VERSATILE AND FLEXIBLE, ENVIRONMENTALLY FRIENDLY AND ECONOMICALLY VIABLE PROCESS FOR CONVERTING SOUR NATURAL GAS TO SWEET NATURAL GAS, GREEN HYDROGEN AND CARBON DISULFIDE

Abstract

A process for preparing hydrogen by a catalytic conversion of sour natural gas, including feeding sour natural gas and one or more H2S recycled streams, optionally mixed with fresh CO2, to a reformer reactor packed with a catalyst activated in-situ by sulfidation. An apparatus for carrying out the process, to convert sour natural gas to sweet natural gas, hydrogen and carbon disulfide, and catalysts that can be used in the process, are also disclosed.

Claims

1. A process for preparing hydrogen by a catalytic conversion of sour natural gas, comprising feeding sour natural gas and one or more H.sub.2S recycled streams, optionally mixed with fresh CO.sub.2, to a reformer reactor packed with a catalyst activated in-situ by sulfidation.

2. The process according to claim 1, wherein the feed stream comprises from 50 to 90 vol % methane, not less than 10 vol % H.sub.2S and 0 to 40 vol % CO.sub.2.

3. The process according to claim 2, wherein the sour natural gas comprises from 15 to 35 vol % H.sub.2S.

4. The process according to claim 1, wherein the catalytic conversion of sour natural gas takes place over the catalyst in the reformer reactor under the following conditions: temperature in the range from 800 to 950 C., WHSV.sub.H2S in the range of 0.5 to 5 h.sup.1, at total pressure of 1 to 3 atm.

5. The process according to claim 1, wherein the effluent from the reactor is passed through a separation system comprising several units; H.sub.2S-containing streams are collected and are recycled to the reformer reactor, whereas CO.sub.2 is produced downstream and is directed to the reformer reactor or is used as a feed component, together with the hydrogen produced by the process, in a plant converting hydrogen and CO.sub.2 into liquid hydrocarbons.

6. The process according to claim 1, wherein separation of unreacted H.sub.2S from the effluent of the reformer reactor, and separation of the effluent into a liquid stream consisting of the C.sub.s2 by-product and the (CH.sub.4+H.sub.2)-containing gas product stream, includes: A) membrane separation followed by B) condensation and gas-liquid separation; or B) condensation and gas/liquid separation followed by A) membrane separation; wherein H.sub.2S-rich streams generated by separation steps A.fwdarw.B or B.fwdarw.A are returned to the reforming reactor and H.sub.2S-lean streams are jointly treated to further minimize H.sub.2S level, then recover the products H.sub.2 and CH.sub.4 therefrom.

7. The process according to claim 6, comprising: feeding sour natural gas mixed with H.sub.2S-rich recycle streams, and optionally with CO.sub.2, to a H.sub.2S reforming reactor packed with a catalyst; catalytically reforming methane with H.sub.2S in said reactor; either passing the effluent from the reformer reactor through one or more membrane separator(s) to generate one or more permeate streams (rich with H.sub.2S) and one or more retentate streams (lean with H.sub.2S), recycling a permeate stream coming from a downstream membrane separator to the reformer reactor; condensing a retentate coming an upstream membrane separator to recover liquid CS.sub.2 and produce a non-condensable H.sub.2S-rich stream, which is recycled to the reformer reactor, wherein during condensation, a non-condensable H.sub.2S-lean stream is formed prior to the recovery of the liquid CS.sub.2, and is optionally combined with a retentate stream coming from an downstream membrane separator; wherein the H.sub.2S-lean stream, or the combined H.sub.2S-lean stream, is treated to recover H.sub.2 and sweet natural gas therefrom; or vice versa, first condensing the effluent from the reformer reactor to recover liquid CS.sub.2 and produce a non-condensable H.sub.2S-rich stream, which is recycled to the reformer reactor, wherein, during condensation, a non-condensable H.sub.2S-lean stream is formed prior to the recovery of the liquid CS.sub.2; and passing the non-condensable H.sub.2S-lean stream through one or more membrane separator(s) to generate one or more permeate streams and one or more retentate streams, recycling a permeate stream coming from a downstream membrane separator to the reformer reactor; and treating a retentate stream coming from a downstream membrane separator to recover H.sub.2 and sweet natural gas therefrom.

