Methods and systems for fuel production in electrochemical cells and reactors

Abstract

Methods and systems for fuel, chemical, and/or electricity production from electrochemical cells are disclosed. A voltage is applied between an anode and a cathode of an electrochemical cell. The anode includes a metal or metal oxide electrocatalyst. Oxygen is supplied to the cathode, producing oxygen ions. The anode electrocatalyst is at least partially oxidized by the oxygen ions transported through an electrolyte from the cathode to the anode. A feed gas stream is supplied to the anode electrocatalyst, which is converted to a liquid fuel. The anode electrocatalyst is re-oxidized to higher valency oxides, or a mixture of oxide phases, by supplying the oxygen ions to the anode. The re-oxidation by the ions is controlled or regulated by the amount of voltage applied.

Claims

1. A method of converting lower-cost gases into higher-value fuels and chemicals, comprising: a. applying a voltage between an anode and a cathode of an electrochemical cell, wherein the anode includes a metal oxide electrocatalyst; b. supplying oxygen to the cathode which produces oxygen ions, wherein the anode electrocatalyst is at least partially oxidized by the oxygen ions transported through an electrolyte from the cathode to the anode; and c. supplying a feed gas stream to the anode electrocatalyst, wherein the feed gas stream is at least partially oxidized by the anode electrocatalyst; and d. re-oxidizing the anode electrocatalyst by supplying the oxygen ions to the anode, the extent of which is controlled by the voltage applied.

2. The method of claim 1 wherein the anode electrocatalyst is re-oxidized to higher valency oxides or a mixture of oxide phases.

3. The method of claim 1 wherein the feed gas stream is methane and the liquid fuel is methanol or formaldehyde.

4. The method of claim 1 wherein the anode electrocatalyst comprises oxides of at least one of the following: Co, Cu, Fe, Mn, Mo, Sb, Ga, Zn, P, Ce, W, Ti, Sn, Zn, Nd, Bi, Re, Ru, Rh, Ga, Cs, and V.

5. The method of claim 4 wherein the cathode is a lithiated composite material and the electrolyte is a composite material.

6. The method of claim 5 wherein the cathode is a lithiated nickel oxide material and the electrolyte is selected from the group consisting of: doped cerium oxide, alkali carbonate, sodium carbonate, and combinations thereof.

7. A method of producing electricity from gases comprising: a. applying a voltage between an anode and a cathode of a first electrochemical cell, wherein the anode includes a metal or a metal oxide electrocatalyst or their mixture; b. supplying oxygen to the cathode which produces oxygen ions, wherein the anode electrocatalyst is at least partially oxidized by the oxygen ions transported through an electrolyte from the cathode to the anode; c. supplying a feed gas stream to the anode electrocatalyst, wherein the feed gas stream is at least partially oxidized by the anode electrocatalyst and converted to a liquid fuel, and wherein the anode electrocatalyst is re-oxidized by the oxygen ions, the extent of which is controlled by the voltage applied; and d. oxidizing the liquid fuel over a second anode electrocatalyst of a second electrochemical cell to produce electricity.

8. The method of claim 7 wherein oxygen lost by the second anode electrocatalyst in oxidizing the liquid fuel is re-oxidized by oxygen ions through a second cathode and electrolyte of the second electrochemical cell.

9. The method of claim 7 wherein the second anode electrocatalyst comprises Ni alloys of at least one of the following: Mo, W, Co, Cu, Fe, Sb, Sn, P, and Zn.

10. The method of claim 7 wherein the feed gas stream is methane and the liquid fuel is methanol or formaldehyde.

11. The method of claim 7 wherein the anode electrocatalyst comprises oxides of at least one of the following: Co, Cu, Fe, Mn, Mo, Sb, Ga, Zn, P, Ce, W, Ti, Sn, Zn, Nd, Bi, Re, Ru, Rh, Ga, Cs, and V.

12. The method of claim 11 wherein the first and second cathodes comprise a lithiated composite material and the first and second electrolytes comprise a composite material.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is a schematic diagram of an electrochemical cell for converting gases to liquids, in accordance with one embodiment of the present invention.

(2) FIG. 2 is a schematic diagram of a system for converting gases to liquids and electricity, in accordance with one embodiment of the present invention.

(3) FIG. 3 is a schematic diagram of a system for converting gases to liquids, in accordance with one embodiment of the present invention.

