Novel compositions capable of operating under high carbon dioxide partial pressures for use in solid-state oxygen producing devices

Abstract: The present invention presents a new class of multicomponent metallic oxides which are particularly suited toward use in fabricating components used in solid-state oxygen separation devices. The compositions of the present invention are represented by the formula Ln x A' x' A'' x'' B y B' y' B'' y'' O 3-z, wherein Ln is an element selected from the f block lanthanides, A' is selected from Group 2, A'' is selected from Groups 1, 2 and 3 and the f block lanthanides, and B,B',B'' are independently selected from the d block transition metals, excluding titanium and chromium, wherein 0≦x<1, 0<x'<1, 0≦x''<1, 0<y<1.1, 0<y'<1.1, 0<y''<1.1, x+x'+x''=1.0 , 1.1>y+y'+y''>1.0 and z is a number which renders the compound charge neutral wherein such elements are represented according to the Periodic Table of the Elements adopted by IUPAC. These compositions provide superior resistance to degradation when employed in such devices under process conditions of high carbon dioxide and water partial pressures.

Description: FIELD OF THE INVENTION This invention relates to novel compositions comprising multicomponent metallic oxides which are particularly suited toward use in fabricating solid-state oxygen producing devices. The multicomponent metallic oxides comprise at least three transition metals, excluding titanium and chromium, wherein the ratio of the transition metals to other metallic components ranges from greater than 1 to less than 1.1. The compositions enable such oxygen producing devices to be operated under elevated carbon dioxide partial pressures. BACKGROUND OF THE INVENTION Solid state membranes formed from oxygen ion-conducting materials continue to show promise for use in commercial processes for separating and recovering oxygen from oxygen-containing gaseous mixtures as well as for reacting oxygen formed therefrom with a feedstock comprising light hydrocarbons such as methane, natural gas, ethane or any available light hydrocarbon mixture. Representative membranes are those formed from multicomponent metallic oxides which are typically operated at high temperatures (e.g. 600°C or more) wherein the membranes conduct both oxygen ions and electrons. When a difference in oxygen partial pressure exists on opposite sides of the multicomponent metallic oxide membrane and operating conditions are properly controlled, oxygen is transported in the form of oxygen ions from the high oxygen partial pressure side to the low oxygen partial pressure side of the membrane while an electron flux occurs in the opposite direction of oxygen ion migration in order to conserve charge, producing pure oxygen on the permeate side of the membrane. Multicomponent metallic oxides to be employed in devices for producing Oxygen must exhibit a variety of mechanical and physical properties in order to provide sufficient operating life and to perform according to desired operating specifications. Devices incorporating such materials should be capable of being subjected to elevated carbon dioxide and water partial pressures without observing any appreciable loss in oxygen transport properties. Unfortunately, typical multicomponent metallic oxides known in the art provide varying degrees of these essential attributes. Therefore, the ceramist must endeavor to optimize the composition of such materials to achieve acceptable levels of each of the identified mechanical and physical properties. Tabata and coworkers (J. Mat. Sci., 22 (1987) 1882-1886)) investigated the surface chemical states of the perovskite-type compounds, strontium-doped lanthanum cobalt oxides(La 1-x Sr x CoO 3 ) utilizing X-ray photoelectron spectroscopy. Catalytic oxidations of both methane and carbon monoxide were also studied using various flow methods. Fig. 9 illustrates that the catalytic activity of La 1-x Sr x CoO 3 increased with an increase in the quantity of cobalt atoms on the material's surface. U.S. Patent 5,261,932 presents a process for recovering oxygen from an oxygen-containing gaseous mixture containing one or more components selected from water, carbon dioxide or a volatile hydrocarbon. The process utilizes ion transport membranes comprising a stoichiometric multicomponent metallic oxide containing strontium, calcium or magnesium. The process utilizes a temperature regime which overcomes problems associated with degradation of strontium-, calcium- and magnesium-containing multicomponent oxides caused by carbon dioxide. Preferred stoichiometric multicomponent metallic oxides are represented by the structure A x A' x' A" x" B y B' y' B" y" O 3-z , where A,A',A" are chosen from the group comprising Groups 1, 2 and 3 and the F block lanthanides; and B,B',B" are chosen from the D block transition metals according to the Periodic Table of the Elements adopted by the IUPAC wherein 0≤x≤1, 0≤x'≤1, 0≤x"≤1, 0<y≤1, 0≤y'≤1, 0≤y"≤1, x+x'+x"=1 , y+y'+y"=1 and z is a number which renders the compound charge neutral. Preferably, A, A' or A" of the enumerated structure is a Group 2 metal selected from the group consisting of calcium, strontium and magnesium. U.S. Patent 5,269,822 presents a process for recovering oxygen from an oxygen-containing gaseous mixture containing one or more components selected from water, carbon dioxide or a volatile hydrocarbon. The process utilizes ion transport membranes comprising a stoichiometric multicomponent metallic oxide containing barium and a temperature regime which overcomes problems associated with degradation of barium-containing multicomponent metallic oxides caused by carbon dioxide. Preferred stoichiometric multicomponent metallic oxides are represented by the structure A x Ba x' B y B' y' B" y" O 3-z , where A is chosen from the group comprising Groups 1, 2 and 3 and the