Systems, methods and materials for hydrogen sulfide conversion

Abstract

Systems and methods use bimetallic alloy particles for converting hydrogen sulfide (H2S) to hydrogen (H2) and sulfur (S), typically during multiple operations. In a first operation, metal alloy composite particles can be converted to a composite metal sulfide. In a second operation, composite metal sulfide from the first operation can be regenerated back to the metal alloy composite particle using an inert gas stream. Pure, or substantially pure, sulfur can also be generated during the second operation.

Description

TECHNICAL FIELD

The present disclosure relates to systems and methods for converting hydrogen sulfide (H₂S) in a gas stream to hydrogen (H₂) and sulfur. More particularly, the present disclosure relates to bimetallic alloys usable in systems and methods for generating hydrogen (H₂) and sulfur streams from hydrogen sulfide (H₂S) streams.

BACKGROUND

Natural gas, petroleum and coal are primarily utilized as energy sources. However, sulfur compounds such as hydrogen sulfide (H₂S) within these fuels limit their use due to the toxic and corrosive nature of such compounds. For example, exposure to H₂S can be harmful for humans even at concentrations as low as 10 ppm. In addition, the applicability of these fuels as a feedstock for value-added chemicals is also limited due to catalyst deactivation as a result of sulfur poisoning.

Currently used processes for removing hydrogen sulfide (H₂S) are intensive and demand high energy. Additionally, currently used processes cannot recover H₂ along with sulfur because H₂ is lost in the form of water vapor. Furthermore, the performance of solids used in hydrogen sulfide (H₂S) processing can deteriorate after a single cycle. Such systems are inefficient and can require replenishing the solids after one or just a few cycles of sulfur capture and regeneration. Therefore, there is a need for an improved process to effectively convert hydrogen sulfide (H₂S) into hydrogen (H₂) and sulfur.

SUMMARY

Disclosed herein are systems and methods for converting hydrogen sulfide (H₂S) in a gas stream to hydrogen (H₂) and sulfur. In one aspect, a method utilizes metal alloy composite particles for converting hydrogen sulfide (H₂S) in a gas stream to hydrogen (H₂) and sulfur. The method is a two-step thermochemical decomposition of H₂S into H₂ and sulfur. The first step is referred to as the sulfidation operation, wherein H₂S reacts with the metal alloy composite particle to form a mixture of metal sulfides and produce H₂. The second step is referred to as the regeneration operation, wherein the mixture of metal sulfides is subjected to a high temperature and gas input stream to remove the captured sulfur and regenerate the metal alloy composite particle. Thereby, separate H₂ and sulfur streams are produced from an input stream including H₂S. Compared to the conventionally used Claus process for sulfur recovery, which only produces sulfur and no H₂, the disclosed method is economically favorable. It is also beneficial to the environment as it converts a toxic, poisonous, and corrosive H₂S gas to valuable chemicals H₂ and sulfur.

There is no specific requirement that a material, technique or method relating to H₂S conversion include all of the details characterized herein, in order to obtain some benefit according to the present disclosure. Thus, the specific examples characterized herein are meant to be exemplary applications of the techniques described, and alternatives are possible. Other aspects of the disclosure will become apparent by consideration of the detailed description and accompanying drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows a schematic diagram of an exemplary system for H₂S conversion to H₂ and S.

FIG. 2 shows a schematic diagram of another exemplary system for H₂S conversion to H₂ and S.

FIG. 3 shows a schematic diagram of another exemplary system for H₂S conversion to H₂ and S.

FIG. 4 shows an example method for H₂S conversion to H₂ and S.

FIG. 5 shows an example method for preparing a metal alloy composite particle for use in H₂S conversion to H₂ and S.

FIG. 6 shows the X-ray diffraction analysis of the iron-chromium metal alloy composite particle obtained after preparation in a fixed bed reactor.

FIG. 7 shows H₂S conversion for an iron-chromium alloy composite particle over five sulfidation-regeneration operations where the gas hourly space velocity for first two sulfidation operations was 5000 hr⁻¹ and for the last three was 2580 hr⁻¹.

FIG. 8 shows X-ray diffraction analysis of solids in a fixed bed reactor after five sulfidation-regeneration operations.

FIG. 9 shows the X-ray diffraction analysis of solids after run 1 in a fixed bed reactor.

FIG. 10 shows the X-ray diffraction analysis of solids after run 2 in the fixed bed reactor used to obtain data shown in FIG. 9.

FIG. 11 shows calculated thermodynamic values of H₂S fractional conversion as a function of iron monosulfide:chromium monosulfide molar ratio.

FIG. 12 shows calculated thermodynamic values for molar composition of iron monosulfide, chromium monosulfide and iron-chromium thiospinel as a function of iron monosulfide:chromium monosulfide molar ratio.

FIG. 13 shows the X-ray diffraction analysis of Fe—Cr alloy with MoS₂ secondary material after reaction with 0.9% H₂S at 800° C.

FIG. 14 shows the X-ray diffraction analysis of Fe—Cr alloy with MoS₂ secondary material and SiO₂ support material after reaction with 0.9% H₂S at 800° C.

FIG. 15 shows H₂S conversion over 12 consecutive sulfidation-regeneration cycles with Fe—Cr alloy containing 20 wt % MoS₂.

FIG. 16 shows H₂S conversion as a function of pressure at 400° C. as obtained by using FactSage 7.3 software.

DETAILED DESCRIPTION

I. Definitions

Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In case of conflict, the present document, including definitions, will control. Example methods and materials are described below, although methods and materials similar or equivalent to those described herein can be used in practice or testing of the present disclosure. The materials, methods, and examples disclosed herein are illustrative only and not intended to be limiting.

The terms “comprise(s),” “include(s),” “having,” “has,” “can,” “contain(s),” and variants thereof, as used herein, are intended to be open-ended transitional phrases, terms, or words that do not preclude the possibility of additional acts or structures. The singular forms “a,” “an” and “the” include plural references unless the context clearly dictates otherwise. The present disclosure also contemplates other embodiments “comprising,” “consisting of” and “consisting essentially of,” the embodiments or elements presented herein, whether explicitly set forth or not.

The modifier “about” used in connection with a quantity is inclusive of the stated value and has the meaning dictated by the context (for example, it includes at least the degree of error associated with the measurement of the particular quantity). The modifier “about” should also be considered as disclosing the range defined by the absolute values of the two endpoints. For example, the expression “from about 2 to about 4” also discloses the range “from 2 to 4.” The term “about” may refer to plus or minus 10% of the indicated number. For example, “about 10%” may indicate a range of 9% to 11%, and “about 1” may mean from 0.9-1.1. Other meanings of “about” may be apparent from the context, such as rounding off, so, for example “about 1” may also mean from 0.5 to 1.4.