(4) FIG. 4 shows critical oxygen partial pressures over metal oxide redox couples (solid lines) as a function of temperature and compares them to minimum oxygen activities required for partial oxidation of methane to methanol and formaldehyde (dashed lines).

(5) FIG. 5 shows cell potential versus air as a function of temperature to partially oxidize methane to methanol and formaldehyde (dashed lines) and the oxygen activities produced by metal oxide redox couples (solid lines).

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

(6) The following description includes the preferred best mode of embodiments of the present invention. It will be clear from this description of the invention that the invention is not limited to these illustrated embodiments but that the invention also includes a variety of modifications and embodiments thereto. Therefore the present description should be seen as illustrative and not limiting. While the invention is susceptible of various modifications and alternative constructions, it should be understood, that there is no intention to limit the invention to the specific form disclosed, but, on the contrary, the invention is to cover all modifications, alternative constructions, and equivalents falling within the spirit and scope of the invention as defined in the claims.

(7) The present invention includes methods and system for converting low-cost gases to higher-value liquids, fuels, and/or electricity, enabling the more efficient use of both electricity and natural gas resources.

(8) Mixed metal oxide-based anode electrocatalysts have been developed for use in an electrochemical cell where low-cost gases will be converted to higher-value fuels, chemicals, and/or electricity. In one embodiment, the electrocatalyst is composed of oxides such as Co, Cu, Fe, Mn, Mo, Sb, Ga, Zn, P, Ce, W, Ti, Sn, Zn, Nd, Bi, Re, Ru, Rh, Ga, Cs, and V oxides, which have sufficient oxidizing power to at least partially oxidize a feed gas stream or low-cost gas. In one example, the anode electrocatalyst oxidizes methane to either methanol or formaldehyde. Oxygen lost from the electrocatalyst in partially oxidizing the feed gas stream is replenished by oxygen ion flux through an electrolyte of the electrochemical cell, and the oxygen ion flux is controlled by a bias potential on the cell.

(9) FIG. 1 is a schematic diagram of an electrochemical cell 100 for converting gases to liquids, in accordance with one embodiment of the present invention. The electrochemical cell 100, which may be an electrochemical reactor or fuel production cell, includes an anode 130, an electrolyte 120, and a cathode 110.

(10) The anode 130 includes a metal or metal-oxide electrocatalyst or mixtures thereof. The electrocatalyst composition may be composed of, but is not limited to, at least one of the following: Co, Cu, Fe, Mn, Mo, Sb, Ga, Zn, P, Ce, W, Ti, Sn, Nd, Bi, Re, Ru, Rh, Ga, Cs, or V. Selectivity and yield are enhanced by electrochemically maintaining a desired redox state or oxygen buffer in the metal oxides that exhibit activity for direct gas-to-liquid conversion, while avoiding conditions that lead to over or deep oxidation.

(11) The cathode 110, which is porous, allows oxygen to pass through to partially oxidize the anode 130. In one embodiment, the cathode 130 is a lithiated composite material such as lithiated nickel oxide.

(12) The electrolyte 120 may be, but is not limited to, a composite material. The composite electrolyte can be a samarium oxide doped cerium oxide or CeO2-Na.sub.2CO.sub.3 composite.

(13) Still referring to FIG. 1, a feed stream 140 is fed to the anode 130 side of the cell 100 for reaction with the anode electrocatalyst. The feed stream 140 is converted to a liquid fuel 150 during the reaction, and the oxygen lost by the anode electrocatalyst in oxidizing the feed stream 140 is replenished by oxygen ion flux, e.g. O.sup.2, pumped into the cell 100. As such, the anode will take the O.sup.2 ions and the metal or metal oxide in the anode will be oxidized to higher valency oxides or a mixture of oxide phases. The oxygen ion flux is at least partially controlled or regulated by the voltage applied between the anode 130 and the cathode 110 through the load. At lower voltages, the flux of oxygen-containing species is lower. Likewise, at higher voltages, the flux of oxygen-containing species is increased.