F block lanthanides with the proviso that A is not yttrium; and B,B',B" are chosen from the D block transition metals according to the Periodic Table of the Elements adopted by the IUPAC wherein 0≤x≤1, 0<x'≤1, 0<y≤1, 0≤y'≤1, 0≤y"≤1, x+x'=1 , y+y'+y"=1 and z is a number which renders the compound charge neutral. U.S. Patent 5,356,728 and European Patent Application WO 94/24,065 disclose cross-flow electrochemical reactor cells formed from multicomponent metallic oxides of the perovskite structure which demonstrate both electron conductivity and oxygen ion conductivity at elevated temperatures. Such cells are useful in carrying out partial oxidation reactions of organic compounds to form added-value products and separating oxygen from oxygen-containing gaseous mixtures. Suitable multicomponent metallic oxides are represented by (Sr 1-y M y)α (Fe 1-x Co x ) α+β O δ where M is a metal selected from the group consisting of elements having atomic number in a range from 56 to 71, calcium, and yttrium, x is a number in a range from about 0.01 to about 0.95, y is a number in a range from about 0.01 to about 0.95, α is a number in a range from about 1 to about 4, β is a number in a range upward from 0 to about 20, such that 1.1 <(α+β)/α≤6, and δ is a number which renders the compound charge neutral, and wherein the composition has a non-perovskite structure. U.S. Patent 5,306,411 discloses a solid multicomponent membrane for use in an electrochemical reactor characterized by (1) an intimate, gas-impervious, multiphase mixture of an electronically-conductive phase and an oxygen ion-conductive phase wherein at least one of said phases is a mixed metal oxide having a perovskite structure represented by the formula: A s A' t B u B' v B" w O x wherein A represents a lanthanide, Y, or mixture thereof; A' represents an alkaline earth metal or mixture thereof: B represents Fe; B' represents Cr, Ti, or mixture thereof; and s, t, u, v, w, and x each represent a number such that: s/t equals from about 0.01 to about 100; u equals from about 0.01 to about 1; v equals from about 0.01 to 1; w equals from zero to about 1; x equals a number that satisfies the valences of the A, A', B, B' and B" in the formula; and 0.9<(s+t)/(u+v+w)<1.1; or (2) a mixed metal oxide material having a perovskite structure represented by the formula: A s A' t B u B' v B" w O x wherein A represents a lanthanide or Y, or a mixture thereof; A' represents an alkaline earth metal or a mixture thereof; B represents Fe, B' represents Cr or Ti, or a mixture thereof; and B'' represents Mn, Co, V, Ni or Cu, or a mixture thereof and s, t, u, v, w, and x each represent a number such that: s/t equals from about 0.01 to about 100; u equals from about 0.01 to about 1; v equals from about 0.01 to 1; w equals from zero to about 1; x equals a number that satisfies the valences of the A, A', B, B' and B" in the formula; and 0.9 < (s+t)/(u+v+w) < 1.1 . Those skilled in the art are searching for multicomponent metallic oxides of the perovskite-type for use in solid-state oxygen-producing devices which would tolerate being subjected to high carbon dioxide and water partial pressures during operation, without suffering a loss in oxygen flux. BRIEF SUMMARY OF THE INVENTION Applicants have discovered a new class of multicomponent metallic oxides which are particularly suited toward use in fabricating components used in solid-state oxygen separation devices. These compositions overcome problems associated with prior art materials by providing superior resistance to degradation when employed in such devices under process conditions of elevated carbon dioxide and water partial pressures. The compositions of the present invention are represented by the formula Ln x A' x' A" x" B y B' y' B" y" O 3-z , wherein Ln is an element selected from the f block lanthanides, A' is selected from Group 2, A" is selected from Groups 1, 2 and 3 and the f block lanthanides, and B,B',B" are independently selected from the d block transition metals, excluding titanium and chromium, wherein 0≤x<1, 0<x'<1, 0≤x"<1, 0<y<1.1, 0<y'<1.1, 0<y"<1.1, x+x'+x"=1.0 , 1.1>y+y'+y">1.0 and z is a number which renders the compound charge neutral wherein such elements are represented according to the Periodic Table of the Elements adopted by IUPAC. Applicants have further discovered that significant cost savings can be enjoyed by utilizing a mixture of lanthanides for Ln as represented by the abovementioned formula instead of individual, highly pure lanthanides of the f block of the IUPAC Periodic Table of the Elements. For example, highly pure lanthanum oxide is substantially more expensive than a mixture of lanthanum oxide, cerium oxide, praseodymium oxide and neodymium oxide which is commercially available from Molycorp, a division of Unical Corporation, Los Angeles, CA . Thus, Ln in the above mentioned formula may comprise a mixture of lanthanum and at least one element other than lanthanum which is selected from the f block lanthanides as represented by the IUPAC Periodic Table of the Elements. Particularly suitable compositions according to the present invention are represented by the formula La x A' x' A" x" Co y Fe y' Cu y" O 3-z wherein A' is selected from strontium, barium, calcium or magnesium, A" is selected from Groups 1, 2 and 3 and the f block lanthanides, wherein 0≤x<1, 0<x'<1, 0≤x"<1, 0<y<1.1, 0<y'<1.1, 0<y"<1.1, x+x'+x"=1.0 , 1.1>y+y'+y">1.0 and z is a number which renders the composition charge neutral. Representative compositions include La 0.2 Ba 0.8 Co 0.62 Cu 0.21 Fe 0.21 O 3-z , wherein A' is barium, x is 0.2, x' is 0.8, x" is 0, y is 0.62, y' is 0.21 and y" is 0.21, La 0.2 Sr 0.8 Co 0.41 Fe 0.41 Cu 0.21 O 3-z , wherein A' is strontium, x is 0.2, x' is 0.8, x" is 0, y is 0.41, y' is 0.41 and y" is 0.21, La 0.4 Sr 0.6 Co 0.41 Fe 0.41 Cu 0.21 O 3-z wherein A' is strontium, x is 