the direct decomposition of the hydrogen sulfide is an ideal hydrogen sulfide resource utilization technical route, the hydrogen sulfide is harmless, the hydrogen and the elemental sulfur can be produced, the cyclic utilization of the hydrogen resource in the petroleum processing process can be realized, and the emission of a large amount of carbon dioxide brought by the conventional hydrocarbon reforming hydrogen production can be reduced.
At present, the hydrogen sulfide decomposition method mainly comprises the following steps: high temperature decomposition, electrochemical, photocatalytic, and low temperature plasma methods. Among the aforementioned methods, the pyrolysis method is relatively mature in industrial technology, but the thermal decomposition of hydrogen sulfide strongly depends on the reaction temperature and is limited by the thermodynamic equilibrium, and the conversion rate of hydrogen sulfide is only 20% even if the reaction temperature is 1000 ℃ or higher. In addition, the high temperature conditions place high demands on reactor materials, which also increases operating costs. In addition, since the thermal decomposition conversion of hydrogen sulfide is low, a large amount of hydrogen sulfide gas needs to be separated from the tail gas and circulated in the system, thereby reducing the efficiency of the apparatus and increasing the energy consumption, which all bring difficulties to large-scale industrial application thereof. Although the adoption of the membrane technology can effectively separate products, thereby breaking balance limitation and improving the conversion rate of hydrogen sulfide, the thermal decomposition temperature often exceeds the limit heat-resistant temperature of the membrane, so that the structure of the membrane material is damaged. The electrochemical method has the defects of multiple operation steps, serious equipment corrosion, poor reaction stability, low efficiency and the like. The photocatalytic method for decomposing hydrogen sulfide mainly refers to the research of photocatalytic water decomposition, and the research focuses on the aspects of developing high-efficiency semiconductor photocatalysts and the like. The method for decomposing the hydrogen sulfide by utilizing the solar energy has the advantages of low energy consumption, mild reaction conditions, simple operation and the like, and is a relatively economic method. However, this method has problems such as a small treatment amount, low catalytic efficiency, and easy deactivation of the catalyst.
Compared with other decomposition methods, the low-temperature plasma method has the advantages of simple operation, small device volume, high energy efficiency and the like, and the involved reaction has high controllability and can be flexibly applied under the conditions of small treatment capacity and difficult centralized treatment. In addition, the hydrogen sulfide decomposition device has the characteristics of high energy density and shortened reaction time, can realize effective decomposition of hydrogen sulfide at a lower temperature, and is suitable for occasions with different scales, dispersed layouts and variable production conditions. Besides, the low-temperature plasma method recovers hydrogen resources while recovering sulfur, and can realize resource utilization of hydrogen sulfide.
CN102408095A uses medium to block discharge and light catalyst to decompose hydrogen sulfide, and its method is to pack solid catalyst with light catalytic activity in plasma zone, however, this method has the disadvantage that sulfur produced by hydrogen sulfide decomposition will deposit under catalyst bed.
CN103495427A discloses a method for preparing a supported metal sulfide catalyst by using low-temperature plasma, which is characterized in that hydrogen sulfide gas or gas containing hydrogen sulfide is ionized by gas discharge to form uniformly distributed low-temperature plasma, and the low-temperature plasma is directly interacted with a supported metal salt precursor to generate metal sulfide. Because the catalyst is prevented from being exposed to overhigh temperature, the prepared catalyst does not have the phenomenon of thermal agglomeration, thereby having smaller particle size and higher dispersity. However, this prior art provides a catalyst which, when used in the decomposition reaction of hydrogen sulfide, does not have a high conversion of hydrogen sulfide.
Disclosure of Invention
The invention aims to overcome the defect of low hydrogen sulfide conversion rate of a catalyst for catalyzing hydrogen sulfide to decompose and generate elemental sulfur and hydrogen in the prior art, and provides a novel method for decomposing hydrogen sulfide by using the catalyst.
The inventors of the present invention have found in their studies that a catalyst containing an auxiliary component of at least one element selected from the group consisting of K, Na, N and P, when used as a decomposition catalyst for decomposing hydrogen sulfide in a low-temperature plasma reactor for dielectric barrier discharge, enables the conversion rate of hydrogen sulfide to be significantly improved relative to the prior art. Accordingly, the present inventors have completed the technical solution of the present invention.