(14) FIG. 2 is a schematic diagram of a system 200 for converting gases to liquids and electricity, in accordance with one embodiment of the present invention. The system 200 includes a first electrochemical cell 205 for fuel generation or production and a second electrochemical cell 265 for electricity production. The first electrochemical cell 205, which is similar to the cell 100 of FIG. 1, includes anode 230, cathode 210, and electrolyte 220. Voltage is applied between the anode 230 and the cathode 210 through the load. The feed stream 240 is converted to liquid fuel 250 by the first electrochemical cell 205. In this fuel generation mode, the anode catalyst is at least partially oxidized by the oxygen ions, shown as O.sup.2, flowing through the electrolyte 220 from the cathode 210. The oxidized anode is then re-reduced through reactions with the feed stream 240.

(15) The second electrochemical cell 265 also includes an anode 235, a cathode 215, and an electrolyte 225. The anode 235 also includes an electrocatalyst. The electrocatalyst composition of the anode 235 may be composed of, but is not limited to, a nickel alloy. The cathode 215 and the electrolyte 225 may be composed of the same cathode and electrolyte materials as used in the first electrochemical cell 205, but can be different materials.

(16) The liquid fuel 250 is supplied to the anode side of the cell 265, where it is oxidized by oxygen ion flux flowing from the cathode 215 through the electrolyte 225. This oxygen ion flux is also controlled by cell voltage on the cell 265. The reactions between the liquid fuel 240 and the oxygen ions produce water, carbon dioxide, and electricity. Other fuels may be produced as well depending on the feed stream. The anode material of the cell 265 includes nickel, which can be additionally alloyed with other elements, such as Mo, W, Co, Cu, Fe, Sb, Sn, P, and Zn, to lower the tendency for fuel cracking without impeding the activity.

(17) FIG. 3 is a schematic diagram of a system 300 for converting gases to liquids, in accordance with one embodiment of the present invention. The system 300 is, in many ways, similar to the system 200 of FIG. 2, with the addition of a support structure or substrate 270. The support 270, cathodes 210, and electrolytes 220 for each cell 305 and 360 may be composed of the same material. The anodes 230 and 235 are composed of the different materials. In one embodiment, the support 270 is a porous ferritic steel/ceramic support, onto which a porous LiNiO cathode and a fully dense ceria/alkali carbonate electrolyte are deposited. As an alternative, the porous ceramic will be the support structure. The porous cathode 210 itself can serve as the ceramic support structure as well.

(18) In one specific embodiment, a cermet consisting of a FeCr ferritic stainless steel combined with an aluminum iron titanate ceramic phase (Al.sub.1.57Fe.sub.0.43TiO.sub.5, AFT) is used as the structural support. The addition of the low-expansion AFT ceramic phase enables the thermal expansion coefficient of the composite to be adjusted to best match that of other electrochemical cell components. Steel and AFT powders may be mixed with water-based binders composed of acrylic polymer suspensions with polyethylene glycol pore formers and processed by firing in forming gas. The thickness may be 2 mm, with 50% porosity to allow adequate gas flow. The formation of a conductive passivation layer rich in chromium oxide, combined with intermediate operating temperatures, enables the cermet composite support to be used on either the cathode or anode side.

(19) In one embodiment, lithiated NiO is used as the cathode. The cathode can be applied by tape-casting methods. An alternative, potentially low cost method is to deposit the cathode directly onto the cermet support using reactive spray deposition technology (RSDT), PVD, and/or plasma spray processing. RSDT flame based processing can produce fuel cell layers more rapidly than traditional techniques, and with no need for high-temperature sintering steps. RSDT can therefore potentially reduce the manufacturing cost and capital cost required, as well as the material costs, by allowing for thinner deposited layers.

(20) In one embodiment, the doped cerium oxide/alkali carbonate materials can be used as the electrolyte. Superionic conductivity in these composites has been attributed to a substantially higher defect concentration near phase boundaries and a high degree of disorder at those interfaces. Simultaneous oxygen ion and proton conductivity has been reported, with transference numbers for protons of 0-0.5 and for oxygen ions from 0.5 to 1.0. Mixed proton and oxygen ion conduction can be of significant benefit for both fuel cell and fuel production cell modes, particularly with regard to activation of non-hydrogen fuels.

(21) In one embodiment, the anode for the electricity production cell includes a nickel-based electrocatalyst. The nickel can be alloyed with Mo, W, Co, Cu, Fe, Sb, Sn, P, and Zn, alone or in combination to decrease Ni tendency for hydrocarbon fuel cracking Effective Ni alloy-based anodes enable effective utilization of alcohol and other biofuels. Dilute alloys of Ni with Sn and Sb are also effective in improving the sulfur tolerance of SOFC anodes, without diminishing its activity. Other possible anodes include metal oxide or metal oxide/ceria/carbon composites. As one example, a Ni alloy/ceria composite electrocatalyst enables effective utilization of methanol and related fuels.