8. The process according to claim 7, wherein H.sub.2S-lean streams generated by the separation methods (A.fwdarw.B or B.fwdarw.A) are jointly treated to recover the products H.sub.2 and CH.sub.4 by removal of residual acidic gases to afford an essentially H.sub.2S-free gas stream, recycling of the acidic gasses to the reformer reactor; optionally reducing CO level by mixing the essentially H.sub.2S-free gas stream with steam under conditions advancing water gas shift reaction; and ultimately, separating H.sub.2 and CH.sub.4 from one another by membrane separation.

9. The process according to claim 1, for converting sour natural gas to sweet natural gas and producing hydrogen and carbon disulfide by H.sub.2S reforming of methane to hydrogen and carbon disulfide, comprising: feeding sour natural gas [1] mixed with H.sub.2S-rich recycle streams [8], [10], [13] and optionally with CO.sub.2 [28], to a H.sub.2S reforming reactor (1) packed with a catalyst; catalytically reforming methane with H.sub.2S in said reactor; directing the reactor effluent [4] into a two-stage membrane unit (2) to separate H.sub.2S-lean retentate [5] from the first stage and H.sub.2S-rich permeate [10] from the second stage; condensing the retentate [5] coming from the first stage to form C.sub.s2-containing condensed component and a first non-condensable component; recycling said H.sub.2S-rich permeate [10] coming from the second stage to the reformer reactor (1); directing H.sub.2S-lean retentate stream [11] coming from the second stage and the first non-condensable component [6] into an absorption unit (5) to separate acidic gas stream [13] and form an essentially H.sub.2S-free, sweet gas product stream [14] comprising methane, carbon monoxide, hydrogen and possibly carbon dioxide; recycling the acidic gas [13] separated from the absorption unit to the reformer reactor (1); recovering liquid CS.sub.2 [7] from the CS.sub.2-containing condensed component, thereby producing a second non-condensable component [8], which contains H.sub.2S and CH.sub.4; recycling the second non-condensable stream [8] back to the reforming reactor (1); feeding the sweet gas stream [14] to a WGS reactor (6) to convert CO and steam [15] into CO.sub.2 and hydrogen; feeding the WGS reactor gas effluent [18] to a membrane to separate hydrogen and CO.sub.2 [19] from the sweet natural gas; and optionally combusting part of the sweet natural gas stream [26] obtained, to supply heat to the reformer reactor; and optionally recycling the CO.sub.2 combustion product to the reformer reactor [28] or supplying it [30] to a plant where CO.sub.2 and hydrogen are converted into liquid hydrocarbons.

10. The process according to claim 1, wherein the catalyst is selected from the group consisting of: i) one or more catalytically active metals on a solid support; ii) one or more catalytically active metals on a solid support, alongside a promoter. iii) a spinel compound, optionally with one or more catalytically active metals dispersed on the surface of the spinel compound, which has the formula (1)
(A.sub.i.sup.2+.sub.i).Math.(B.sub.j.sup.3+.sub.j).sub.2O.sub.4Formula (1) wherein: A.sub.i.sup.2+ is a bivalent metal; B.sub.j.sup.3+ is a trivalent metal; 1i4; 1j4; i+j>3; 0<i1, i=1; 0<j1, Bj=1.

11. The process according to claim 10, wherein the catalyst is selected from the group consisting of: i) molybdenum on a solid support; ii) molybdenum on a solid support, alongside a promoter, which is potassium; iii) a spinel compound of Formula 1 selected from the group consisting of: (A.sub.1.sup.2+).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2).sub.2O.sub.4, (A.sub.1.sup.2+.sub.1A.sub.2.sup.+.sub.2d ).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2).sub.2O.sub.4, (A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3)(B.sub.1.sup.3+.sub.1B.sub.2.sup.3.sub.2).sub.2O.sub.4, (A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2B.sub.3.sup.3+.sub.3).sub.2O.sub.4 and (A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3A.sub.4.sup.2+.sub.4).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2B.sub.3.sup.3+.sub.3).sub.2O.sub.4, wherein the divalent metal A.sub.1.sup.2+ is selected from the group consisting Ni.sup.2+, Co.sup.2+, Cu.sup.2+ and Zn.sup.2+, the trivalent metal B.sub.j.sup.3+ is selected from the group consisting of Fe.sup.3+, Cr.sup.3+ and Al.sup.3+; 0<i1, i=1, 0<j1, j=1, wherein molybdenum is dispersed on the spinel.

