Methods for producing syngas from H2S and CO2 in an electrochemical cell

Abstract

The present application provides systems, apparatuses, and methods for simultaneous processing of tow waster gases, namely H.sub.2S and CO.sub.2. In an exemplary process of this disclosure H.sub.2S is supplied to anode side of an electrochemical cell, while CO.sub.2 is supplied to the cathode side. As a result, valuable commercial products are produced. In particular, SO.sub.2 is harvested from the anode side, while synthesis gas, CO+H.sub.2) is harvested from the cathode side. An electric current is also produced, which can be supplied to a local utility grid.

Claims

1. A method for producing syngas and SO.sub.2 from H.sub.2S, CO.sub.2, and H.sub.2O in an electrochemical cell comprising an anode, a cathode, and a conductive membrane positioned between and in electrochemical contact with the anode and the cathode, the method comprising: contacting the anode of the electrochemical cell with a stream comprising H.sub.2S and H.sub.2O to produce a stream comprising SO.sub.2; and contacting the cathode of the electrochemical cell with a stream comprising CO.sub.2 and H.sub.2O to produce a stream comprising syngas.

2. The method of claim 1, wherein contacting the anode and contacting the cathode occur simultaneously.

3. The method of claim 1, further comprising collecting the stream comprising SO.sub.2 from the anode side of the electrochemical cell.

4. The method of claim 1, further comprising collecting the stream comprising the syngas from the cathode side of the electrochemical cell.

5. The method of claim 1, wherein the stream comprising H.sub.2S and H.sub.2O is a gas.

6. The method of claim 5, wherein the pressure of the stream is from about 1 bar to about 20 bar.

7. The method of claim 5, wherein the temperature of the stream is from about 100° C. to about 1,500° C.

8. The method of claim 5, wherein molar ratio of H.sub.2S to H.sub.2O in the stream is from about 0.1:1 to about 10:1.

9. The method of claim 5, wherein temperature of the stream is from about 700° C. to about 1,000° C.

10. The method of claim 1, wherein the anode material comprises WS.sub.2, CoS.sub.1.035 or Li.sub.2S.

11. The method of claim 1, wherein the stream comprising CO.sub.2 and H.sub.2O is a gas.

12. The method of claim 11, wherein the pressure of the stream is from about 1 bar to about 20 bar.

13. The method of claim 11, wherein the temperature of the stream is from about 100° C. to about 1,500° C.

14. The method of claim 11, wherein molar ratio of CO.sub.2 to H.sub.2O in the stream is from about 0.1:1 to about 10:1.

15. The method of claim 11, wherein temperature of the stream is from about 700° C. to about 1,000° C.

16. The method of claim 1, wherein the cathode material comprises a perovskite material of the general type La.sub.1-xSr.sub.xCr.sub.1-yM.sub.yO.sub.3, where M is a metal selected from Mn, Fe, Co, and Ni.

17. The method of claim 1, wherein the conductive membrane comprises a material selected from yttria-stabilized zirconia (YSZ), scandia stabilized zirconia (ScSZ), gadolinium doped ceria (GDC), lanthanum strontium cobalt ferrite (LSCF), Sr-doped La manganites (LSM), and ferrites-nickelates (LSFN).

18. The method of claim 1, wherein molar ratio of H.sub.2S to CO.sub.2 in the electrochemical cell is from about 0.1:1 to about 10:1.

19. The method of claim 1, wherein molar ratio of CO to H.sub.2 in the syngas is from about 1:1 to about 1:5.

20. The method of claim 1, wherein the syngas comprises no more than from about 0.5 wt. % to about 10 wt. % of CO.sub.2 or H.sub.2O, or a combination thereof.

Description

DESCRIPTION OF DRAWINGS

[0028] FIG. 1 is a schematic description of the electrochemical process of producing SO.sub.2, CO, and H.sub.2 from H.sub.2S, CO.sub.2, and H.sub.2O.