(22) In one embodiment, the anode for the fuel production cell includes a metal oxide-based anode electrocatalyst, where a gas feed stream such as methane will be converted to liquid fuels. The anode electrocatalyst is composed of metal oxides including, but not limited to, Co, Cu, Fe, Mn, Mo, Sb, Ga, Zn, P, Ce, W, Ti, Sn, Zn, Nd, Bi, Re, Ru, Rh, Ga, Cs, and/or V. These metal oxide couples have sufficient oxidizing power to partially oxidize methane to either CH.sub.3OH or HCHO. Oxygen lost from the electrocatalyst in partially oxidizing the feed stream is replenished by the oxygen ion flux through the electrolyte, controlled by the bias potential on the cell, shown schematically in FIG. 3.

(23) FIG. 4 shows critical oxygen partial pressures over metal oxide redox couples (solid lines) as a function of temperature and compares them to minimum oxygen activities required for partial oxidation of methane to methanol and formaldehyde (dashed lines).

(24) Polarization at the anode of the electrochemical cells can drive the formation of new phases at the electrolyte/electrode interface that may not be possible elsewhere in the cell. Thus, anodic polarization is used in the present invention to tune the oxygen activity at the active interface. Selectivity and yield will be enhanced by electrochemically maintaining a desired redox state (oxygen buffer) in metal oxides that exhibit activity for certain gas to liquids conversion, while avoiding conditions that could lead to deep oxidation of the feed stream.

(25) FIG. 5 shows cell potential versus air as a function of temperature to partially oxidize methane to methanol and formaldehyde (dashed lines) and the oxygen activities produced by metal oxide redox couples (solid lines).

(26) Experimental Section

(27) The following examples serve to illustrate embodiments and aspects of the present invention and should not be construed as limiting the scope thereof.

(28) Electrochemical Conversion of Methane to Methanol and Formaldehyde

(29) The fuel production cell would utilize the same support, cathode, and electrolyte as was described in connection with FIG. 3 above. Following FIGS. 4 and 5 to achieve the minimum oxygen activity needed to oxidize methane to methanol, the cell would operate at <0.5 V at 450 C., while formaldehyde synthesis calls for a cell potential of <0.75V. Formaldehyde is typically produced by methanol oxidation, so it may not be possible to convert methane directly to formaldehyde. The oxygen activity at the anode/electrolyte is determined by (1) the thermodynamics of the particular redox couple (this defines the cell open circuit voltage), and (2) the anodic overpotential. The anodic overpotential, the result of faradaic processes with current flow, renders the interface more oxidizing than elsewhere in the anode, providing much greater flexibility with respect to choice of anode materials than the redox couple alone. The oxygen most able to convert methane to liquid fuels is available at the active interface. By choosing metal oxide electrocatalysts that have promise for methanol synthesis, and by carefully regulating their oxygen activity, high selectivity can be achieved.

(30) Total polarization losses up to about 0.3 V are anticipated at a current density of approximately 100 mA/cm.sup.2. The allowable cell resistance is thus approximately 0.3V/0.1 A/cm.sup.23 ohms-cm.sup.2, most of which will arise from anode reactions.

(31) The present invention includes electrochemical technology that converts low-cost gases to higher-value fuels and other liquids in the fuel production electrochemical cell and produces electricity from the liquids and other fuels in the electricity production electrochemical cell, by controlling the oxygen activity of the anode electrocatalyst. These cells can also be operated at intermediate temperatures.

(32) As one example, the methods and systems of the present invention can convert low-cost natural gas to high-value alcohol fuels and chemical intermediates at commercially competitive capital and operating costs. This would be especially valuable at low-scale at the wellhead and at landfill sites, in addition to traditional chemical processing plant settings. The present invention enables the more efficient use of both electricity and natural gas resources, by producing liquid fuels during periods of excess renewable energy capacity, and by converting those liquid fuels back to electricity in periods of greater need.

(33) While a number of embodiments of the present invention have been shown and described, it will be apparent to those skilled in the art that many changes and modifications may be made without departing from the invention in its broader aspects. The appended claims, therefore, are intended to cover all such changes and modifications as they fall within the true spirit and scope of the invention.