Definitions of specific functional groups and chemical terms are described in more detail below. For purposes of this disclosure, the chemical elements are identified in accordance with the Periodic Table of the Elements, CAS version, Handbook of Chemistry and Physics, 75^th Ed., inside cover, and specific functional groups are generally defined as described therein.

For the recitation of numeric ranges herein, each intervening number there between with the same degree of precision is explicitly contemplated. For example, for the range of 6-9, the numbers 7 and 8 are contemplated in addition to 6 and 9, and for the range 6.0-7.0, the number 6.0, 6.1, 6.2, 6.3, 6.4, 6.5, 6.6, 6.7, 6.8, 6.9, and 7.0 are explicitly contemplated. For example, when a pressure range is described as being between ambient pressure and another pressure, a pressure that is ambient pressure is expressly contemplated.

II. Metal Alloy Composite Particles

Disclosed herein are metal alloy composite particles for use in systems and methods for converting H₂S into hydrogen (H₂) and sulfur (S). Typical metal alloy composite particles disclosed and contemplated herein include metal alloy material, secondary material, and support material. Without being bound by a particular theory, it is believed that each component plays a role in H₂S processing. For instance, the metal alloy material captures sulfur generated from dissociation of H₂S. Additionally, efficient capture of sulfur appears to be linked to the formation of spinel phase, which thermodynamically favors near, or complete, sulfur capture. The secondary material forms active centers on the surface of the metal alloy composite particle where it catalytically dissociates H₂S to H₂ and sulfur. The metal alloy material is dispersed in the support material to prevent sintering and agglomeration of the metal alloy composite particle, which could reduce the regenerability of the particle.

A. Metal Alloy Material

Metal alloy material comprises a first metal component and a second metal component. The first metal component comprises a first metal, a first metal sulfide comprising the first metal, a first metal oxide comprising the first metal, or combinations thereof. The second metal component comprises a second metal, a second metal sulfide comprising the second metal, a second metal oxide comprising the second metal, or combinations thereof.

Usually, each of the first metal and second metal is selected from: iron (Fe), chromium (Cr), nickel (Ni), Zinc (Zn), cobalt (Co), manganese (Mn) and copper (Cu). For example, the first metal component may comprise iron and the second metal component may comprise chromium. In some embodiments, the first metal component comprises iron sulfide and the second metal component comprises chromium sulfide.

The metals of the metal alloy material may be dispersed uniformly as this results in high conversion of H₂S to H₂ and also improves the regenerability of the metal alloy composite particle. Non-uniform dispersion and/or a layered structure may result in diffusion limitations of H₂S in the metal alloy composite particle product layer and lower the reaction kinetics.

B. Secondary Material

The metal alloy composite particle may further comprise one or more secondary material components. In some instances, secondary material is a dopant, as that term is typically understood in the art. In some instances, secondary material has similar properties to a dopant and/or imparts similar characteristics as a dopant, but exists as a different phase. In various implementations, the secondary material is dispersed uniformly along the surface of the particle and is surrounded by the alloy material.

Typically, secondary material is in the form of MS_x, where M is a metal, S is sulfur, and x is in the range of values between 0 and 2. For example, x maybe 0, 1, or 2. X may also be a non-integer value. For example, x may be 0.5 or 1.5. Example metals M include, but are not limited to, molybdenum, nickel, cobalt, manganese, tungsten, vanadium and combinations thereof.

The secondary material may be a sulfide. For example, the secondary material may be a molybdenum disulfide, a nickel sulfide, a cobalt sulfide, a manganese sulfide, a tungsten sulfide, vanadium sulfide or combinations thereof.

In some instances, secondary material is a metal oxide. For example, the secondary material may be a molybdenum oxide, a nickel oxide, a cobalt oxide, a manganese oxide, a tungsten oxide, a vanadium oxide or combinations thereof.

C. Support Material

The metal alloy composite particle may further comprise one or more support materials. The support material can be any inert material. The one or more support materials can be metals, metal oxides, non-metal oxides, zeolites or metal organic frameworks. Suitable support materials include, but are not limited to, alumina, bauxite, titania, silicon, zirconium, and alumina silicate. For example, the support material may be an aluminum oxide, a silicon oxide, a titanium oxide, a zirconium oxide, and the like.

D. Example Amounts and Sizes

The metal alloy composite particle may comprise any suitable ratio of components to produce the desired effect. For example, the metal alloy composite particle may comprise 10-95% by weight of the first metal component, 5-80% by weight of the second metal component, and 0-50% by weight of the secondary material. For example, the metal alloy composite particle may comprise 10-95% by weight iron, 5-80% by weight chromium, and 0-50% by weight of the secondary material.

For example, the metal alloy composite particle may comprise about 10%, about 15%, about 20%, about 25%, about 30%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, about 70%, about 75%, about 80%, about 85%, about 90%, or about 95% by weight of the first metal component. In various implementations, the metal alloy composite particle comprises 10 wt % to 50 wt %; 40 wt % to 95 wt %; 20 wt % to 75 wt %; 30 wt % to 50 wt %; 35 wt % to 65 wt %; 50 wt % to 80 wt %; or 40 wt % to 70 wt % of the first metal component.

The metal alloy composite particle may comprise about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, about 50%, about 55%, about 60%, about 65%, about 70%, about 75%, or about 80% by weight of the second metal component. In various implementations, the metal alloy composite particle comprises 5 wt % to 50 wt %; 45 wt % to 80 wt %; 15 wt % to 65 wt %; 10 wt % to 35 wt %; 35 wt % to 60 wt %; 60 wt % to 80 wt %; or 20 wt % to 45 wt % of the second metal component.

The metal alloy composite particle may comprise about 0%, about 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 40%, about 45%, or about 50% by weight of the secondary material. In various implementations, the metal alloy composite particle comprises 5 wt % to 45 wt %; 10 wt % to 50 wt %; 20 wt % to 40 wt %; 30 wt % to 50 wt %; 10 wt % to 20 wt %; 15 wt % to 35 wt %; or 20 wt % to 30 wt % of the secondary material.

The metal alloy composite particle has a diameter of between about 100 μm and about 10 mm. For example, the metal alloy composite particle may have a diameter of about 100 μm to about 10 mm, about 1 mm to about 9 mm, about 2 mm to about 8 mm, about 3 mm to about 7 mm, or about 4 mm to about 6 mm.