12. The process according to claim 11, wherein the catalyst is selected from the group consisting of: i) Mo/-alumina; ii) K-Mo-/-alumina]; and iii) Mo/Ni(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4, Mo/(Ni.sub.0.5Cu.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4, Mo/(Ni.sub.0.5Co.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 and Mo/(Ni.sub.0.5Zn.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4.

13. A spinel compound of Formula 1:
(A.sub.1.sup.2+.sub.1).Math.(B.sub.j.sup.3+.sub.2).sub.2O.sub.4Formula (1) selected from the group consisting of:
(A.sub.1.sup.2+).Math.*B.sub.1.sup.3+.sub.1B.sub.2.sup.3.sub.2).sub.2O.sub.4;
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2).sub.2O.sub.4;
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3 +.sub.2).sub.2O.sub.4;
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2B.sub.3.sup.3+.sub.3).sub.2O.sub.4; and
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3A.sub.4.sup.2+.sub.4).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2B.sub.3.sup.3+.sub.3).sub.2O.sub.4. wherein the divalent metal A.sub.1.sup.2+ is selected from the group consisting Ni.sup.2+, Co.sup.2+, Cu.sup.2+ and Zn.sup.2+, the trivalent metal B.sub.j.sup.3+ is selected from the group consisting of Fe.sup.3+, Cr.sup.3+ and Al.sup.3+; 0<i1, i=1, 0<j1, j=1.

14. A catalyst comprising molybdenum dispersed on the spinel of Formula 1 as defined in claim 13.

15. The catalyst according to claim 14, selected from the group consisting of: Mo/Ni(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4, Mo/(Ni.sub.0.5Cu.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4, Mo/(Ni.sub.0.5Co.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 and Mo/(Ni.sub.0.5Zn.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4.

16. A sol-gel method for preparing a spinel of Formula 1 selected from the group consisting of:
(A.sub.1.sup.2+).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2).sub.2O.sub.4;
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2).sub.2O.sub.4;
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2).sub.2O.sub.4;
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2B.sub.3.sup.3+.sub.3).sub.2O.sub.4; and
(A.sub.1.sup.2+.sub.1A.sub.2.sup.2+.sub.2A.sub.3.sup.2+.sub.3A.sub.4.sup.2+.sub.4).Math.(B.sub.1.sup.3+.sub.1B.sub.2.sup.3+.sub.2B.sub.3.sup.3+.sub.3).sub.2O.sub.4. wherein the divalent metal A.sub.1.sup.2+ is selected from the group consisting Ni.sup.2+, Co.sup.2+, Cu.sup.2+ and Zn.sup.2+, the trivalent metal B.sub.j.sup.3+ is selected from the group consisting of Fe.sup.3+, Cr.sup.3+ and Al.sup.3+; with 0<i1, i=1, 0<j1, j=1, the process comprising dissolving in water Ni, Co, Zn, Cu, Fe, Cr and Al salts to form Ni.sup.2+, Co.sup.2+, Zn.sup.2+, Cu.sup.2+, Fe.sup.3+, Cr.sup.3+ and Al.sup.3+ solution, adding a complexing agent to the salt solution, heating the mixture to 60-90 C. until the gel is formed, and recovering a spinel powder.

17. A process according to claim 16, further comprising the step of loading molybdenum onto the spinel surface by impregnation.