0.4, x' is 0.6, x" is 0, y is 0.41, y' is 0.41 and y" is 0.21, La 0.3 Sr 0.7 Co 0.82 Fe 0.11 Cu 0.11 O 3-z wherein A' is strontium, x is 0.3, x' is 0.7, x" is 0, y is 0.82, y' is 0.11 and y'' is 0.11. La 0.2 Sr 0.8 Co 0.42 Fe 0.42 Cu 0.21 O 3-z wherein A' is strontium, x is 0.2, x' is 0.8, x" is 0, y is 0.42, y' is 0.42 and y" is 0.21, and Sr 1.0 Co 0.42 Fe 0.42 Cu 0.21 O 3-z wherein A' is strontium, x is 0, X' is 1.0, x" is 0, y is 0.42, y' is 0.42 and y" is 0.21. Applicants' invention can be more readily understood by referring to the Detailed Description of the Invention and the figures which are attached hereto. BRIEF DESCRIPTION OF THE DRAWINGS In the drawings, which illustrate what is currently considered to be the best mode for carrying out the invention, FIG. 1 is an exploded perspective view of one embodiment of a planar solid-state electrochemical module comprising a plurality of planar membrane units formed from a dense multicomponent metallic oxide layer which is supported by and contiguous with a channel-free porous support having connected through porosity. The removal means for discharging oxygen from each planar membrane unit comprises at least one conventional manifold. FIG. 2 is a sectional view of the planar solid-state electrochemical module of FIG. 1 which illustrates three membrane unit embodiments, each embodiment which presents a dense multicomponent metallic oxide layer which is supported by a channel-free porous support have connected through porosity; FIG. 3 is an exploded perspective view of another embodiment of a planar solid-state electrochemical module comprising a plurality of planar membrane units formed from a dense multicomponent metallic oxide layer which is supported by and contiguous with a channel-free porous support having connected through porosity. The removal means for discharging oxygen from each planar membrane unit comprises a conduit which traverses each planar membrane unit and is in flow communication with the porous support of each membrane unit of the module; FIG. 4 is an exploded view of the planar solid-state electrochemical module of FIG. 3 which illustrates three membrane unit embodiments, each which present a dense multicomponent metallic oxide layer which is supported by a channel-free porous support have connected through porosity; FIG. 5 is an exploded view of a preferred embodiment of a planar membrane unit suitable for incorporation into the planar solid-state membrane module illustrated in FIG. 3; FIG. 6 is a top view of a housing suitable for receiving the planar membrane modules of the present invention which provides a means for introducing a heated oxygen-containing gaseous mixture to be separated into contact with the planar membrane modules and a means for discharging oxygen from the plurality of planar membrane units of the planar solid-state membrane modules; FIG. 7 illustrates the dimensional changes of a multicomponent metallic oxide, La 0.2 Sr 0.8 Co 0.4 Fe 0.4 Cu 0.2 O 3-z, which is given for comparison as a function of temperature thereby illustrating control of the coefficient of thermal expansion when copper is introduced into the perovskite structure; FIG. 8 presents x-ray diffraction patterns of a stoichiometric multicomponent metallic oxide, a non-stoichiometric multicomponent metallic oxide which is A-site rich and a non-stoichiometric multicomponent metallic oxide which is B-site rich; each which has been subjected to elevated carbon dioxide partial pressures at elevated temperatures for a one week period; and FIG. 9 illustrates a plot of oxygen flux as a function of water, carbon dioxide and oxygen partial pressures present in a process feedstream obtained by employing membranes formed from A-site rich non-stoichiometric and B-site rich non-stoichiometric multicomponent metallic oxides. DETAILED DESCRIPTION OF THE INVENTION Applicants have discovered a new class of multicomponent metallic oxides which are particularly suited toward use in fabricating components used in solid-state oxygen separation devices. These compositions overcome problems associated with prior art materials by providing superior resistance to degradation when employed in such devices under process conditions of elevated carbon dioxide and water partial pressures. The compositions of the present invention are represented by the formula Ln x A' x' A" x" B y B' y' B" y" O 3-z , wherein Ln is an element selected from the f block lanthanides, A' is selected from Group 2, A" is selected from Groups 1, 2 and 3 and the f block lanthanides, and B,B',B" are independently selected from the d block transition metals, excluding titanium and chromium, wherein 0≤x<1, 0<x'<1, 0≤x"<1, 0<y<1.1, 0<y'<1.1, 0<y"<1.1, x+x'+x"=1.0 , 1.1>y+y'+y">1.0 and z is a number which renders the compound charge neutral wherein such elements are represented according to the Periodic Table of the Elements adopted by IUPAC. Applicants have further discovered that significant cost savings can be enjoyed by utilizing a mixture of lanthanides for Ln as represented by the above-mentioned formula instead of individual, highly pure lanthanides of the f block of the IUPAC Periodic Table of the Elements. For example, highly pure lanthanum oxide is substantially more expensive than a mixture of lanthanum oxide, cerium oxide, praseodymium oxide and neodymium oxide which is commercially available from Molycorp, a division of Unical Corporation, Los Angeles, CA. Thus, Ln in the above mentioned formula may comprise a mixture of lanthanum and at least one element other than lanthanum which is selected from the f block lanthanides as represented by the IUPAC Periodic Table of the Elements. Particularly suitable materials according to the present invention are represented by the formula La x A' x' A" x" Co y Fe y' Cu y" O 3-z wherein A' is selected from strontium, barium, calcium or