The grain size of the first metal component, the second metal component, and the secondary material can vary depending on the type of material used and the temperature at which the metal alloy composite particle is sintered. A smaller grain size is preferred as it results in faster reaction kinetics due to elimination of diffusion limitations in the metal alloy composite particle.

The range of grain size for the first metal component, the second metal component, and the secondary material can be between 10⁻³ μm to 50 μm. For example, the grain size can be about 10⁻³ μm, about 10⁻² μm, about 1 μm, about 5 μm, about 10 μm, about 15 μm, about 20 μm, about 25 μm, about 30 μm, about 35 μm, about 40 μm, about 45 μm, or about 50 μm.

Another parameter that affects the reaction kinetics is the porosity of the metal alloy composite particle which determines the gas diffusion within the metal alloy composite particle. Porosity of the metal alloy composite particle is proportional to the concentration of support material and it can be in the range of 10⁻³ to 5 cm³/g. The surface area of the metal alloy composite particle is dependent on the grain size as well as the porosity and is in the range of 0.1 to 100 m²/g.

III. Systems and Methods for Converting H₂S into Hydrogen (H₂) and Sulfur

Disclosed herein are systems and methods for converting H₂S into hydrogen (H₂) and sulfur. The system for converting H₂S into hydrogen (H₂) and sulfur may comprise multiple reactors. For example, the system may comprise a sulfidation reactor and a regeneration reactor. The conditions in each of the sulfidation reactor and the regeneration reactor are modified as described below to ensure that the appropriate sulfidation and regeneration reactions occur in each reactor. In other embodiments, the system may comprise one reactor. The conditions in the single reactor may be modified such that the sulfidation and regeneration operations can occur in the single reactor.

Broadly speaking, the disclosed systems and methods reduce the amount of H₂S in the input gas stream. For example, the disclosed method can be used to reduce the amount of H₂S in the gas stream to below 100 ppm. For example, the disclosed method can be used to reduce the amount of H₂S in the gas stream to less than about 100 ppm, less than about 90 ppm, less than about 80 ppm, less than about 70 ppm, less than about 50 ppm, less than about 40 ppm, less than about 30 ppm, less than about 20 ppm, less than about 10 ppm, less than about 5 ppm, less than about 1 ppm, less than about 1 ppm, or less than about 0.1 ppm. For example, the disclosed method can be used to reduce the amount of H₂S in the gas stream to less than 0.1 ppm.

A. Sulfidation Operation

The disclosed method comprises a sulfidation operation. The sulfidation operation can be performed in a sulfidation reactor. The sulfidation reactor can be a fixed bed reactor, a fluidized bed reactor, a co-current moving bed reactor, or a counter-current moving bed reactor. A moving bed reactor configuration also includes a packed moving bed, staged fluidized bed, a downer and/or a rotary kiln.

The sulfidation operation comprises contacting a first gaseous stream comprising H₂S with a metal alloy composite particle. The first gaseous stream may further comprise additional gases. For example, the H₂S-containing gas stream can also include CO, H₂, and/or hydrocarbons. Example hydrocarbons include but are not limited to methane, ethane, propane, butane and higher alkanes. The first gaseous stream may contain H₂S and additional gases in other proportions or quantities. Usually, the first gaseous stream includes trace amounts or no oxygen (O₂).

The sulfidation operation may be performed at any suitable temperature to facilitate sulfidation of the metal alloy composite particle. For example, the sulfidation operation may be performed at about 100° C. to about 950° C. For example, the sulfidation operation may be performed at about 100° C., about 150° C., about 200° C., about 250° C., about 300° C., about 350° C., about 400° C., about 450° C., about 500° C., about 550° C., about 600° C., about 650° C., about 700° C., about 750° C., about 800° C., about 850° C., about 900° C., or about 950° C. In some instances, the sulfidation operation is performed at about 300° C. to about 450° C. As another example, the sulfidation operation is performed at about 350° C. to about 400° C.

The equilibrium of sulfidation reaction favors operating at lower temperatures, but the reaction kinetics is faster at higher temperatures. As such, some embodiments perform the sulfidation operation at a temperature of 300° C. to 450° C. Performing sulfidation at 300° C. to 450° C. can eliminate the need for cooling and reheating the H₂S containing gas stream as is done for conventional H₂S removal processes such as Selexol, Rectisol, or amine based processes.

The sulfidation operation may be performed at any suitable pressure. For example, the pressure at which sulfidation operation occurs can be about 1 atm to about 150 atm. For example, the pressure can be about 1 atm, about 2 atm, about 3 atm, about 4 atm, about 5 atm, about 6 atm, about 7 atm, about 8 atm, about 9 atm, about 10 atm, about 15 atm, about 20 atm, about 25 atm, about 30 atm, about 35 atm, about 40 atm, about 45 atm, about 50 atm, about 55 atm, about 60 atm, about 65 atm, about 70 atm, about 75 atm, about 80 atm, about 85 atm, about 90 atm, about 95 atm, about 100 atm, about 105 atm, about 110 atm, about 115 atm, about 120 atm, about 125 atm, about 130 atm, about 135 atm, about 140 atm, about 145 atm, or about 150 atm. In various instances, the pressure at which the sulfidation operation occurs is from 1 atm to 30 atm; 1 atm to 5 atm; 1 atm to 60 atm; 5 atm to 20 atm; 2 atm to 10 atm; or 1 atm to 15 atm. Generally, the kinetics of the sulfidation reaction appear to be faster at higher pressures and there is not an effect of pressure on the equilibrium of sulfidation reaction.

The kinetic rate of sulfidation reaction determines the gas residence time in the sulfidation reactor for maximum conversion of H₂S. The gas residence time can vary from 0.2 seconds to 45 minutes. It is preferred to have the gas residence time between 0.5 s to 15 min. For example, the gas residence time can be around 0.5 seconds, about 1 second, about 30 seconds, about 1 minute, about 2.5 minutes, about 5 minutes, about 7.5 minutes, about 10 minutes, about 12.5 minutes, or about 15 minutes.

The amount of H₂S gas that can be treated by the disclosed process is dependent on the composition of the metal alloy composite particle. The ratio of gas to metal alloy composite particle that can be used in the disclosed systems and methods can be about 1:5 to about 10:1. Preferably, the ratio of gas to metal alloy composite particle ranges from about 1:2 to about 5:1. For example, the ratio of gas to metal alloy composite particle can be about 1:2, about 1:1, about 2:1, about 3:1, about 4:1, or about 5:1.