In order to achieve the above object, the present invention provides a method for decomposing hydrogen sulfide using a catalyst, the method comprising: introducing a feed gas containing hydrogen sulfide into a low-temperature plasma reactor, and contacting the feed gas with a decomposition catalyst in the low-temperature plasma reactor under a dielectric barrier discharge condition to perform decomposition reaction, wherein the decomposition catalyst contains a carrier, an active metal component and an auxiliary agent, the active metal component is supported on the carrier, the carrier is at least one of molecular sieves, alumina and silica, the active metal component is at least one of metal elements selected from IB group, IIB group, IVB group, VB group, VIB group, VIIB group and VIII group, and the auxiliary agent is at least one element selected from K, Na, N and P; based on the total weight of the decomposition catalyst, the content of the carrier is 40-90 wt%, the content of the active metal component is 1-50 wt% calculated by oxide, and the content of the auxiliary agent is 0.01-10 wt% calculated by oxide.
Compared with the method provided by the prior art, the method for improving the hydrogen sulfide conversion rate has higher hydrogen sulfide conversion rate; in particular, the present invention provides processes which enable the conversion of hydrogen sulphide to be maintained at a stable high level over a relatively long period of time.
In addition, the method provided by the invention has the advantages of simple operation and low cost.
Drawings
Fig. 1 is a schematic structural view of a low-temperature plasma reactor used in an embodiment of the present invention.
Description of the reference numerals
1. Inner cylinder 2, outer cylinder
11. Reactor inlet 21, heat transfer medium inlet
12. Gas product outlet 22 and heat-conducting medium outlet
13. Liquid product outlet
3. Center electrode
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
As previously described, the present invention provides a method for decomposing hydrogen sulfide using a catalyst, the method comprising: introducing a feed gas containing hydrogen sulfide into a low-temperature plasma reactor, and contacting the feed gas with a decomposition catalyst in the low-temperature plasma reactor under a dielectric barrier discharge condition to perform decomposition reaction, wherein the decomposition catalyst contains a carrier, an active metal component and an auxiliary agent, the active metal component is supported on the carrier, the carrier is at least one of molecular sieves, alumina and silica, the active metal component is at least one of metal elements selected from IB group, IIB group, IVB group, VB group, VIB group, VIIB group and VIII group, and the auxiliary agent is at least one element selected from K, Na, N and P; based on the total weight of the decomposition catalyst, the content of the carrier is 40-90 wt%, the content of the active metal component is 1-50 wt% calculated by oxide, and the content of the auxiliary agent is 0.01-10 wt% calculated by oxide.
In order to further increase the conversion rate of hydrogen sulfide, it is preferable that the carrier is contained in an amount of 62 to 85 wt%, the active metal component is contained in an amount of 7 to 30 wt% in terms of an oxide, and the auxiliary is contained in an amount of 0.1 to 8 wt% in terms of an oxide, based on the total weight of the decomposition catalyst.
Particularly preferably, in the decomposition catalyst, the auxiliary is K and/or Na. The inventors have found that the use of K and/or Na as an auxiliary in the decomposition catalyst of the process of the invention enables the process of the invention to achieve significantly higher hydrogen sulphide conversion.
According to a preferred embodiment, in the decomposition catalyst, the support contains a molecular sieve as component a and alumina and/or silica as component B.
Preferably, in the decomposition catalyst, the content weight ratio of the component a and the component B is preferably 1: (0.01 to 1.2); preferably 1: (0.02-1); more preferably 1: (0.05-0.95); more preferably 1: (0.1-0.8).
In the method of the present invention, when the decomposition catalyst contained in the low-temperature plasma reactor contains an auxiliary agent, and the carrier in the decomposition catalyst contains a molecular sieve as component a and alumina and/or silica as component B, and the content weight ratio of component a and component B is within the above-described preferred range of the present invention, under the dielectric barrier discharge condition, the method of the present invention can achieve a higher hydrogen sulfide conversion rate with relatively lower energy consumption.