magnesium, A'' is selected from Groups 1, 2 and 3 and the f block lanthanides wherein 0≤x<1, 0<x'<1, 0≤x"<1, 0<y<1.1, 0<y'<1.1, 0<y"<1.1, x+x'+x''=1.0 , 1.1>y+y'+y">1.0 and z is a number which renders the composition charge neutral. Representative compositions include La 0.2 Ba 0.8 Co 0.62 Cu 0.21 Fe 0.21 O 3-z , wherein A' is barium, x is 0.2, x' is 0.8, x" is 0, y is 0.62, y' is 0.21 and y", is 0.21, La 0.2 Sr 0.8 Co 0.41 Fe 0.41 Cu 0.21 O 3-z , wherein A' is strontium, x is 0.2, x' is 0.8, x" is 0, y is 0.41, y' is 0.41 and y" is 0.21, La 0.4 Sr 0.6 Co 0.41 Fe 0.41 Cu 0.21 O 3-z wherein A' is strontium, x is 0.4, x' is 0.6, x" is 0, y is 0.41, y' is 0.41 and y" is 0.21, La 0.3 Sr 0.7 Co 0.82 Fe 0.11 Cu 0.11 O 3-z wherein A' is strontium, x is 0.3, x' is 0.7, x" is 0, y is 0.82, y' is 0.11 and y" is 0.11, La 0.2 Sr 0.8 Co 0.42 Fe 0.42 Cu 0.21 O 3-z , wherein A' is strontium, x is 0.2, x' is 0.8, x" is 0, y is 0.42, y' is 0.42 and y" is 0.21, and Sr 1.0 Co 0.42 Fe 0.42 Cu 0.21 O 3-z wherein A' is strontium, x is 0, X' is 1.0, x" is 0, y is 0.42, y' is 0.42 and y" is 0.21. Applicants' invention can be more readily understood by referring to the Detailed Description of the Invention and the figures which are attached hereto. The improvements afforded by the novel multicomponent metallic oxides of the present invention shall be best appreciated following a description of the oxygen separation devices which utilize such materials and a presentation of the data which compares the properties of the claimed compositions to the properties afforded by prior art compositions for the subject process applications. FIG. 1 is an exploded perspective view of an embodiment of a planar module comprising a plurality of air separation membrane units. Planar module 10 possesses an array 15 of gas separation membrane units 20 which are separated by passageways 25. Each membrane unit 20 comprises a porous support 22 and dense multicomponent metallic oxide layer 21. Structures 35 and 40 adjacent opposite entrance and exit surfaces of the membrane array of modules 15 defines spaced entrance and exit manifolds having receiving structures 55 into which membrane units 20 are received. Thus, manifolds 35 and 40 are in flow communication with the porous layers 22 of each membrane 20 within the array of membranes 15. Inlet lines 45 and 50 are situated in manifolds 35 and 40 and are adapted to carry oxygen product from the module 10. The embodiment according to FIG. 1 can be conveniently utilized to separate oxygen from an oxygen-containing gaseous mixture by introducing the oxygen-containing gaseous mixture through passageways 25 and into contact with the dense multicomponent metallic layers 21 of each of the membrane units 20. The driving force for separating oxygen from an oxygen-containing gaseous mixture is provided by creating a difference in oxygen partial pressure on opposite sides of the dense multicomponent metallic oxide layer of each membrane unit. An oxygen partial pressure difference on opposite sides of dense multicomponent metallic oxide layer 21 can be created by compressing the oxygen-containing gaseous mixture within passageways 25 to a pressure sufficient to recover the oxygen permeate stream at a pressure of greater than or equal to about one atmosphere. Typical pressures range from about 15 psia to about 250 psia and the optimum pressure will vary depending upon the amount of oxygen in the oxygen-containing gaseous mixture. Conventional compressors are capable of achieving the required compression. Alternately, a positive oxygen partial pressure on opposite sides of dense multicomponent metallic oxide layer 21 can be achieved by partially evacuating the porous support to a pressure sufficient to recover the oxygen permeate. The oxygen which has been separated from the oxygen-containing gaseous mixture can be stored in a suitable container or utilized in another process. The oxygen permeate typically comprises pure oxygen or high purity oxygen defined as a gas generally containing at least about 90 vol.% O 2 , preferably more than about 95 vol% O 2 and especially more than 99 vol.% O 2 . The planar membrane modules of the present invention can be used for a variety of processes including the separating of any ionizable component from a feedstream wherein such ionizable component is capable of being transported through the ionic conducting electrolyte layer. For example, the ionizable component may be oxygen present in air wherein oxygen ions are passed through the ionic conducting separation components comprising the electrochemical device. Hydrogen can also be separated from a feed stream by fabricating the ions conducting electrolyte layer from a ceramic which is capable of transporting the ionized hydrogen species. These devices can also be readily adapted to function as partial oxidation devices. When the membrane unit is to be utilized for producing synthesis gas, the membrane module is heated to a temperature ranging from 700° to 1200°C, preferably from 800° to 1000°C. A feedstock comprising light hydrocarbons such as methane, natural gas, ethane or any available light hydrocarbon mixture is introduced into passageways 25 and an oxygen-containing gaseous mixture is introduced into the porous supports 22 of each membrane unit 20 by passage into manifold 35 via manifold inlet 45. The oxygen-containing gaseous mixtures flows into porous supports 22 of each membrane unit 20 wherein oxygen is ionized and passed across the dense multicomponent metallic oxide layer 21. The feedstock contacts oxygen ions which are formed at the surface of dense layers 21 resulting in the formation of synthesis gas. The feedstock to be utilized in carrying out the synthesis gas reaction is preferably natural gas which may be utilized straight from the wellhead or produced industrially by making a composition having about 70 