In the sulfidation operation, the hydrogen sulfide (H₂S) in the first gaseous input stream reacts in a sulfidation reaction with the metal alloy composite particle to generate hydrogen gas (H₂) and one or more sulfide minerals. The hydrogen gas (H₂) may be collected and stored for future use in other processes. The sulfide mineral is selected from the group consisting of a metal sulfide, a thiospinel and combinations thereof. Without being bound by a particular theory, it appears that the presence of thiospinel is responsible for favorable equilibrium towards H₂S decomposition and is non-reactive towards other gases that may be present in the H₂S containing gas stream. For example, the sulfide mineral may be an iron sulfide, a chromium sulfide, or combinations thereof. In some embodiments, sulfide mineral comprises FeCr₂S₄.

B. Regeneration Operation

The disclosed method further comprises a regeneration operation. Typically, the regeneration operation occurs at higher temperatures than those used during the sulfidation operation. The regeneration operation can be performed in a regeneration reactor. The regeneration reactor can be a fixed bed reactor, a fluidized bed reactor, a co-current moving bed reactor, or a counter-current moving bed reactor. A moving bed reactor configuration also includes a packed moving bed, staged fluidized bed, a downer and/or a rotary kiln.

The regeneration operation comprises contacting a second gaseous input stream comprising at least one inert gas with the one or more sulfide minerals generated during the sulfidation operation. The regeneration operation thereby generates sulfur gas and regenerates the metal alloy composite particle for subsequent use. The sulfur gas obtained from the regeneration operation can be collected for future use in downstream applications. For example, the sulfur gas can be condensed and removed as solid or liquid sulfur based on its downstream application.

The at least one inert gas can include nitrogen, carbon dioxide and combinations thereof. For example, the at least one inert gas can be nitrogen. For example, regeneration operation can comprise contacting FeCr₂S₄ produced during the sulfidation operation with nitrogen gas, thereby regenerating iron sulfide and chromium sulfide and producing sulfur gas.

The regeneration operation may be performed at any suitable regeneration temperature to facilitate regeneration of the metal alloy composite particle. The regeneration temperature is dependent on the sulfur pressure in the regeneration reactor. A lower sulfur pressure in the regeneration reactor favors the equilibrium towards removal of sulfur and hence lower regeneration temperatures can be used. The regeneration temperatures can vary from 500° C. to 1100° C. For example, the regeneration operation may be performed at about 750° C., about 800° C., about 850° C., about 900° C., about 950° C., about 1000° C., about 1050° C., or about 1100° C. In various implementations, the regeneration temperature may be from 600° C. to 1000° C.; from 700° C. to 1100° C.; from 800° C. to 1000° C.; or from 700° C. to 900° C.

The regeneration operation may be performed under vacuum. Alternatively, the regeneration operation may be performed under pressure conditions. The pressure conditions in the regeneration reactor can range from 1 atm to 150 atm. For example, the pressure can be about 1 atm, about 2 atm, about 3 atm, about 4 atm, about 5 atm, about 6 atm, about 7 atm, about 8 atm, about 9 atm, about 10 atm, about 15 atm, about 20 atm, about 25 atm, about 30 atm, about 35 atm, about 40 atm, about 45 atm, about 50 atm, about 55 atm, about 60 atm, about 65 atm, about 70 atm, about 75 atm, about 80 atm, about 85 atm, about 90 atm, about 95 atm, about 100 atm, about 105 atm, about 110 atm, about 115 atm, about 120 atm, about 125 atm, about 130 atm, about 135 atm, about 140 atm, about 145 atm, or about 150 atm.

In some instances, a high gas:solids ratio is employed for the regeneration operation as it keeps the sulfur pressure low in the regeneration reactor, thus enabling a relatively lower regeneration temperature. For example, the gas:solids molar ratio can range from 0.2 to 10, preferably, from 0.5 to 5. For example, gas:solids molar ratio can be about 1:2, about 1:1, about 2:1, about 3:1, about 4:1, or about 5:1.

A low gas residence time is preferred to aid in maintaining low sulfur pressures in the regeneration reactor. The gas residence time can vary from 0.05 seconds to about 5 minutes, preferably from about 0.1 s to about 2 minutes. For example, the gas residence time can be about 0.05 seconds, about 0.1 seconds, about 1 second, about 5 seconds, about 10 seconds, about 30 seconds, about 60 seconds, about 90 seconds, about 2 minutes, about 3 minutes, about 4 minutes, or about 5 minutes.

The disclosed method can be operated in batch operational mode, a semi-batch operational mode, or continuous operation mode. The method can further comprise contacting the metal alloy composite particle produced following the regeneration operation, (i.e. the regenerated metal alloy composite particle) with a subsequent first gaseous input stream, thus repeating the process of isolating hydrogen gas (H₂) and sulfur from an H₂S containing feed stream. The hydrogen gas (H₂) production performance of the regenerated metal alloy composite particle can be similar to the performance of the original metal alloy composite particle.

C. Example Configurations of Systems and Method for H₂S Conversion

FIG. 1, FIG. 2, and FIG. 3 are schematic diagrams of exemplary systems for conversion of H₂S. Various aspects regarding possible operating conditions for the exemplary systems, such as temperature, pressure, residence time, etc., as well as exemplary metal alloy composite particles usable in the exemplary systems, are described in greater detail above, apply to the following discussion, and are not repeated below for the purpose of conciseness.

FIG. 1 shows a schematic diagram of exemplary system 100 for H₂S conversion to H₂ and S. As shown in FIG. 1, system 100 comprises sulfidation reactor 102 and regeneration reactor 104. The sulfidation reactor 102 includes a metal alloy composite particle as disclosed herein. An H₂S containing gas stream is provided into the sulfidation reactor 102, resulting in the formation of hydrogen gas (H₂) and one or more sulfide minerals. The hydrogen gas (H₂) is collected, and the one or more sulfide minerals are provided to the regeneration reactor 104. An inert gas stream is provided into the regeneration reactor 104, resulting in the formation of sulfur gas and regeneration of the metal alloy composite particle. The metal alloy composite particle is provided back to the sulfidation reactor 102 and the sulfur gas is collected.

FIG. 2 shows a schematic diagram of exemplary system 200 for H₂S conversion to H₂ and S. In system 200, alloy material reacts with H₂S or H₂S containing gas (stream number 251) in reactor 202. The alloy material with the captured sulfur is then transferred to reactor 204, where the alloy material is regenerated by an inert gas such as N₂. The N₂ sent to reactor 204 (stream number 252) is preheated with the gas outlet from reactor 204 and additional heating may be provided by burning fuel gas. The sulfur is removed in reactor 204, and the sulfur is then condensed by cooling with water and finally separated from N₂ in a gas-liquid separator 206. The regenerated solids are sent to reactor 208, where they are fluidized with heated N₂ (stream number 253) and then transported back to reactor 202. N₂ and solids separation occurs in the cyclone separator 210. The separated N₂ is recycled back to reactor 204 (stream number 255). The separated N₂ can also be sent to the reactor 208 for fluidization (stream number 256) or to an outlet of reactor 204 (stream number 257) for pushing the solids into reactor 208. H₂ is injected as a zone seal gas to prevent gas mixing between reactor 202, reactor 204 and cyclone separator 210. This is important to reduce downstream H₂ product gas purification.