Preferably, in the decomposition catalyst, the molecular sieve is selected from at least one of a medium pore molecular sieve and a large pore molecular sieve.
Preferably, the average pore size of the mesoporous molecular sieve is greater than or equal to 0.3nm and less than 0.6 nm; the average pore diameter of the large pore molecular sieve is 0.6-1.0 nm.
Preferably, the mesoporous molecular sieve is selected from at least one of ZSM-35, ZSM-48, ZSM-5, ZSM-11, ZSM-22, ZSM-23, ZSM-12, ZSM-57, and SAPO-11.
Preferably, the large pore molecular sieve is selected from at least one of ZSM-20, SAPO-5, USY, ZSM-3, SAPO-37, beta, MCM-68, and mordenite.
According to a preferred embodiment, in the decomposition catalyst, the molecular sieve is a mixture of a medium pore molecular sieve and a large pore molecular sieve.
Preferably, in the decomposition catalyst, the content weight ratio of the medium pore molecular sieve to the large pore molecular sieve is 1: (0.05-0.85); more preferably 1: (0.1 to 0.8); more preferably 1: (0.25-0.55).
The inventors of the present invention have found that when the decomposition catalyst contains both the medium-pore molecular sieve and the large-pore molecular sieve in a weight ratio within the aforementioned preferable range of the present invention, the conversion rate of hydrogen sulfide can be significantly increased and the conversion rate of hydrogen sulfide can be stably maintained at a high level when the decomposition catalyst is applied to catalyze the decomposition reaction of hydrogen sulfide in a low-temperature plasma reactor.
Preferably, in the decomposition catalyst, the active metal component is at least one metal element selected from Cu, Ag, Zn, Cd, Ti, Zr, V, Cr, Mo, W, Mn, Fe, Co, Ni, Pd and Pt; more preferably, the active metal component is at least one metal element selected from the group consisting of Ti, Zr, Mo, W, Mn, Co, Ni and Cr.
According to a preferred embodiment, in the decomposition catalyst, the active metal component is a mixture containing a first metal element and a second metal element, the first metal element being Ti and/or Zr, and the second metal element being Co and/or Ni.
Preferably, the content weight ratio of the first metal element to the second metal element is 1: (0.5-2).
In the decomposition catalyst of the present invention, the active metal component may be present in the form of a metal oxide, a metal salt or a metal sulfide, and preferably the active metal component is present in the form of a metal oxide or a metal sulfide.
The method of the present invention is not particularly limited as to the method for preparing the decomposition catalyst, and the preparation can be carried out by a catalyst preparation method which is conventional in the art as long as the decomposition catalyst having the aforementioned characteristics of the present invention can be obtained.
Preferably, the decomposition catalyst of the present invention is in the form of microspheres, and the average particle diameter of the decomposition catalyst is 0.1 to 50 mm.
Preferably, the discharge conditions include: the discharge voltage is 5-30 kV, the discharge frequency is 200-30000 Hz, and the discharge current is 0.1-100A.
Preferably, the conditions of the decomposition reaction include: the reaction temperature is 0-800 ℃, the preferable reaction temperature is 0-200 ℃, the reaction pressure is-0.06 MPa-0.6 MPa, and reactants are reacted in the low-temperature plasmaResidence time in reactor 1 × 10-5～120s。
The method provided by the present invention has no particular limitation on the structure of the low-temperature plasma reactor, and the specific example section of the present invention provides only one specific structure of the low-temperature plasma reactor for illustrating the effect of the provided method, and those skilled in the art should not be construed as limiting the present invention.
The present invention will be described in detail below by way of examples. In the following examples, various raw materials used were commercially available unless otherwise specified.
The decomposition catalysts used in the following examples were prepared as follows: the carrier is mixed with a binder optionally contained, then extruded and molded on a bar extruder, and then dried at 120 ℃ for 2 hours, and then calcined at 300 ℃ for 6 hours to obtain the catalyst carrier.
100g of the carrier was mixed with a metal salt solution containing an element of an active metal component and a salt solution containing an auxiliary element to carry out impregnation treatment, followed by drying at 120 ℃ for 2 hours and then calcining at 320 ℃ for 5 hours, to obtain the corresponding catalyst.