18. An apparatus suitable for converting sour natural gas to sweet natural gas, hydrogen and carbon disulfide, comprising: a reformer reactor (1), packed with a catalyst, supplied by a feed line [1] from a sour natural gas reservoir, optionally by a feed line [2] connected to an external fresh CO.sub.2 source; and by one or more recycle lines; a separation unit (S) connected to the outlet of the reformer reactor (1) through a line [4] equipped with a heat exchanger and a compressor; the separation unit consisting of membrane separator(s) (2), gas-liquid separators arranged in series, with a heat exchanger in the line connecting a pair of adjacent gas-liquid separators (3) and a terminus gas-liquid separator (4); acidic gas removal unit (5), which comprises either an absorption unit filled with a liquid, suitable for separating a gas mixture passing therethrough by dissolving one or more acidic components of the mixture, or a membrane separator; wherein the acidic gas removal unit (5) is supplied by one or more feed lines from the separation unit (S), and is connected by a recycle line [13] to the reformer reactor (1) and through a product delivery line [14] to a WGS reactor (6); one or more WGS reactors in series (6), wherein the first WGS reactor is supplied with a steam feed line [15] and a feed line [14] that is connected to the outlet of the acidic gas removal unit (5), to deliver one or more gas components which were not captured in the acidic gas removal unit, to said first WGS reactor; hydrogen separation membrane unit (7), configured to receive a non-condensable component of the effluent of the WGS reactor, or of the last WGS reactor is said series of WGS reactors, wherein the permeate side of said hydrogen separation membrane unit (7) is connected [19 ] to a plant suitable for producing liquid hydrocarbons from hydrogen and CO.sub.2; such that hydrogen and CO.sub.2-containing permeate generated in said membrane can be used as a feed material in production of liquid hydrocarbons in said plant; optionally a combustion chamber (8), connected [20, 26] to the retentate side of said hydrogen separation membrane unit (7), to receive CH.sub.4-containing stream, wherein the combustion chamber is supplied by an oxygen feed line [27], wherein the combustion chamber is linked to the reformer reactor to supply heat by radiation and convection, and deliver CO.sub.2 combustion product [28] to the inlet of said reactor or as a feed material in production of liquid hydrocarbons in said plant; optionally an WGS reactor connected [20, 21] to the retentate side of said hydrogen separation membrane unit (7), to receive CH.sub.4 and CO-containing stream, wherein the WGS reactor is supplied with a steam feed line [22], with gas-liquid separator placed downstream of said WGS reactor to recover sweet natural gas [25] and water [24]; wherein the separation unit (S) consists of: A) a single or multistage membrane separator(s) (2); B) n gas-liquid separators positioned in series (3.sub.1, . . . , 3.sub.n; n2; e.g., 3n7), wherein lines delivering condensates from said gal-liquid separators (3.sub.1, . . . , 3.sub.n) are joined to provide a feed line for the terminus gas-liquid separator (4) which is configured to operate under atmospheric pressure, wherein the liquid discharge line [7] of said terminus gas-liquid separator (4) is connected to a storage tank for holding CS.sub.2, with a recycle line [8] connecting the gas outlet of said terminus gas-liquid separator (4) to the reformer reactor (1); wherein either A is upstream of B, in which case: the gas-liquid separator (3.sub.n) is connected [6] by a pipe to supply non-condensable matter to acidic gas removal unit (5); and when A) consists of a single membrane separator (2), then the retentate side of said single membrane separator is connected to the inlet of the first gas-liquid separator (3.sub.1), and the permeate side of said single membrane separator (2) is connected to the reformer reactor; or when A) consists of a multistage membrane separator (2), then the retentate and permeate sides of the first stage membrane separator are connected to the inlet of the first gas-liquid separator (31) and to a second stage membrane separator, respectively, and for any stage other than the first stage, the permeate side is connected by recycle line [10] to the reformer reactor (1) and the retentate side is either connected to the next stage or, in case of the last stage, to an acidic gas removal unit (5) via pipe [11]; or A is downstream to B, in which case then the gas-liquid contactor (3.sub.n) is connected by a pipe to supply non-condensable matter to a single or multistage membrane separator(s) (2).

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0069] FIG. 1 displays block diagram for sour natural gas processing adopted from Mansi S. Shah, Michael Tsapatsis and J. Ilja Siepmann, Hydrogen Sulfide Capture: From Absorption in Polar Liquids to Oxide, Zeolite, and Metal-Organic Framework Adsorbents and Membranes, Chem. Rev. 2017, 117, 9755-9803.

[0070] FIG. 2 displays the thermodynamic analysis of hydrogen sulfide reforming with methane using CHEMCAD software at 1 bar from 700 to 1000 C. with inlet feed ratio of H.sub.2S/CH.sub.40.6 and CO.sub.2/CH.sub.4=0.3 with products CS.sub.2, H.sub.2 and CO.

[0071] FIG. 3 displays the design of the process of the invention.

[0072] FIG. 4 depicts a schematic description of an experimental set up for H.sub.2S reforming of methane.