Reactors 202 and 204 are operated as countercurrent moving bed reactors. The residence time of gas and solids in reactors 202 and 204 may be controlled such that there is complete H₂S conversion in reactor 202 and complete regeneration in reactor 204. Reactor 208 is a fluidized bed reactor and its main purpose is for transporting solids via a riser back to reactor 202.

FIG. 3 shows a schematic diagram of exemplary system 300 for H₂S conversion to H₂ and S. System 300 includes three fixed bed reactors. At a given time, sulfidation occurs in reactor 302, regeneration in reactor 304 and reactor 306 is on standby. H₂S or H₂S containing gas (stream number 351) is sent to reactor 302 and the outlet gas is sent to a pressure swing adsorption (PSA) unit 308 to produce high purity H₂. N₂ (stream number 352) is heated in two stages by preheater and then by fuel gas, before being sent to reactor 304 for removing sulfur from the solids. The sulfur removed is then condensed out in a sulfur condenser and the cooled down N₂ is recycled (stream number 353) back to the preheater. Once reactor 302 is saturated with sulfur, it is switched to regeneration with the use of remote operated valves. Reactor 306 is switched to sulfidation as it contains regenerated solids and reactor 304 is switched to standby. The number of reactors and switching time is contingent on the gas flow rates and amount of solids used in each of the reactors.

FIG. 4 shows an example method 400 for H₂S conversion to H₂ and S. Method 400 begins by contacting the metal alloy composite particle (such as a metal alloy composite particle prepared by example method 500) with an H₂S containing gas stream in a sulfidation reactor (operation 402). Operation 402 results in the formation of hydrogen gas (H₂) and one or more metal sulfides. Next, the hydrogen gas (H₂) is collected (operation 404). The remaining sulfide minerals are provided to the regeneration reactor (operation 406). The sulfide minerals are contacted with an inert gas in the regeneration reactor (operation 408). Operation 408 results in the formation of sulfur gas and regeneration of the metal alloy composite particle. The sulfur gas is collected (operation 410). The regenerated metal alloy composite particle is provided back to the sulfidation reactor (operation 412). The process then begins again by contacting the regenerated metal alloy composite particle with an H₂S containing gas stream in the sulfidation reactor (operation 414). The process may be repeated for any desired number of cycles.

D. Example Improvements and Industrial Applications

The systems and methods disclosed herein result in conversion of a poisonous, toxic and corrosive gas like H₂S to highly valuable chemicals like hydrogen (H₂) and sulfur (S₂). The methods can use a two-reactor system with few heat exchangers, or a one reactor system, to produce H₂ and sulfur from H₂S. Therefore, there are capital cost benefits in using fewer processing units compared to typically used methods. Moreover, the methods described herein are robust towards other gases, like carbon monoxide, hydrogen and hydrocarbons, commonly found in industrial process streams that contain H₂S. Therefore, the instant systems and methods typically do not require separating these gases before treating H₂S, which allows for savings in energy and capital costs that are usually involved with separating these gases.

The methods described herein allow H₂S to be treated at very high temperatures. Treating at high temperatures reduces or eliminates the need for cooling and reheating the H₂S containing gas stream as is typically done for conventional H₂S removal processes such as Selexol, Rectisol, or amine based processes. Moreover, the disclosed methods and process utilize solids with high recyclability, resulting in the capacity for long term use and minimal replacement and waste management costs.

The methods described herein can be used in multiple industrial applications. For example, the methods described herein can be used for coal gasification to produce synthesis gas (syngas). The major components of synthesis gas are carbon monoxide (CO) and H₂ and this gas stream is at >500° C. This gas can be directly sent to the process disclosed herein without the need for cooling the gas stream or removing CO or H₂.

The methods described herein can be used in natural gas processing methods. H₂S is typically removed from natural gas before it is sent to catalytic processes, such as steam methane reforming, to produce syngas and H₂. Steam methane reforming occurs in temperature range of 700-1000° C. and requires very low concentrations of H₂S in the gas stream. The methods described herein can be used to reduce H₂S concentrations in a gas stream to the desired values before use of the gas stream in catalytic processes such as steam methane reforming.

The methods described herein can be used in crude oil processing. Sulfur from crude oil is typically removed in a hydrodesulfurization unit by treating it with H₂ in a temperature range from 300-400° C. The gas from this unit is a mixture of H₂S and H₂. The gas from such a hydrodesulfurization unit can be directly treated by a method described herein to produce H₂ and sulfur.

IV. Systems and Methods for Producing Metal Alloy Composite Particles

Further disclosed herein are systems and methods for producing metal alloy composite particles. The metal alloy composite particle may be produced by mixing the first metal component and the second metal component in their respective desired amounts. The mixture of the first metal component and the second metal component is reacted with H₂S at a temperature of about 300° C. to about 900° C. For example, the mixture of the first metal component and the second metal component can be reacted with H₂S at a temperature of about 300° C., about 350° C., about 400° C., about 450° C., about 500° C., about 550° C., about 600° C., about 650° C., about 700° C., about 750° C., about 800° C., about 850° C., or about 900° C. The time of the reaction is dependent on the amount of first metal component and the second metal component used. A mixture of thiospinel and higher metal sulfides is formed at the end of the reaction.

Nitrogen is then passed over the reacted mixture in a temperature range of about 600° C. to about 1200° C. For example, nitrogen may be passed over the reacted mixture at a temperature of about 600° C., about 650° C., about 700° C., about 750° C., about 800° C., about 850° C., about 900° C., about 950° C., about 1000° C., about 1050° C., about 1100° C., about 1150° C., or about 1200° C.

Subsequently, a secondary material can be mixed together with the alloy material. Additionally, a support material can be mixed together with the alloy material. The mixture is then sintered at a temperature of about 700° C. to about 1400° C. For example, the mixture may be sintered at a temperature of about 700° C., about 750° C., about 800° C., about 850° C., about 900° C., about 950° C., about 1000° C., about 1050° C., about 1100° C., about 1150° C., about 1200° C., about 1250° C., about 1300° C., about 1350° C., or about 1400° C.