percent by weight of methane, about 10 percent by weight of ethane, 10 percent to 15 percent by weight of carbon dioxide with the balance comprising smaller amounts of propane, butane and nitrogen. The feedstock may optionally be diluted with any inert diluent such as nitrogen, helium and the like. Suitable catalysts include conventional catalysts for producing synthesis gas as are well known in the art. The membrane module according to FIG. 1 may also be utilized to produce unsaturated hydrocarbons. The process is conducted in a manner analogous to the preparation of synthesis gas wherein the membrane module is heated to a temperature in excess of 500°, preferably from 800° to 1100°C. Thus, the feedstock and oxygen-containing gaseous mixture are passed through the membrane module in the same path as the feedstock and oxygen-containing gaseous mixture discussed in the synthesis gas reaction description. The feedstock may comprise any fully or partially saturated hydrocarbon which is susceptible to dehydrogenation and which is stable at operating temperatures in either its saturated or unsaturated form. Representative feedstocks include aliphatic hydrocarbons containing 1 to 6 carbon atoms, cycloaliphatic hydrocarbons containing 5 or 6 carbon atoms, aromatic compounds having an aliphatic moiety of 2 to 6 carbon atoms. Preferred feedstocks include ethane, propane, ethylbenzene and mixtures containing the same. The feedstock may optionally be diluted with any inert diluent such as nitrogen, helium and the like. Suitable catalysts include Shell 105 catalyst which comprises about 90% iron oxide, 4% chromium oxide and 6% potassium carbonate. FIG. 2 presents a sectional view of the planar solid-state module of FIG. 1. FIG. 2 presents three general embodiments of membrane units which are suitable for practicing the present invention. Referring to FIG. 2, membrane units 20a, 20b, and 20c each possess a dense multicomponent metallic oxide layer 21 which is situated contiguous to porous support 22. Thus, membrane unit 20a represents the most general membrane unit of the planar modules of the present invention. Membrane unit 20b of FIG. 2 presents an alternate embodiment which comprises a symmetrical arrangement of layers bounded by dense layer 21. Dense layer 21 is contiguous to support layer 22. Situated adjacent to and contiguous with the support layer 22 are a first porous layer 23 and a second porous layer 24. As noted in the cross-section of membrane unit 20b, the membrane unit possesses symmetry wherein the second porous layer 24 forms the interior portion of the membrane unit onto which a first porous layer 23 is deposited on both sides of the second porous layer 24. Thus, porous support 22 and first and second porous layers 23 and 24, respectively, provide an integral support for the dense separating layer which can withstand the pressure differential exerted on opposite sides of the dense multicomponent metallic layer of the membrane unit during operating conditions. The first and second porous layers of membrane unit 20b can be individually deposited such that the second porous layer has a larger average pore radii than the first porous layer 21. Any number of porous layers can be used such that the respective porous layers form a gradient having an average pore radius increasing from 0.5 to about 10 micrometers or more moving away from the interface with the porous support. These porous layers can be fabricated by starting with a green state formed of a plurality of layers wherein each respective layer comprises successively larger particles. A preferred technique for manufacturing ultrathin solid state membranes is presented in United States Patent Serial No. 5,160,618 issued 11/3/92, which is assigned to Air Products and Chemicals, Inc., Allentown, PA. Alternately, the membrane unit 20b can be fabricated such that each respective porous layer has an average pore radius which progressively increases as a function of distance from the porous support. Membrane unit 20c represents an adaptation of membrane unit 20b wherein the second porous layer 24 of membrane unit 20b is replaced by a channeled layer 26. Channeled layer 26 provides channels for receiving oxygen which has permeated dense separating layer 21, passed through porous support 22 and porous layer 23 into the channels of channeled layer 26 for collection as described in this Specification. FIG. 3 presents an exploded perspective view of another embodiment of the present invention. Planar solid-state electrochemical module 300 comprises an array 315 of membrane units 320 wherein each membrane unit comprises a dense multicomponent metallic oxide layer 321 which is supported by and contiguous with a channel-free porous support 322 having connected through porosity. The plurality of membrane units 320 are separated by passageways 325 for contacting the oxygen-containing gaseous mixture with the dense layers 321 of membrane units 320. The array of membranes 315 are traversed by conduit 335 having opening 345 and conduit 345 having opening 350. Conduits 335 and 345 are placed in flow communication with porous supports 322 of each membrane unit 320 and are secured to the membrane array by conduit collar 337 and a conduit collar (not shown) associated with conduit 345. Conduit collar 337 provides a gas-tight seal between conduit 335 and the array 315 of the membrane units thereby preventing leakage. The collar 337 can be chosen from a wide variety of materials such as oxidation-resistant ceramics, such as ceria or calcia doped ceria, which have a thermal expansion coefficient which is compatible with that of the multicomponent metallic oxide with which the collars are associated. The material used for the collars may also be ion-conducting. Other suitable materials include any inert material which has a thermal expansion coefficient