DETAILED DESCRIPTION

[0029] Generally, the present disclosure related to systems, apparatuses, and methods to effectively react waste gases CO.sub.2 and H.sub.2S, in the presence of H.sub.2O, to produce syngas (a mixture of mainly CO and H.sub.2), SO.sub.2, and a direct electric current, all of which are valuable industrial products. In one aspect, the disclosure provides an electrochemical cell, which includes an anode, a cathode, and a conductive membrane positioned between and in electrochemical contact with the anode and the cathode. The disclosure further provides a method of using said electrochemical cell to produce SO.sub.2, syngas, extra H.sub.2, and an electric current, from CO.sub.2, H.sub.2S, and H.sub.2O. Certain embodiments of the aforementioned electrochemical cell and methods are described herein.

[0030] FIG. 1 schematically shows the electrochemical cell and the process within the present claims. Referring to FIG. 1, the electrochemical cell 100 includes an anode 102, a cathode 104, and a conductive hybrid membrane 106. The cell 100 also includes a “fuel” stream feed channel 108 through which the fuel stream consisting mainly of H.sub.2S and H.sub.2O may be supplied to the anode 102 side. Simultaneously, a feed stream 118 of an “oxidizer” consisting mainly of CO.sub.2 and H.sub.2O may be supplied to the cathode 104 side of the cell through the oxidizer feed channel 116. Upon contacting the anode, H.sub.2S and water in the fuel feed stream undergo the following oxidation reaction:

2H.sub.2S+2H.sub.2O+2O.sup.2−.fwdarw.2SO.sub.2+8H.sup.++12e.sup.−

[0031] In essence, the oxygen ions O.sup.2− that have migrated to the surface of the anode 102 from the cathode 104 through the membrane 106 (see 122 in FIG. 1) oxidize the fuel to produce SO.sub.2, hydrogen ions H.sup.+, as well as the electric current (a number of e.sup.−). The stream of gaseous SO.sub.2 114 being produced in this reaction can be harvested from the anode 102 side of the cell 100 through the outlet channel 114. In the meantime, the H.sup.+ produced in the oxidation reaction migrate through the conductive membrane 106 from the anode 102 to the cathode 104 side of the cell 100 (see 120 in FIG. 1). The electric current that is produced in the oxidation reaction also flows through the electrically conductive hybrid membrane from anode 102 to cathode 104 (flow of elections not shown). At the cathode 104 side of the membrane, CO.sub.2 and water supplied through 116, along with the H.sup.+ ions that migrated from the anode side (see 120), and with the aid of the electric current produced on the anode 102 side, undergo the following cascade of reduction reactions:

CO.sub.2+2e.sup.−.fwdarw.CO+O.sup.2−  (1)

H.sub.2O+2e.sup.−.fwdarw.H.sub.2+O.sup.2−  (2)

8H.sup.++8e.sup.−.fwdarw.4H.sub.2  (3)

[0032] In essence, the CO.sub.2 and the H.sub.2O are electrolyzed by the electric current to produce syngas, a gaseous mixture of CO and H.sub.2. The oxygen anions O.sup.2− that are produced in reactions (1) and (2) become the oxidizing reagent when those anions migrate to the anode 102 side (see 122). The H.sup.+ cations are also reduced by the electric current to supply an additional amount of molecular gaseous H.sub.2 to the syngas mixture. The syngas 126, including the extra H.sub.2, can be collected rom the cathode side of the cell 100 through the outlet channel 124. In addition, the electric current produced on the anode side, depending on the flow rates of streams 110 and 118, instead of reducing CO.sub.2 and H.sub.2O to produce syngas, can be diverted in 128 and supplied to a local utility grid (the electric current 128 is DC, and may be converted to AC before being supplied to the users of electricity).