The catalyst prepared by the method comprises the following components:
cat 1: based on the total weight of the decomposition catalyst, the content of active metal components (Ti and Co, and the weight ratio of Ti to Co elements is 1: 1) in terms of oxide is 16.8 wt%, the content of gamma-alumina is 26.9 wt%, and K is2The content of O is 3.2 weight percent, the content of ZSM-23 molecular sieve is 34.6 weight percent, and the balance is β molecular sieve.
Cat 2: the content of active metal components (Zr and Ni, and the weight ratio of Zr to Ni elements is 1: 0.65) in terms of oxide was 25.9 wt%, the content of silica was 27.6 wt%, and K was calculated on the total weight of the decomposition catalyst2The content of O is 5.6 weight percent, the content of ZSM-35 molecular sieve is 27.6 weight percent, and the balance is ZSM-3 molecular sieve.
Cat 3: the content of active metal components (Ti and Ni, and the weight ratio of Ti to Ni elements is 1: 1.65) in terms of oxide was 13.2 wt%, based on the total weight of the decomposition catalyst, and gamma-alumina was usedIs 14.5 wt% Na2The content of O is 1.8 weight percent, the content of ZSM-11 molecular sieve is 52.6 weight percent, and the balance is SAPO-37 molecular sieve.
Cat 4: based on the total weight of the decomposition catalyst, the content of active metal components (Ti and Co, and the weight ratio of Ti to Co elements is 1: 1) in terms of oxide is 16.6 wt%, the content of gamma-alumina is 24.6 wt%, and K is2The content of O is 9.3 wt%, the content of ZSM-23 molecular sieve is 30.2 wt%, and the rest is β molecular sieve.
Cat 5: the content of active metal components (Zr and Ni, and the weight ratio of Zr to Ni elements is 1: 0.65) in terms of oxide was 26.2 wt%, the content of silica was 26.9 wt%, and P was 26.9 wt%, based on the total weight of the decomposition catalyst2O5The content of (A) is 5.8 wt%, the content of ZSM-35 molecular sieve is 28.3 wt%, and the rest is ZSM-3 molecular sieve.
Cat 6: the content of active metal components (Ti and Ni, and the weight ratio of Ti to Ni elements is 1: 1.65) in terms of oxide was 13.2 wt%, and Na was contained in terms of the total weight of the decomposition catalyst2The content of O is 1.9 weight percent, the content of ZSM-11 molecular sieve is 67.1 weight percent, and the balance is SAPO-37 molecular sieve.
Cat 7: based on the total weight of the decomposition catalyst, the content of active metal components (Ti and Co, and the weight ratio of Ti to Co elements is 1: 1) in terms of oxide is 16.5 wt%, the content of gamma-alumina is 27.3 wt%, and K is2The content of O is 3.4 weight percent, and the balance is ZSM-23 molecular sieve.
D-Cat 1: the content of active metal components (Ti and Co, with a Ti to Co element weight ratio of 1: 1) in terms of oxide was 16.7 wt%, and the balance was γ -alumina, based on the total weight of the decomposition catalyst.
D-Cat 2: based on the total weight of the decomposition catalyst, the content of active metal components (Ti and Co, and the weight ratio of Ti to Co elements is 1: 1) in terms of oxide is 16.9 wt%, the content of ZSM-23 molecular sieve is 53.6 wt%, and the balance is beta molecular sieve.
D-Cat 3: based on the total weight of the decomposition catalyst, the content of active metal components (Zr and Ni, and the weight ratio of Zr to Ni elements is 1: 0.65) calculated by oxide is 26.3 wt%, the content of silicon oxide is 28.0 wt%, the content of ZSM-35 molecular sieve is 14.2 wt%, and the balance is ZSM-3 molecular sieve.