comparable to that of the multicomponent metallic oxide, such as stainless steel or forsterite (a composite magnesium silicate oxide). The collars may be secured to the conduit 335 and the array 315 of membrane unit by co-sintering or by applying a high temperature material such as aluminosilicate glass. When the membrane module of FIG. 3 is to be utilized for producing synthesis gas, the membrane module is heated to a temperature ranging from 700° to 1200°C, preferably from 800° to 1000°C. A feedstock comprising light hydrocarbons such as methane, natural gas, ethane or any available light hydrocarbon mixture is introduced into passageways 325 and an oxygen-containing gaseous mixture is introduced into the porous supports 322 of each membrane unit 320 by passage into conduit 335 via conduit inlet 345. The oxygen-containing gaseous mixtures flows into porous supports 322 of each membrane unit 320 wherein oxygen is ionised and passed across the dense multicomponent metallic oxide layer 321. The feedstock contacts oxygen ions which are formed at the surface of dense layers 321 resulting formation of synthesis gas. The feedstock to be utilized in carrying out the synthesis gas reaction is preferably natural gas which may be utilized straight from the wellhead or produced industrially by making a composition having about 70 percent by weight of methane, about 10 percent by weight of ethane, 10 percent to 15 percent by weight of carbon dioxide with the balance comprising smaller amounts of propane, butane and nitrogen. The feedstock may optionally be diluted with any inert diluent such as nitrogen, helium and the like. Suitable catalysts include conventional catalysts for producing synthesis gas as are well known in the art. The membrane module according to FIG 3 may also be utilized to produce unsaturated hydrocarbons. The process is conducted in a manner analogous to the preparation of synthesis gas wherein the membrane module is heated to a temperature in excess of 500°, preferably from 800° to 1100°C. Thus, the feedstock and oxygen-containing gaseous mixture are passed through the membrane module in the same path as the feedstock and oxygen-containing gaseous mixture discussed in the synthesis gas reaction description. The feedstock may comprise any fully or partially saturated hydrocarbon which is susceptible to dehydrogenation and which is stable at operating temperatures in either its saturated or unsaturated form. Representative feedstocks include aliphatic hydrocarbons containing 1 to 6 carbon atoms, cycloaliphatic hydrocarbons containing 5 or 6 carbon atoms, aromatic compounds having an aliphatic moiety of 2 to 6 carbon atoms. Preferred feedstocks include ethane, propane. ethylbenzene and mixtures containing the same. The feedstock may optionally be diluted with any inert diluent such as nitrogen, helium and the like. Suitable catalysts include Shell 105 catalyst which comprises about 90% iron oxide, 4% chromium oxide and 6% potassium carbonate. FIG. 4 is an exploded view of the planar solid-state electrochemical module of FIG. 3 which illustrates three membrane unit embodiments, each which present a dense multicomponent metallic oxide layer which is supported by a channel-free porous support have connected through porosity. Membrane units 320a, 320b, and 320c each possess a dense multicomponent metallic oxide layer 321 which is situated contiguous to porous support 322. Thus, membrane unit 320a represents the most general membrane unit of this embodiment. Membrane unit 320b of FIG. 4 presents an alternate embodiment wherein the membrane unit 320b comprises a symmetrical arrangement of layers bounded by dense layer 321. Dense layer 321 is contiguous to support layer 322. Situated adjacent to and contiguous with the support layer 322 are a first porous layer 323 and a second porous layer 324. Membrane unit 320b possess symmetry wherein the second porous layer 324 forms the interior layer of the membrane unit onto which a first porous layer 323 is deposited on both sides of the second porous layer 324. Thus, porous support 322 and first and second porous layers 323 and 324, respectively provide an integral support for the dense separating layer which can withstand the pressure differential exerted on opposite side of the membrane unit during operating conditions. The porous layers of this embodiment can be fabricated utilizing the methods presented under FIG. 2. Membrane unit 320c represents an adaptation of membrane unit 320b wherein the second porous layer 324 of membrane unit 320b is replaced by channeled layers 326, 327 and 328. Channeled layer 328 is situated between channeled layers 326 and 327 creating a network of channels which are in flow communication with conduits 335 and 345. Thus, channeled layers 326, 327 and 328 provide channels for receiving oxygen which has permeated dense separating layer 321, passed through porous support 333 and porous layer 323 into the channels of channeled layer 326 for collection as described in this Specification. FIG. 5 presents an exploded view of a preferred embodiment of a planar membrane unit suitable for incorporation into the planar solid-state electrochemical module illustrated in FIG. 3. Membrane unit 320c possesses a symmetrical array of layers wherein the outermost layer of the membrane unit comprises a dense layer 321 and the innermost layer is a third channeled layer 328. The third channeled layer is contiguous to a first channeled layer 326 and a second channeled layer 327 wherein the channels of third channeled layer 328 are positioned is a direction substantially perpendicular to the channels in channeled layers 326 and 327. The channels of channels layers 326, 327 and 328 are in flow communication with conduits 335 and 350. Conduit collar 337 serves to secure conduit 335 to membrane unit 320c. Situated between porous support 322 and