[0033] Accordingly, the present disclosure provides a method of reacting H.sub.2S and CO.sub.2, a method of co-processing H.sub.2S and CO.sub.2, or a method of producing syngas (CO and H.sub.2) and SO.sub.2 from H.sub.2S, CO.sub.2, and H.sub.2O. The method generally includes an electrochemical cell containing an anode, a cathode, and a conductive membrane positioned between and in electrochemical contact with the anode and the cathode. The method further includes contacting the anode of the electrochemical cell with a stream consisting mainly of H.sub.2S and H.sub.2O. In one example, this contacting leads to producing a stream consisting mainly of SO.sub.2 on the anode side of the electrochemical cell. The method may further include collecting (e.g., harvesting) the stream of SO.sub.2 for further use. Additionally, the method further includes contacting the cathode of the electrochemical cell with a stream consisting mainly of CO.sub.2 and H.sub.2O to produce a stream containing mainly syngas (CO and H.sub.2). The method may also include collecting (e.g., harvesting) the stream of syngas for further use. In some embodiments, contacting the anode with H.sub.2S and contacting the cathode with CO.sub.2 occur simultaneously.

[0034] The anode side of the electrochemical cell is generally operated in a manner applicable to operation of a fuel cell, for example, a solid oxide fuel cell (“SOFC”). In this arrangement, the H.sub.2S is oxidized at the anode to produce electric current, where the electricity in the form of a direct current of electrons is moving through the electrically conductive electrolyte of the conductive hybrid membrane (as discussed above with reference to FIG. 1).

[0035] Generally, the anode is made of a solid electrolyte material and is either in direct contact with the electrolyte of the hybrid membrane, or is connected to the conductive membrane material through an interconnect layer, such as a metallic or ceramic layer. Suitable examples of anode materials include pure metals, metal sulfides, metal oxides, yttria-stabilized zirconia (YSZ), or any combination thereof. Suitable examples of metal sulfides include thiospinels, such as WS.sub.2, CoS.sub.1.035 or Li.sub.2S. Suitable examples of metal oxides include LiCoO.sub.2, V.sub.2O.sub.5, NiO, LaSrMnO.sub.6, CeO.sub.2, Y.sub.2O.sub.3, La.sub.2O.sub.3, MgO, and TiO.sub.2. Other suitable anode materials include metallic Ru, Cu, Co, Ni, Pt, or Ag, or any combination thereof. Other examples of anode materials include perovskite and chromite (La.sub.0.8Sr.sub.0.2Cr.sub.0.5Mn.sub.0.5O.sub.3). Any anode material generally known to be useful in SOFC operation may be used in the electrochemical cell of this disclosure. Anode layers in the cells of this disclosure may be of various thickness ranging from about 1 nm to about 1 cm, or more, depending on the needs, the scale, and the output of the process.

[0036] The stream containing H.sub.2S and H.sub.2O can generally be a liquid phase or a gas phase. When the stream is a liquid, an aqueous solution of H.sub.2S in water, the concentration of H.sub.2S may be from about 0.01M to about 1M. In one example, the stream is a saturated solution of H.sub.2S in water at the operating temperature. When the stream is a gas, it may be applied to the anode side of the electrochemical cell at a pressure from about 1 bar to about 20 bar, from about 1 bar to about 15 bar, from about 1 bar to about 10 bar, or from about 1 bar to about 5 bar. In some embodiments, the pressure of the gaseous stream containing H.sub.2S and H.sub.2O is about 1 bar, about 2 bar, about 3 bar, about 5 bar, or about 10 bar. The temperature of the H.sub.2S stream is generally a high operating temperature. For example, the operating temperature on the anode side of the cell may be from about 100° C. to about 1,500° C., from about 200° C. to about 1,200° C., from about 400° C. to about 1,100° C., from about 500° C. to about 1,200, or from about 700° C. to about 1,000° C. Any suitable molar ratio of H.sub.2S to H.sub.2O may be used in this fuel stream. In some embodiments, molar ratio of H.sub.2S to H.sub.2O in the fuel stream is about 0.1:1, about 0.5:1, about 1:1, about 1:2, about 1:5, or about 1:10.