Example 1
Example a decomposition reaction of hydrogen sulfide was performed using a low-temperature plasma reactor shown in fig. 1, specifically, the structure of the low-temperature plasma reactor shown in fig. 1 was:
the reactor comprises:
the device comprises an inner cylinder 1, wherein the inner cylinder is provided with a reactor inlet 11, a gas product outlet 12 and a liquid product outlet 13, all side walls of the inner cylinder are formed by blocking media, the material forming the blocking media is hard glass, 200mL of catalyst is filled in the inner cylinder of the reactor in each test, and the filling types of the catalyst are shown in Table 1;
the outer cylinder 2 is nested outside the inner cylinder, and a heat-conducting medium inlet 21 and a heat-conducting medium outlet 22 are respectively arranged on the outer cylinder;
the central electrode 3 is arranged at the central axis position of the inner cylinder, and the material forming the central electrode is a stainless steel metal rod;
a space between the inner wall of the outer cylinder and the outer wall of the inner cylinder is filled with a heat-conducting medium (specifically, a 15 wt% NaCl aqueous solution), and the heat-conducting medium also serves as a liquid grounding electrode;
a distance L between the outer side wall of the central electrode and the inner side wall of the blocking medium1And thickness D of barrier medium1The ratio of (A) to (B) is 6: 1;
the position of the gas product outlet is relative to the height H of the bottom of the inner cylinder1And the length L of the discharge region containing the barrier medium2The proportion relation between the components is as follows: h1：L2＝1：30；
The volume of the inner cylinder of the reactor in this example was 500 mL.
Gas containing hydrogen sulfide enters the inner cylinder of the reactor from the upper part of the inner cylinder of the reactor, a gas product is led out from a gas product outlet positioned at the lower part of the inner cylinder of the reactor, and elemental sulfur is led out from a liquid product outlet positioned at the bottom of the reactor; and the heat-conducting medium is introduced from the lower part of the outer barrel of the reactor and is led out from the upper part of the outer barrel of the reactor.
The operation steps of the low-temperature plasma reactor are as follows:
nitrogen gas is introduced into the inner cylinder of the low-temperature plasma reactor from the reactor inlet to purge the discharge region of air, and the gas is withdrawn from the gaseous product outlet and the liquid product outlet. Meanwhile, heat-conducting medium is led into the outer cylinder from the heat-conducting medium inlet, the led-in heat-conducting medium is led out from the heat-conducting medium outlet, and the temperature of the heat-conducting medium is kept at 40 ℃.
Then introducing H into the inner cylinder of the low-temperature plasma reactor from the inlet of the reactor2S/Ar mixed gas, in which H2The volume fraction of S is 30%, the flow rate of the mixed gas is controlled so that the average residence time of the gas in the discharge area is 17.6S, and the reaction pressure is 0.02 MPa. H2And (3) introducing the S/Ar mixed gas into the reactor for 30min, switching on an alternating-current high-voltage power supply, and adjusting the voltage and the frequency to form a plasma discharge field between the central electrode and the liquid grounding electrode.
Wherein the discharge conditions are as follows: the voltage was 17.2kV, the frequency was 7.8kHz, and the current was 0.75A. The hydrogen sulfide gas is ionized in the discharge area and decomposed into hydrogen and elemental sulfur, and the elemental sulfur generated by discharge slowly flows down along the inner cylinder wall and flows out from the liquid product outlet. The gas flows out from the gas product outlet after the reaction.
Test H was carried out for 10min, 20min and 60min after the decomposition reaction was continued2S conversion, the results are listed in table 1.
TABLE 1
Example 2
This example was carried out in a similar manner to example 1, except that the discharge conditions in this example were: the voltage was 18.5kV, the frequency was 8.0kHz, and the current was 0.75A.
And the conditions of the decomposition reaction are as follows: the reaction temperature was 60 ℃, the reaction pressure was 0.05MPa, and the average residence time of the reactants in the low temperature plasma reactor was 18.2 s.
The rest is the same as in example 1.
The results of this example are shown in Table 2.