FIG. 5 shows an example method 500 for preparing a metal alloy composite particle for use in the disclosed method of H₂S conversion to H₂ and S. Method 500 begins by mixing the first metal component and the second metal component (operation 502). The mixture of the first metal component and the second metal component is reacted with a gas containing H₂S (operation 504). Next, nitrogen is passed over the mixture (operation 506). Next, a secondary material (operation 508) and a support material (510) are added to the mixture. Lastly, the mixture is sintered (operation 512).

V. Experimental Examples

Example 1

Iron-Chromium (Fe—Cr) Metal Alloy Preparation

Iron sulfide (FeSx, 0<x<2) and chromium sulfide (CrSy, 0<y<1.5) were mixed in a molar ratio of 1:2. Iron oxide, chromium oxide, iron metal, chromium metal or a mixture of these compounds can also be taken as the starting material. The said mixture was reacted with gas containing H₂S at a concentration of 0.9% in a fixed bed reactor kept in a horizontal tube furnace. The said gas containing H₂S was reacted at a temperature of 800° C. After reaction with H₂S, the gas was switched to N₂ and the temperature was increased to 950° C. FIG. 6 shows the X-ray diffraction (XRD) analysis of the solid sample obtained after cooling down to room temperature under the N₂. The presence of an Fe—Cr alloy is clearly visible from the XRD spectra.

Example 2

H₂S Conversion by Exemplary Metal Alloy Composite Particles

FIG. 7 shows the performance of an Fe—Cr alloy in a fixed bed reactor for H₂S conversion to H₂ and S over multiple sulfidation and regeneration operations. The temperatures of sulfidation and regeneration operations were 800° C. and 950° C., respectively. A 0.9% H₂S/N₂ gas was injected into the fixed bed reactor during sulfidation operation and N₂ was injected during the regeneration operation. The gas hourly space velocity (GHSV) for sulfidation operation for the first and second cycle was 5000 hr-1, whereas, GHSV for third, fourth and fifth sulfidation operation was 2580 hr-1. The concentration of gas leaving the fixed bed reactor was measured using a Siemens CALOMAT 6E H₂ analyzer. The gas was also intermittently sampled by Interscan's Model RM17-500m Toxic gas monitor to measure H₂S concentration in the reactor outlet. H₂S conversion was calculated based on the H₂ concentration detected by the H₂ analyzer. A high H₂S conversion over multiple GHSVs repeated over several sulfidation-regeneration operations demonstrates excellent performance and recyclability of the Fe—Cr alloy. FIG. 8 shows the presence of iron-chromium thiospinel (FeCr₂S₄) via XRD analysis of the solids after the fifth sulfidation operation.

Table 1 shows the inlet and outlet composition of gas sent during sulfidation operation for two different runs at 800° C. in a fixed bed reactor containing Fe—Cr alloy. In run 1, 50 ml/min of 0.9% H₂S/N₂ and 46.95 ml/min 9.6% methane (CH₄)/19% CO/81.4% N₂ was co-injected into the fixed bed reactor for 30 min. The reactor outlet gas concentration was measured using a Siemens Ultramat 23 gas analyzer to measure CO, CO₂ and CH₄ concentrations and Siemens Calomat 6E gas analyzer to measure H₂ concentration. In run 2, 100 ml/min of 0.9% H₂S/N₂ and 100 ml/min of 100% H₂ was co-injected into the fixed reactor for 30 min. The reactor outlet gas concentration was measured using a Siemens CALOMAT 6E H₂ analyzer. The fact that the inlet and outlet gas compositions are the same indicates that CH₄, CO and H₂ do not react with the Fe—Cr alloy.

TABLE 1
Inlet and outlet gas composition for two experiments in a fixed bed
reactor at 800° C., (*based on XRD analysis results and mass balance).
	Run 1	Run 2
	Inlet gas	Outlet gas	Inlet gas	Outlet gas
	composition	composition	composition	composition
Gases	(%)	(%)	(%)	(%)*
H2S	0.46	0.009	0.45	0
CH4	9.28	9.28	0	0
CO	4.55	4.55	0	0
H2	0	0.451	50	50.45
N2	85.71	85.71	49.55	49.55

XRD analysis of the sample at the end of the Run 1 and Run 2 shown in FIG. 9 and FIG. 10, respectively, proved that sulfur in H₂S was captured by the Fe—Cr alloy and FeCr₂S₄ was formed.

FIG. 11 and FIG. 12 illustrate the favorable effect that FeCr₂S₄ formation has on the thermodynamic equilibrium conversion of H₂S to Hz. Equilib module in FactSage 7.1 software was used to perform the thermodynamic calculations. A basis of 1 mol of iron monosulfide (FeS) and 1 mol of H₂S was selected whereas the moles of chromium monosulfide (CrS) were varied. In FIG. 12, FeCr₂S₄ is observed to form at FeS:CrS molar ratio of 2 and from that value of ratio onwards the corresponding H₂S fractional conversion to H₂ is 1 as seen in FIG. 11.

Example 3

Fe—Cr Bimetallic Alloy Comparison with Fe—Cr Bimetallic Alloy and MoS₂ Secondary Material

Table 2 shows the comparison of H₂S conversion by Fe—Cr alloy material (sample 1) against that of Fe—Cr alloy material added with MoS₂ secondary material (sample 2). The primary phases present in the Fe—Cr alloy based on XRD analysis are FeCr₂S₄ (31.3 wt %), FeCr or 410 L stainless steel (63.4 wt %) and Cr₂O₃ (5.2 wt %). The composition of sample 2 is 50 wt % of the Fe—Cr alloy (sample 1) and 50 wt % MoS₂. For both samples, powder of size less than 125 microns was placed in between quartz wool and supported in the heated region of a 0.5 inch inner diameter ceramic reactor. The samples were heated to a temperature of 800° C. under nitrogen followed by reaction with 0.9% H₂S in the sulfidation step, where the gas flow rate was varied to test different gas hourly space velocities (GHSVs). The sulfidation step was followed by a regeneration step under nitrogen flow at 950° C. Multiple sulfidation and regeneration steps were conducted for both the samples where different GHSVs were tested during the sulfidation step. The reactor outlet gas composition was measured using a Siemens CALOMAT 6E H₂ analyzer for H₂ concentration and intermittently using Interscan's Model RM17-500m Toxic gas monitor for H₂S concentration. A high H₂S conversion for sample 2 indicates faster reaction kinetics of the solid sample with H₂S, which may be a result of addition of MoS₂ as the secondary material. The XRD analysis of Sample 2 after reaction is shown in FIG. 13, where FeCr₂S₄ and MoS₂ phases have been marked.