[0037] Generally, the cathode in the electrochemical cell is made of a solid electrolyte material and is either in direct contact with the electrolyte of the hybrid membrane, or is connected to the membrane material through an interconnect layer, such as a metallic or ceramic layer. Suitable examples of cathode materials include lanthanum strontium manganite (“LSM”), conductive ceramics, or perovskite. In one example, the cathode material is a perovskite material of the general type La.sub.1-xSr.sub.xCr.sub.1-yM.sub.yO.sub.3, where M is a metal selected from Mn, Fe, Co, and Ni. Any cathode material generally known to be useful in CO.sub.2 electrolysis (including high-temperature electrolysis) maybe used in the electrochemical cell of this disclosure. Cathode layers in the cells of this disclosure may be of various thickness ranging from about 1 nm to about 1 cm, or more, depending on the needs, the scale, and the output of the process. The cathode material may be selected to operate at high temperatures, for example, from about 500° C. to about 1,500° C., or from about 800° C. to about 1,200° C.

[0038] The stream containing CO.sub.2 and H.sub.2O can generally be a liquid phase or a gas phase. When the stream is a liquid, an aqueous solution of CO.sub.2 in water, the concentration of CO.sub.2 may be from about 0.01M to about 1M. In one example, the stream is a saturated solution of CO.sub.2 in water at the operating temperature. When the stream is a gas, it may be applied to the cathode side of the electrochemical cell at a pressure from about 1 bar to about 20 bar, from about 1 bar to about 15 bar, from about 1 bar to about 10 bar, or from about 1 bar to about 5 bar. In some embodiments, the pressure of the gaseous stream containing CO.sub.2 and H.sub.2O is about 1 bar, about 2 bar, about 3 bar, about 5 bar, or about 10 bar. The temperature of the CO.sub.2 stream is generally a high operating temperature. For example, the operating temperature on the cathode side of the cell may be from about 100° C. to about 1,500° C., from about 200° C. to about 1,200° C., from about 400° C. to about 1,100° C., from about 500° C. to about 1,200, or from about 700° C. to about 1,000° C. Any suitable molar ratio of CO.sub.2 to H.sub.2O may be used in this oxidizer stream. In some embodiments, molar ratio of CO.sub.2 to H.sub.2O in the oxidizer stream is about 0.1:1, about 0.5:1, about 1:1, about 1:2, about 1:5, or about 1:10.

[0039] In a general aspect, the electrochemical cell of this disclosure contains a hybrid conductive membrane between the anode and the cathode. The membrane is hybrid in that it is both ion-conductive and electrically conductive. For example, the ion-conductive membrane may allow a simultaneous free flow of hydrogen cation (H.sup.+), oxygen anion (O.sup.2−), as well as the other ions between the anode and the cathode (as discussed for FIG. 1 discussed above). At the same time, the membrane is electrically conductive, allowing a direct electric current (unidirectional flow of electrons) from the anode to the cathode through the membrane. The membrane may be water-permeable, partially water-permeable, or water-impermeable. In one example, the conductive membrane may be a single layer. In another example, the conductive membrane may have a multilayered structure, where each layer contains a different conductive material. The membrane may contain, for example, a layer of a liquid electrolyte, such as a NaCl solution, in between the two layers of solid electrolytes. The membrane may also have a segmented structure, where each of the segments is selectively conductive for one ion. In one example, the membrane may contain two segments: a segment selectively conductive for H.sup.+ and a segment selectively conductive for O.sup.2−, where each segment is made from an electrically conductive material. In another example, the membrane may contain three separate segments: s segment selectively conductive for H.sup.+, a segment selectively conductive for O.sup.2−, and an electrically conductive segment (allowing flow of e.sup.− from anode to cathode) which is not conductive to H.sup.+ and O.sup.2−. Examples of mixed solid ion conductive electrolytes of the hybrid membrane include a dense layer of ceramic capable or conducting oxygen ions, yttria-stabilized zirconia (YSZ), scandia stabilized zirconia (ScSZ) (e.g., about 9 mol,% Sc.sub.2O.sub.3—9ScSZ), gadolinium doped ceria (GDC), lanthanum strontium cobalt ferrite (LSCF), Sr-doped La manganites (LSM), and ferrites-nickelates (LSFN). Some examples of hybrid materials include CaO, ZrO, and TiO, and combinations thereof. Other examples include BaZr.sub.0.4Ce.sub.0.4Y.sub.0.1Yb.sub.0.1 (BZCYYb—4411), BaZr.sub.0.4Ce.sub.0.4Y.sub.0.1Yb.sub.0.103-d, and BaZr.sub.0.1Ce.sub.0.7Y.sub.0.1Yb.sub.0.1 (BZCYYb1711), or a combination thereof. The membrane material may be chosen to withstand the high temperature operating conditions from about 700° C. to about 1,000° C. In some embodiments, electric conductivity of the hybrid membrane is from about 10.sup.−1 S/m to about 10.sup.8 S/m (Siemens per meter). For example, electric conductivity of the hybrid membrane at the operating conditions (such as high temperature) is about 10.sup.2 S/m, about 10.sup.4 S/m, about 10.sup.6 S/m, or about 10.sup.7 S/m.