the third channeled layer 328 are a first porous layer porous layer 323a and second porous layer 323b. Under operating conditions, an oxygen-containing gaseous mixture is placed in flow communication with dense layer 321 and oxygen is ionized and transferred through the dense layer 321 passing through the porous support 322, through first porous layer 323a, second porous layer 323b and into channeled layers 326, 327 and 328 which are in flow communication with conduits 335 and 350. Oxygen is collected via conduit opening 340 (not shown) and 350. FIG. 6 presents a top view of a housing suitable for receiving the planar membrane modules of the present invention. Housing structure 610, typically formed of a stainless steel pipe or conduit, is sized to a diameter capable of receiving planar module unit 620a, 620b, 620c and 620d. As depicted in FIG. 6, planar module units 620a and 620b are linked in series and planar module 620c and 620d are linked in series. Housing structure 610 is packed with insulation 615 in order to facilitate heat transfer between hot air which is passed through housing structure 610 into the passageways between the individual membrane units of the respective planar modules. The heated oxygen-containing gaseous mixture is in flow communication with the dense multicomponent metallic oxide layers of the respective membrane units of the gas separation modules 620a, 620b, 620c and 620d. Oxygen residing at the surface of the dense separating layer is caused to ionize and transfer through and into the dense separation layer of each membrane unit and to recombine into molecular oxygen in the porous support of each respective gas separation unit Oxygen separated from the oxygen-containing gaseous mixture within membrane module 620a and 620b are collected via conduits 630 and 650. Oxygen separated by gas separation module 620c and 620d are collected in conduit 635 and 655. Thus, oxygen separated from the plurality of planar modules is collected in conduits 640 and 660, which conduits exit housing 610 via housing openings 635 and 665. Planar modules 620a, 620b, 620c and 620d are fixably attached to housing structure 610 by supporting means (not shown) as is conventionally known in the art. The oxygen-containing gaseous mixture to be separated into an oxygen stream and an oxygen-depleted stream can be heated by any conventional means including gas-fired turbines, conventional heat exchangers and catalytic combustors. Having described in detail the embodiments of the planar membrane modules, the following information is provided to further describe the membrane units which form the membrane modules as well as the materials and methods for making the same. The porous support may be fabricated from an inert material in the sense that the material does not conduct oxygen ions and/or electrons at process operating conditions, or a multicomponent metallic oxide material of the same or different composition with respect to the dense layer of the membrane module. Preferably, the dense multicomponent metallic oxide layer comprises a multicomponent metallic oxide and the porous support comprises a multicomponent metallic oxide. Representative examples of such suitable materials suitable for fabricating the porous support which do not conduct oxygen ions and electrons at elevated temperatures include alumina, ceria, silica, magnesia, titania, a high temperature oxygen compatible metal alloy, a metal oxide stabilized zirconia and compounds and mixtures thereof. However, the porous support is typically fabricated from a multicomponent metallic oxide material having thermal expansion properties which are compatible with the dense multicomponent metallic oxide layer. As described in the patent application from which this patent application claims priority, suitable compositions for use in fabricating the dense multicomponent metallic oxide layer an/or the porous support of the membrane units depicted in the FIGS. 1 through 6. are represented by the formula A x A' x' A" x" B y B' y' B" y" O 3-z , where A,A',A" are chosen from the group comprising Groups 1, 2 and 3 and the F block lanthanides; and B,B',B" are chosen from the D block transition metals according to the Periodic Table of the Elements adopted by the IUPAC wherein 0<x≤1, 0≤x'≤1, 0≤x"≤1, 0<y≤1, 0≤y'≤1, 0≤y"≤1, 1.1>x+x'+x">0.9 , 1.1>y+y'+y">0.9 and z is a number which renders the compound charge neutral. Preferably, A, A' or A" of the enumerated formula is a Group 2 metal selected from the group consisting of calcium, strontium, barium and magnesium. Multicomponent metallic oxides presented in the patent application from which this application depends are represented by the formula La x A' x' Co y Fe y' Cu y" O 3-z wherein x+x'=0.9-1.1 , y+y'+y"=0.9-1.1 with the proviso that y' and y" are greater than zero and less than or equal to 0.4, and A' is selected from strontium, barium or calcium. The planar dense layer is preferably formed from a multicomponent metallic oxide selected from the group consisting of La 0.2 Ba 0.8 Co 0.8 Fe 0.2 O 3-z , Pr 0.2 Ba 0.8 Co 0.8 Fe 0.2 O 3-z , La 0.2 Ba 0.8 Co 0.6 Cu 0.2 Fe 0.2 O 3-z , La 0.2 Sr 0.8 Co 0.4 Fe 0.4 Cu 0.2 O 3-z , La 0.4 Sr 0.6 Co 0.4 Fe 0.4 Cu 0.2 O 3-z , La 0.3 Sr 0.7 Co 0.8 Fe 0.1 Cu 0.1 O 3-z and SrCo 0.4 Fe 0.4 Cu 0.2 O 3-z . The thickness of the porous support of each membrane unit can be varied to ensure sufficient mechanical strength of the membrane unit. The planar porous support preferably has an average pore diameter of less than 6 times the thickness of the planar dense multicomponent metallic oxide layer. The planar dense multicomponent metallic oxide layer of each membrane unit typically has' a thickness ranging from 0.01 micrometer to about 500 micrometers. The inert porous layer can be formed from materials which do not conduct electrons but which conduct oxygen ions, such