TABLE 2
H2S conversion comparison between
sample 1 and sample 2 at 800° C. with 0.9% H2S
	H2S conversion (%)
GHSV (hr−1)	Sample 1	Sample 2
12000	83.33	100
15000	73.24	88.55
18000	61.04	78.84

Example 4

Fe—Cr Bimetallic Alloy Comparison with Fe—Cr Bimetallic Alloy with MoS₂ Secondary Material and SiO₂ Support Material

Table 3 compares the H₂S conversion of Fe—Cr alloy (sample 3) with that of Fe—Cr alloy with added MoS₂ secondary material and SiO₂ as the support material (sample 4). Based on XRD analysis, sample 3 has FeCr₂S₄ (37.3 wt %), FeCr or 410 L stainless steel (25 wt %) and Fe_0.879S (37 wt %) as the major phases. The composition of sample 4 is 37.5 wt % Fe—Cr alloy (sample 3), 25 wt % MoS₂ and 37.5 wt % SiO₂. Multiple sulfidation-regeneration steps were conducted on both the samples in a 0.5 inch inner diameter ceramic reactor. The sulfidation temperature was 800° C. and regeneration temperature was 950° C. H₂S conversion was measured during one of the sulfidation steps at the same H₂S flow rate per unit active material weight for both the samples. The active material consists of both the Fe—Cr alloy as well as the secondary material-MoS₂. The reactor outlet gas composition was measured using a Siemens CALOMAT 6E H₂ analyzer for H₂ concentration and intermittently using Interscan's Model RM17-500m Toxic gas monitor for H₂S concentration. The H₂S conversion of sample 4 is slightly higher than sample 3 which may be a result of faster reaction kinetics with H₂S. The H₂S conversion for sample 4 may be further enhanced by varying its alloy, secondary material and/or support material composition. FIG. 14 shows the FeCr₂S₄ and MoS₂ phases present in sample 4 based on XRD analysis.

TABLE 3
H2S conversion comparison between
sample 3 and sample 4 at 800° C. with 0.9% H2S
0.9% H2S flow rate/weight of	H2S conversion (%)
active material (ml/min · g)	Sample 3	Sample 4
128	83.33	86.11

Example 5

Fe—Cr Bimetallic Alloy with MoS₂ Secondary Material with Different Gas Mixtures

Fe—Cr alloy with 20 wt % MoS₂ was tested with four different gas mixtures, shown in Table 4 below, and at a pressure of 1.8 bar.

TABLE 4
Reaction performance of Fe—Cr alloy with 20 wt % MoS2 with different gas mixtures
[*HCs = (1.04 vol %) 1,3-butadiene, (2.02 vol %) 2-butene, (6.04 vol %) hydrogen,
(7.25 vol %) methane, (2.07 vol %) n-pentane, (2 vol %) propylene, (79.58 vol %)
ethylene].
		Gas
		hourly
		space
		velocity
Mixture	Inlet gas composition (%)	GHSV	Reaction
No.	CH4	CO	H2	CO2	H2S	N2	HCs*	(hr−1)	performance
1	7.08	3.52	—	—	0.56	88.84	—	8800	95-100% H2S
									conversion for 45
									min
									No oxides in solids
2	—	—	75	—	0.25	24.75	—	24000	95-100% H2S
									conversion for 15
									min
3	—	—	—	25	0.67	74.33	—	10000	95-100% H2S
									conversion for 36
									min
									No oxides in solids
4	—	—	—	—	0.4	43.89	55.71	12000	95-100% H2S
									conversion for 23
									min
									No carbon
									deposition

The Fe—Cr alloy was used in powder form with particle size <125 microns in a ceramic fixed bed reactor of 0.5 inch inner diameter. The reactor was heated using an electrical heater to a temperature of 400° C. under the flow of N₂. Once the reactor temperature reached 400° C., mixing of the various gas compositions mentioned in Table 4 was started.

Gas hourly space velocity (GHSV) shown in the second to last column in Table 4 was calculated based on the gas flow rate and metal alloy composite bed volume. H₂S conversion was measured based on measuring sulfur content in the alloy before and after the reaction. Sulfur content was measured using a Thermo Fisher Scientific TS 3000 total sulfur analyzer (Waltham, Mass.). The H₂S conversion for the different gas mixtures is shown in the last column of Table 4.

For gas mixtures 1 and 3, no oxides were observed in the solids from XRD analysis. Moreover, no carbon deposition was observed for gas mixture 4 based on XRD analysis of the reacted sample. Therefore, the alloy appears to be resistant to oxidation with CO₂ and CO along with being resistant to carbon deposition in presence of hydrocarbons at 400° C. This resistance allows for application of the alloy for H₂S capture from a variety of process streams that can contain any of the contaminants mentioned in Table 4.

Example 6

Recyclability of Fe—Cr Alloy Sample

Recyclability of exemplary Fe—Cr alloy particles was tested by performing twelve consecutive sulfidation-regeneration cycles over Fe—Cr alloy with 20 wt % MoS₂ in a fixed bed reactor. The fixed bed reactor was made of ceramic material and had an inner diameter of 0.5 inch. The sulfidation temperature was 400° C. and the regeneration temperature was 950° C. The gas feed during sulfidation step was 0.9% H₂S balanced with N₂ at a GHSV of 1490 hr⁻¹. The reactor pressure was 1 bar for all the sulfidation steps except for the 8^th step where the reactor pressure was increased to 1.8 bar. H₂S conversion was calculated based on the H₂ concentration measured using a Siemens CALOMAT 6E H₂ analyzer. Nearly 100% conversion (FIG. 15) was observed over the 12 cycles, which indicated excellent recyclability of the Fe—Cr alloy.

Example 7

Effect of Pressure on H₂S Conversion with Fe—Cr Alloy

Effects of pressure on H₂S conversion with a Fe—Cr alloy were tested. Thermodynamic calculations conducted in FactSage 7.3 software demonstrate no effect of pressure on the conversion of H₂S. The H₂S input was 1 mole, whereas, FeS and CrS input was 1 mole and 2 moles, respectively. FIG. 16 shows that at 400° C., H₂S conversion is nearly 100% for all the pressures between 1 to 60 atm.

Experimentally, pressure was observed to improve the kinetics of H₂S conversion. Fe—Cr alloy powder of particle size <125 microns was reacted with 0.9% H₂S in a 0.5 inch inner diameter ceramic reactor. H₂S conversion was calculated based on the H₂ concentration measured using a Siemens CALOMAT 6E H₂ analyzer and intermittently with Interscan's Model RM17-500m Toxic gas monitor for H₂S concentration. At 400° C. reactor temperature, the H₂S conversion was 32% higher at 1.8 atm compared to 1 atm for a GHSV of 4500 hr⁻¹.