[0040] In some embodiments, molar ratio of H.sub.2S to CO.sub.2 in the electrochemical cell is from about 0.1:1 to about 10:1. For example, the molar ratio of H.sub.2S to CO.sub.2 is about 1:10, about 1:2, about 1:1, about 1:2, about 1:5, or about 1:10. In some embodiments, the flow of H.sub.2S to anode and the flow of CO.sub.2 to cathode may be selected such that instead of a syngas, an electric current is produced and harvested to a local utility grid. In one example, the electric current produced from the electrochemical cell is from about 50 W to about 100 MW. In another example, the electric current produced in the cell is from about 1 A to about 1,000 A, or from about 1 A to about 100 A. In yet another example, the electric current is from about 1 V to about 300 V, or from about 50 V to about 250 V.

[0041] In some embodiments, the stream containing SO.sub.2 collected from the anode side of the electrochemical cell is substantially pure. In one example, the stream comprises no more than from about 0.5 wt. % to about 10 wt. % of H.sub.2S or H.sub.2O, or a combination thereof. In some embodiments, the stream containing SO.sub.2 contains about 80 wt. %, about 85 wt. %, about 90 wt. %, about 95 wt. %, or about 99 wt. % of SO.sub.2.

[0042] In some embodiments, molar ratio of CO to H.sub.2 in the stream containing syngas is from about 1:10 to about 10:1, from about 1:10 to about 5:1, or from about 1:5 to about 1:1. In some embodiments, molar ratio of CO to H.sub.2 is about 1:10, about 1:5, about 1:2, about 1:1, about 2:1, about 5:1, or about 10:1. In one example, the syngas is collected from the cathode side of the cell at a temperature insufficient to react CO and H.sub.2 to produce any other chemical compound. In some embodiments, the syngas is substantially free of components other than CO and H.sub.2. For example, the syngas contains no more than about 0.5 wt. %, about 1 wt. %, about 2 wt. %, about 5 wt. %, or about 10 wt. % of H.sub.2O or CO.sub.2, or a combination thereof.

[0043] The syngas produced according to the methods of this disclosure may be used in any field where syngas is generally useful. For example, the syngas can be burned (reacted with O.sub.2 at elevated temperature) to produce lighting (commonly known as gas lighting), or it may be used as fuel for cooking and heating. In another example, syngas may be used to produce sponge iron by reduction of iron ore. Syngas can also be useful to produce diesel in Fischer-Tropsch process, or it may be chemically converted to other useful chemicals, such as methane, methanol, or dimethyl ester.

[0044] Likewise, SO.sub.2 produced using the methods of this disclosure may be useful in any manner where this compound is generally useful. In one example, SO.sub.2 may be used to react with H.sub.2S to produce elemental sulfur (Claus process). SO.sub.2 may also be reacted with Cl.sub.2 to yield sulfuryl chloride (SO.sub.2Cl.sub.2). Importantly, SO.sub.2 may be oxidized by oxygen in the presence of water to produce sulfuric acid (H.sub.2SO.sub.4). Various S-containing heterocyclic reagents may also be prepared from SO.sub.2 for pharmaceutical industry, sulfolane being one of the examples.

OTHER EMBODIMENTS

[0045] It is to be understood that while the present application has been described in conjunction with the detailed description thereof, the foregoing description is intended to illustrate and not limit the scope of the present application, which is defined by the scope of the appended claims. Other aspects, advantages, and modifications are within the scope of the following claims.