[0073] FIG. 5 displays the XRD patterns of the CrNiFeO.sub.4 catalyst sample.

[0074] FIG. 6 displays the XRD patterns of the CrNiCuFeO.sub.4 catalyst sample.

[0075] FIG. 7 displays the XRD patterns of the CrNiCoFeO.sub.4 catalyst sample.

[0076] FIG. 8 displays the XRD patterns of the CrNiZnFeO.sub.4 catalyst sample.

DETAILED DESCRIPTION

[0077] Conventional wide-angle XRD patterns were measured with a Panalytical Empyrean Powder Diffractometer equipped with position sensitive detector X'Celerator fitted with a graphite monochromator, at 40 kV and 30 mA and analyzed using software developed by Crystal Logic. The phase identification was performed by using an SBDE ZDS computer search/match program coupled with the International Center for Diffraction Data (ICDD). BET was measured by NOVA 3200e Quantachrome adsorption analyzer.

Preparation 1

Mo/-Al.SUB.2.O.SUB.3 .(20 wt. % MoO.SUB.3.)

[0078] Mo/-Al.sub.2O.sub.3 catalyst was prepared by incipient wetness impregnation. 8 g of -Al.sub.2O.sub.3 support (NORTON, SA6175, extrudates, 230-290 m.sup.2/g) were calcined at 500 C. for 2 h prior to impregnation. After calcination the support was held under vacuum for 1 h and further impregnated with solution of 2.454 g (NH.sub.4).sub.6Mo.sub.7O.sub.24.Math.4H.sub.2O in 4.25 g H.sub.2O and 1.5 ml NH.sub.4OH 25%. The material was dried at room temperature for 24 h. Next, the catalyst was dried at 120 C. for 12 h and calcined at 550 C. for 4 h (3 C./min).

Preparation 2

K-Mo/-Al.SUB.2.O.SUB.3 .(20 wt. % MoO.SUB.3., 5 wt. % K)

[0079] K-Mo/-Al.sub.2O.sub.3 catalyst was prepared by incipient wetness impregnation in two steps. At first step Mo/-Al.sub.2O.sub.3 material was prepared according to previous synthesis (Preparation 1). After that, the 10.67 g of obtained material was held under vacuum for 1 h and further impregnated with solution of 0.988 g K.sub.2CO.sub.3 in 5.85 g H2O. The catalyst was dried at 120 C. overnight and calcined at 500 C. for 2 h (5 C./min). BET surface area was 166 m.sup.2/g.

Preparation 3

Mo/Ni(Fe.SUB.0.5.Cr.SUB.0.5.).SUB.2.O.SUB.4 .(5 wt. % MoO.SUB.3.)

[0080] Ni(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was synthesized by the sol-gel method. The metal salt precursors were dissolved separately in 10 ml H.sub.2O each: 8.591 g Cr (NO.sub.3).sub.3.Math.9H.sub.20; 6.570 g Ni(NO.sub.3).sub.2.Math.6H.sub.2O; 9.128 g Fe(NO.sub.3).sub.3.Math.9H.sub.2O. Once fully dissolved, the metal precursors were mixed and 32.566 g of citric acid (complexant) was added to the solution (the ratio of moles complexant to total moles of metal ions was 2.5). Then the mixed solution was heated to 80 C. on a hot plate until the gel was formed. The material was dried overnight at 110 C., calcined in air at 200 C. (10 C./min) for 2 h and then at 700 C. (5 C./min) for 4 h. X-ray powder diffraction is shown in FIG. 5. BET surface area was 17 m.sup.2/g.

[0081] 4.61 g of Ni(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was held under vacuum for 1 h and impregnated with solution of 0.298 g (NH.sub.4).sub.6Mo.sub.7O.sub.24.Math.4H.sub.2O in 3.24 g H.sub.2O and 0.18 ml NH.sub.4OH 25%. The material was dried at room temperature for 24 h. After that the catalyst was dried at 120 C. for 12 h and calcined at 550 C. for 4 h (3 C./min).

Preparation 4

Mo/(Ni.SUB.0.5.Cu.SUB.0.5.)(Fe.SUB.0.5.C.SUB.0.5.).SUB.2.O.SUB.4 .(5 wt. % MoO.SUB.3.)