TABLE 2
As can be seen from the results of tables 1 and 2, the process provided by the present invention allows for a significant increase in the conversion of hydrogen sulfide; in addition, the method provided by the invention can ensure that the conversion rate of the hydrogen sulfide in the decomposition reaction of the hydrogen sulfide is stably maintained at a higher level.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (19)
1. A method for decomposing hydrogen sulfide using a catalyst, the method comprising: introducing a feed gas containing hydrogen sulfide into a low-temperature plasma reactor, and contacting the feed gas with a decomposition catalyst in the low-temperature plasma reactor under a dielectric barrier discharge condition to perform decomposition reaction, wherein the decomposition catalyst contains a carrier, an active metal component and an auxiliary agent, the active metal component is supported on the carrier, the carrier is at least one of molecular sieves, alumina and silica, the active metal component is at least one of metal elements selected from IB group, IIB group, IVB group, VB group, VIB group, VIIB group and VIII group, and the auxiliary agent is at least one element selected from K, Na, N and P; based on the total weight of the decomposition catalyst, the content of the carrier is 40-90 wt%, the content of the active metal component is 1-50 wt% calculated by oxide, and the content of the auxiliary agent is 0.01-10 wt% calculated by oxide.
2. The method according to claim 1, wherein the carrier is contained in an amount of 62 to 85 wt%, the active metal component is contained in an amount of 7 to 30 wt% in terms of oxide, and the auxiliary is contained in an amount of 0.1 to 8 wt% in terms of oxide, based on the total weight of the decomposition catalyst.
3. The method of claim 1, wherein the adjuvant is K and/or Na.
4. A process according to any one of claims 1 to 3, wherein in the decomposition catalyst the support comprises molecular sieve as component a and alumina and/or silica as component B.
5. The method of claim 4, wherein the weight ratio of the component A to the component B is 1: (0.01-1.2).
6. The method of claim 4, wherein the weight ratio of the component A to the component B is 1: (0.05-0.95).
7. The method of claim 4, wherein the weight ratio of the component A to the component B is 1: (0.1-0.8).
8. The method of claim 4, wherein, in the decomposition catalyst, the molecular sieve is selected from at least one of a medium pore molecular sieve and a large pore molecular sieve.
9. The process of claim 8, wherein the average pore size of the mesoporous molecular sieve is from 0.3nm or more to less than 0.6 nm; the average pore diameter of the large pore molecular sieve is 0.6-1.0 nm.
10. The method of claim 8, wherein the mesoporous molecular sieve is selected from at least one of ZSM-35, ZSM-48, ZSM-5, ZSM-11, ZSM-22, ZSM-23, ZSM-12, ZSM-57, and SAPO-11;
the large pore molecular sieve is selected from at least one of ZSM-20, SAPO-5, USY, ZSM-3, SAPO-37, beta molecular sieve, MCM-68 and mordenite.
11. The process according to claim 4, wherein in the decomposition catalyst the molecular sieve is a mixture of a medium pore molecular sieve and a large pore molecular sieve.
12. The method of claim 11, wherein, in the decomposition catalyst, the content weight ratio of the medium pore molecular sieve and the large pore molecular sieve is 1: (0.05-0.85).
13. The method of claim 11, wherein, in the decomposition catalyst, the content weight ratio of the medium pore molecular sieve and the large pore molecular sieve is 1: (0.25-0.55).
14. The method according to any one of claims 1 to 3, wherein, in the decomposition catalyst, the active metal component is at least one metal element selected from Cu, Ag, Zn, Cd, Ti, Zr, V, Cr, Mo, W, Mn, Fe, Co, Ni, Pd and Pt.
15. The method according to any one of claims 1 to 3, wherein in the decomposition catalyst, the active metal component is at least one metal element selected from the group consisting of Ti, Zr, Mo, W, Mn, Co, Ni and Cr.
16. The method according to claim 14, wherein, in the decomposition catalyst, the active metal component is a mixture containing a first metal element and a second metal element, the first metal element being Ti and/or Zr, and the second metal element being Co and/or Ni.
17. The method of claim 16, wherein the content weight ratio of the first metal element to the second metal element is 1: (0.5-2).
18. The method of any of claims 1-3, wherein the discharge condition comprises: the discharge voltage is 5-30 kV, the discharge frequency is 200-30000 Hz, and the discharge current is 0.1-100A.
19. The method as claimed in any one of claims 1 to 3, wherein the decomposition reaction conditions include a reaction temperature of 0 to 800 ℃, a reaction pressure of-0.06 MPa to 0.6MPa, and a residence time of the reactants in the low-temperature plasma reactor of 1 × 10-5～120s。
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