Example 8

Performance of Fe—Cr Alloy Material with Ni

Fe—Cr alloy material with Ni was tested in a fixed bed reactor for H₂S conversion. The sample consisted of 45 wt % Fe—Cr alloy, 10 wt % Ni₃S₂ and 45 wt % SiO₂. The Fe—Cr alloy material was used in a powder form in a 0.5 inch inner diameter ceramic reactor, which was heated by an electrical heater to a temperature of 800° C. H₂S conversion was calculated by measuring the H₂S concentration in the reactor outlet using Interscan's Model RM17-500m Toxic gas monitor. 0.9% H₂S balanced with N₂ was reacted with Sample 1 at a GHSV of 3800 hr⁻¹. The maximum H₂S conversion was >90%.

Claims

1. A method comprising: contacting a first gaseous input stream comprising hydrogen sulfide (H2S) with a metal alloy particle at a temperature between 300° C. and 450° C., the metal alloy particle comprising at least a first metal component comprising a first metal, and a second metal component comprising a second metal that is different from the first metal, whereupon the hydrogen sulfide (H2S) in the first gaseous input stream reacts in a sulfidation reaction with the metal alloy particle to generate hydrogen gas (H2) and one or more sulfide minerals,collecting a first gaseous product stream comprising the hydrogen gas (H2);after collecting the first gaseous product stream, contacting a second gaseous input stream comprising at least one inert gas with the one or more sulfide minerals, thereby generating sulfur gas and regenerating the metal alloy particle; andcollecting a second gaseous product stream comprising the sulfur gas.

2. The method according to claim 1, wherein the first gaseous input stream further comprises one or more of CO, H2, CO2, and a hydrocarbon feedstock.

3. The method of claim 1, wherein the first metal component comprises the first metal, a first metal sulfide comprising the first metal, a first metal oxide comprising the first metal, or combinations thereof, and wherein the second metal component comprises the second metal, a second metal sulfide comprising the second metal, a second metal oxide comprising the second metal, or combinations thereof.

4. The method of claim 1, wherein each of the first metal and second metal is selected from the group consisting of iron (Fe), chromium (Cr), nickel (Ni), Zinc (Zn), cobalt (Co), manganese (Mn) and copper (Cu).

5. The method of claim 1, wherein the sulfide mineral is selected from the group consisting of a metal sulfide, a thiospinel and combinations thereof.

6. The method of claim 5, wherein the sulfide mineral is selected from the group consisting of an iron sulfide, a chromium sulfide, and combinations thereof.

7. The method of claim 6, wherein the sulfide mineral comprises FeCr2S4.

8. The method of claim 1, wherein the first metal is iron (Fe) and the second metal is chromium (Cr).

9. The method of claim 1, wherein the at least one inert gas is selected from the group consisting of nitrogen, carbon dioxide, air and combinations thereof.

10. The method of claim 1, wherein the metal alloy particle is a particle having a diameter of between about 100 microns and about 10 mm.

11. The method of claim 1, wherein the step of contacting the first gaseous input stream with the metal alloy particle is carried out in a sulfidation reactor selected from the group consisting of a fixed bed reactor, a fluidized bed reactor, a co-current moving bed reactor and a counter-current moving bed reactor.

12. The method of claim 11, wherein the molar ratio of gases:solids within the sulfidation reactor during the step of contacting the first gaseous input stream with the metal alloy particle is between about 0.2 to about 10.

13. The method of claim 1, wherein the step of contacting the first gaseous input stream with the metal alloy particle is carried out at a first pressure between about 1 atm and about 150 atm.

14. The method of claim 1, wherein the step of contacting the second gaseous input stream with the one or more sulfide minerals is carried out in a regeneration reactor selected from the group consisting of a fixed bed reactor, a fluidized bed reactor, a co-current moving bed reactor and a counter-current moving bed reactor.

15. The method of claim 14, wherein the molar ratio of gases:solids within the regeneration reactor during the step of contacting the second gaseous input stream with the one or more sulfide minerals is between about 0.2 to about 10.

16. The method of claim 1, wherein the step of contacting the second gaseous input stream with the one or more sulfide minerals is carried out at a second temperature between about 500° C. and about 1100° C., and a second pressure between about vacuum conditions and about 150 atm.

17. The method of claim 1, wherein the first gaseous product stream comprises less than 100 ppmv H2S.

18. The method of claim 1, further comprising after collecting the second gaseous product stream, contacting the regenerated metal alloy with a subsequent first gaseous input stream such that a hydrogen gas (H2) production performance of the regenerated metal alloy particle is similar to a hydrogen gas (H2) production performance of the metal alloy particle.

19. The method of claim 1, wherein contacting the first gaseous input stream and contacting the second gaseous input stream is performed in a batch operational mode, in a semibatch operational mode, or in a continuous operational mode.

20. The method of claim 1, wherein the first gaseous input stream does not include oxygen (O2).

21. A metal alloy particle for use in a method of converting H2S to hydrogen (H2) and sulfur, the metal alloy particle comprising a first metal component, a second metal component, and at least one secondary material, wherein the first metal component comprises iron, the second metal component comprises chromium, and the at least one secondary material is molybdenum, nickel, cobalt, manganese, tungsten, vanadium or a combination thereof.

22. The metal alloy particle of claim 21, wherein the metal alloy particle further comprises one or more support materials.

23. The metal alloy particle of claim 21, wherein the first metal component comprises an iron sulfide and the second metal component comprises a chromium sulfide.

24. The metal alloy particle of claim 21, wherein the at least one secondary material is a molybdenum sulfide, a nickel sulfide, a cobalt sulfide, a manganese sulfide, a tungsten sulfide, vanadium sulfide or a combination thereof.

25. The metal alloy particle of claim 21, wherein the metal alloy particle comprises 10-95% by weight of the first metal component, 5-80% of the second metal component, and 1-50% by weight of the at least one secondary material.

26. The metal alloy particle of claim 21, wherein the metal alloy comprises a support material selected from Al2O3, SiO2, TiO2, and ZrO2.

27. A method of producing the metal alloy particle of claim 21, the method comprising mixing the first metal component with the second metal component to produce a mixture, contacting the mixture with a gas stream comprising H2S to produce a reacted mixture, passing nitrogen over the reacted mixture to form a bimetallic alloy, and mixing one or more secondary materials and optionally one or more support materials with the bimetallic alloy to produce the metal alloy.