[0082] (Ni.sub.0.5Cu.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was synthesized by the sol-gel method. The metal salt precursors were dissolved separately in 10 ml H.sub.2O each: 8.591 g Cr(NO.sub.3).sub.3.Math.90.sub.H2O; 3.286 g Ni(NO.sub.3).sub.2.Math.6H.sub.2O; 9.128 g Fe(NO.sub.3).sub.3.Math.9H.sub.2O; 2.730 g Cu(NO.sub.3).sub.2.Math.3H.sub.2O. Once fully dissolved, the metal precursors were mixed and 32.566 g of citric acid (complexant) was added to the solution (the ratio of moles complexant to total moles of metal ions was 2.5). Then the mixed solution was heated to 80 C. on a hot plate until the gel was formed. The material was dried overnight at 110 C., calcined in air at 200 C. (10 C./min) for 2 h and then at 700 C. (5 C./min) for 4 h. X-ray powder diffraction is shown in FIG. 6.

[0083] 4.66 g of (Ni.sub.0.5Cu.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was held under vacuum for 1 h and impregnated with solution of 0.286 g (NH.sub.4).sub.6Mo.sub.7O.sub.24.Math.4H.sub.2O in 2.88 g H.sub.2O and 0.18 ml NH.sub.4OH 25%. The material was dried at room temperature for 24 h. After that the catalyst was dried at 120 C. for 12 h and calcined at 550 C. for 4 h (3 C./min).

Preparation 5

Mo/(Ni.SUB.0.5.Co.SUB.0.5.)(Fe.SUB.0.5.Cr.SUB.0.5.).SUB.2.O.SUB.4 .(5 wt. % MoO.SUB.3.)

[0084] (Ni.sub.0.5Co.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was synthesized by the sol-gel method. The metal salt precursors were dissolved separately in 10 ml H.sub.2O each: 8.591 g Cr(NO.sub.3).sub.3.Math.9H.sub.2O; 3.286 g Ni(NO.sub.3).sub.2.Math.6H.sub.2O; 9.128 g Fe(NO.sub.3).sub.3.Math.9H.sub.2O; 3.288 g Co(NO.sub.3).sub.2.Math.6H.sub.2O. Once fully dissolved, the metal precursors were mixed and 32.566 g of citric acid (complexant) was added to the solution (the ratio of moles complexant to total moles of metal ions was 2.5). Then the mixed solution was heated to 80 C. on a hot plate until the gel was formed. The material was dried overnight at 110 C., calcined in air at 200 C. (10 C./min) for 2 h and then at 700 C. (5 C./min) for 4 h. X-ray powder diffraction is shown in FIG. 7.

[0085] 3.58 g of (Ni.sub.0.5Co.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was held under vacuum for 1 h and impregnated with solution of 0.219 g (NH.sub.4).sub.6Mo.sub.7O.sub.24.Math.4H.sub.2O in 1.58 g H20 and 0.11 ml NH4OH 25%. The material was dried at room temperature for 24 h. After that the catalyst was dried at 120 C. for 12 h and calcined at 550 C. for 4 h (3 C./min).

Preparation 6

Mo/(Ni.SUB.0.5.Zn.SUB.0.5.)(Fe.SUB.0.5.Cr.SUB.0.5.).SUB.2.O.SUB.4 .(5 wt. % MoO.SUB.3.)

[0086] (Ni.sub.0.5Zn.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was synthesized by the sol-gel method. The metal salt precursors were dissolved separately in 10 ml H2O each: 8.591 g Cr(NO.sub.3).sub.3.Math.9H.sub.2O; 3.286 g Ni(NO.sub.3).sub.2.Math.6H.sub.2O; 9.128 g Fe(NO.sub.3).sub.3.Math.9H.sub.2O; 2.480 g Zn(CH.sub.3COO).sub.2.Math.2H.sub.2O. Once fully dissolved, the metal precursors were mixed and 32.566 g of citric acid (complexant) was added to the solution (the ratio of moles complexant to total moles of metal ions was 2.5). Then the mixed solution was heated to 80 C. on a hot plate until the gel was formed. The material was dried overnight at 110 C., calcined in air at 200 C. (10 C./min) for 2 h and then at 700 C. (5 C./min) for 4 h. X-ray powder diffraction is shown in FIG. 8.

[0087] 4.79 g of (Ni.sub.0.5Zn.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 material was held under vacuum for 1 h and impregnated with solution of 0.293 g (NH.sub.4).sub.6Mo.sub.7O.sub.24.Math.4H.sub.2O in 4.23 g H.sub.2O and 0.23 ml NH.sub.4OH 25%. The material was dried at room temperature for 24 h. After that the catalyst was dried at 120 C. for 12 h and calcined at 550 C. for 4 h (3 C./min).

Examples 1 and 2

H.SUB.2.S Reforming of Methane with Complete Conversion of CO.SUB.2 .in a Fixed Bed Reactor

[0088] A schematic description of the experimental set-up used for running the H.sub.2S reforming of methane is depicted in FIG. 4. Catalyst activation was done by in-situ sulfidation at temperature of 530 C. and atmospheric pressure in reactor (11) at 200 mL min.sup.1 flow of 20 vol % H.sub.2S/N.sub.2 gas for 1 hour. The gaseous reactants are controlled by Brooks mass flow controllers (FC).

[0089] Methane was contacted with H.sub.2S and CO.sub.2 by passing a mixture of CH.sub.4, H.sub.2S and CO.sub.2 streams (indicated by numerals [101], [102] and [103], respectively) at a molar ratio H.sub.2S/CH.sub.4 and CO.sub.2/CH.sub.4 of 0.6 and 0.3, respectively, through a tubular reactor (11) (11 mm ID, 600 mm long) made of alumina, packed with 1.5 gram of the catalyst powder of Preparation 1 (Mo/-Al.sub.2O.sub.3) or 0.75 gram of the catalyst powder of Preparation 2 (K-Mo/-Al.sub.2O.sub.3) and 4 gram of quartz powder and heated up to 900 C. at a total pressure of 1 atm (Examples 1 and 2, respectively). All gaseous reactants are fed via line [106] to the reactor (11).

[0090] The reaction products are cooled down to 150 C. with the aid of an electric heater (12) to separate and capture sulfur residues, which may form in the H.sub.2S decomposition reaction. With the aid of a cooler (13), the gaseous products [108] were cooled down to 5 C. The gaseous products [109] flow in line [110] to GC analyzer or to an absorption column (14) containing paraffinic solvent to absorb most of the CS.sub.2 produced in the reformer (11). The effluent gas stream [112] containing H.sub.2S, CS.sub.2, CH.sub.4, CO.sub.2, CO and H.sub.2 is fed into two scrubber vessels in series (15) containing 2 L of sodium hydroxide solution, to remove H.sub.2S, CO.sub.2 and CS.sub.2 effectively.

[0091] The exhaust components [113] flowing in line [114] were analyzed in online Agilent 7890A Series Gas Chromatograph (GC) equipped with 7 columns and 5 automatic valves using helium as a carrier gas. The flow rate was measured by Alicat mass flow meter (FI).

[0092] In the tables below, the capital letters X and S stand for conversion and selectivity, respectively. The selectivity towards H.sub.2S reforming reaction was calculated as S.sub.H2S_reforming=[(X.sub.H2S(reforming)*/2)/X.sub.CH4], where is the H.sub.2S/CH.sub.4 molar ratio at feed.

[0093] The reaction of H.sub.2S (H.sub.2S reforming) and CO.sub.2 (dry reforming) with CH.sub.4 in reactor (11) to produce H.sub.2, CO and CS.sub.2 was run under specific conditions at close to equilibrium conversions: Temperature of 900 C., total pressure of 1 atm, H.sub.2S/CH.sub.4=0.6 mol/mol and CO.sub.2/CH.sub.4=0.3 mol/mol. Results are shown in Table 2.

TABLE-US-00003 TABLE 2 Time on WHSV.sub.H2S, X.sub.CH4, X.sub.H2S; X.sub.CO2, Example Catalyst stream, h h.sup.1 % % % S.sub.H2S.sub..sub.reforming 1 Mo/-Al.sub.2O.sub.3 50 2.0 43.2 45.8 100.0 31.8 2 K-Mo/-Al.sub.2O.sub.3 100 4.0 43.5 46.7 100.0 32.2

Examples 3-5

H.SUB.2.S Reforming of Methane with Low Conversion of CO.SUB.2 .in a Fixed Bed Reactor

[0094] This experiment was conducted in an experimental unit with a similar design as in Examples 1-2, schematically described in FIG. 4. The tubular reactor (11) (11 mm ID, 600 mm long) was packed with 2 grams of the catalyst powder of Preparation 3 (Mo/Ni (Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4) or 1.5 gram of Preparation 6 (Mo/(Ni.sub.0.05Zn.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4) and 5 gram of quartz powder.

[0095] CO.sub.2 [103] and H.sub.2S [102] streams were contacted with CH.sub.4 [101] to form a feed mixture [106] containing H.sub.2S/CH4 and CO.sub.2/CH.sub.4 in a molar ratio of 0.4-0.6 and 0.08-0.30, respectively. CO.sub.2 was partially reacting with CH.sub.4 and H.sub.2 in the dry reforming and RWGS reactions, respectively.

[0096] The reaction was run under the following specific conditions: [0097] Temperature 900 C. and total pressure of 1 atm. Conditions and results are shown in Table 3.

TABLE-US-00004 TABLE 3 Time on Stream CO.sub.2/CH.sub.4 H.sub.2S/CH.sub.4 WHSV.sub.H2 X.sub.CH4 X.sub.H2S X.sub.CO2 Ex. Catalyst (h) mol/mol mol/mol h.sup.1 % % % S.sub.H2S.sub..sub.reforming 3 Mo/Ni(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 45 0.30 0.6 0.6 13.5 30.0 11.0 66.7 4 Mo/Ni(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 165 0.15 0.6 1.3 9.8 29.2 3.0 89.7 5 Mo(Ni.sub.0.5Zn.sub.0.5)(Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4 45 0.08 0.4 0.9 8.0 25.1 25.0 62.8

Example 6

H.SUB.2.S Reforming of Methane Mixed with CO.SUB.2 .and H.SUB.2 .in a Fixed Bed Reactor

[0098] This experiment was conducted in an experimental unit with a similar design as in Examples 1-2 schematically described in FIG. 4. The tubular reactor (11) (11 mm ID, 600 mm long) was packed with 1.5 grams of the catalyst powder of Preparation 1 (Mo/-Al.sub.2O.sub.3) and 4 gram of quartz powder.

[0099] H.sub.2S [102], CO.sub.2 [103] and H.sub.2 [104] streams were contacted with CH.sub.4 [101] to evaluate the performance of the projected gas composition with hydrogen at feed mixture [106].

[0100] The reaction was run under the following specific conditions: [0101] WHSV.sub.H2S=2.0 h.sup.1, temperature 900 C., total pressure of 1 atm, 8% v/v H.sub.2, H.sub.2S/CH.sub.4=0.6 mol/mol and CO.sub.2/CH.sub.4=0.3 mol/mol in the feed. The time on stream was 70 hours. The results are shown in Table 4.

TABLE-US-00005 TABLE 4 X.sub.CH4, % X.sub.H2S, % x.sub.CO2, % S.sub.H2S.sub..sub.reforming, % 38.0 40.0 86.6 31.6

Example 7

H.SUB.2.S Reforming of Methane Without CO.SUB.2 .at Feed in a Fixed Bed Reactor

[0102] This experiment was conducted in an experimental unit with a similar design as in Examples 1-2 schematically described in FIG. 4. The tubular reactor (11) (11 mm ID, 600 mm long) was packed with 2 grams of the catalyst powder of Preparation 3 (Mo/Ni (Fe.sub.0.5Cr.sub.0.5).sub.2O.sub.4) and 5 gram of quartz powder.

[0103] H.sub.2S [102] stream was contacted with CH.sub.4 [101] to form a feed mixture [106] containing H.sub.2S/CH.sub.4 in a molar ratio of 0.6, without CO.sub.2 in feed.

[0104] The reaction was run under the following specific conditions: [0105] WHSV.sub.H2S=0.6 h.sup.1, temperature 900 C., total pressure of 1 atm, H.sub.2S/CH.sub.4=0.6 mol/mol in the feed. The time on stream was 75 hours. The results are shown in Table 5.

TABLE-US-00006 TABLE 5 X.sub.CH4, % X.sub.H2S,% 12.8 39.5

[0106] While the present disclosure has been illustrated and described with respect to a particular embodiment thereof, it should be appreciated by those of ordinary skill in the art that various modifications to this disclosure may be made without departing from the spirit and scope of the present disclosure.