as a high temperature oxygen compatible metal alloy, metal oxide-stabilized zirconia such a yttria-stabilized zirconia and calcium-stabilized zirconia or materials which do not conduct electrons or oxygen ions, such as alumina, magnesia, silica, titania and compounds and mixtures thereof. Any combination of inert porous layers and porous multicomponent metallic oxide layers can be utilized so long as their coefficients of thermal expansion are compatible and chemical reactions are minimized between the respective layers at membrane operating temperatures. Thin dense layers of the desired multicomponent metallic oxide having a thickness ranging from 100 micrometers to about 0.01 micrometers in thickness can be deposited onto the enumerated porous layers by known techniques. For example, the membrane composites can be manufactured by first forming a porous body from relatively coarse sized particles of the multicomponent metallic oxide. A slurry of finer particles of the same material or a similar, compatible multicomponent metallic oxide may then be coated onto the porous material and cured to the green state, the two layer system then being fired to form the composite membrane. Multicomponent metallic oxides suitable for practicing the present invention are referred to as "mixed" conducting oxides because such multicomponent metallic oxides conduct electrons as well as oxygen ions at elevated temperatures. A material which primarily demonstrates electronic conductivity can be combined with a material which primarily demonstrates ionic conductivity to form a composite which demonstrates mixed conductivity. The multicomponent metallic oxides of the claimed invention may be prepared according to conventional methods including mixing and firing a desired stoichiometric ratio of the respective metallic oxides making up the multicomponent metallic oxide, thermally decomposing nitrates and acetates and utilizing the citric acid preparation method. Each of these methods is well known in the art and is suitable for making the multicomponent metallic oxides of the claimed invention. The porous layers act as a compatible mechanical support for the dense multicomponent metallic oxide layer and provide two interacting diffusion paths for oxygen; through the pores, and through the solid. Surface kinetic rate limitations for gas-solid oxygen exchange are mitigated by the availability of a large "active" surface area in the small pore structure of the support, especially in the vicinity of the dense layer. On the other hand, the effect of the small pores in hindering diffusion is mitigated by fast ionic conduction in the solid. The channeled layers may be fabricated from materials which possess connected through porosity or dense materials which do not possess connected through porosity. The channeled layers may be fabricated from an inert material in the sense that the material does not conduct oxygen ions or electrons at process operating conditions, or a multicomponent metallic oxide material of the same or different composition with respect to the dense layer or the porous support of the membrane module. As such, suitable materials are those previously described as suitable for fabricating the dense multicomponent metallic oxide layer and the porous support The composite membranes can be prepared by applying a dense layer of a desired multicomponent metallic oxide onto the desired porous substrate by conventional chemical vapor deposition techniques followed by sintering to obtain the desired dense layer. In order to obtain an optimal dense coating, a smaller average pore radius in the surface of the porous support may be used compared to the average pore radius in the bulk. This may be achieved by using two or more porous layers which differ in properties such as pore radius and porosity. EXPERIMENTAL SECTION The following examples are provided to further illustrate embodiments of the present invention and are not intended to limit the scope of the attached claims. EXAMPLE 1 PREPARATION OF La 0.2 Ba 0.8 Co 0.62 Fe 0.21 Cu 0.21 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from La 0.2 Ba 0.8 Co 0.52 Fe 0.21 Cu 0.21 O 3-z . This composition was prepared by a powder preparation technique wherein 1.95 parts by weight of La 2 O 3 , 9.45 parts by weight of BaCO 3 , 2.78 parts by weight of CoO, 1.00 part by weight of Fe 2 O 3 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was air milled to about 1-5 micrometers particle size and combined with a plasticizer, binder and toluene solvent to form a slip suitable for tape casting. EXAMPLE 2 PREPARATION OF La 0.2 Sr 0.8 Co 0.41 Fe 0.41 Cu 0.21 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from La 0.2 Sr 0.8 Co 0.41 Fe 0.41 Cu 0.21 O 3-z . This composition is the example of a so-called B-site rich composition, where (y+y'+y")/(x+x') is greater than 1.0. This composition was prepared by a powder preparation technique wherein 1.95 parts by weight of La 2 O 3 , 7.07 parts by weight of SrCO 3 , 1.84 parts by weight of CoO, 1.96 parts by weight of Fe 2 O 3 and 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was air milled to about 1-5 micrometers particle size. The multicomponent metallic oxide was combined with a plasticizer, binder and toluene solvent to form a slip suitable for tape casting. The slip was cast into a tape and dried using standard methods. Disk-shaped membranes were cut from the tape using standard methods. The disks were fired in air in a controlled manner to remove the plasticizer, binder and toluene solvent and to sinter the tape into a dense membrane. EXAMPLE 3 PREPARATION OF La 0.4 Sr 0.6 Co 0.41 Fe 0.41 Cu 0.21 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from La 0.4 Sr 0.6 Co 0.41 Fe 0.41 Cu 0.21 O 3-z . This composition was prepared by a powder preparation technique wherein 3.90 parts by weight of La 2 O 3 , 5.30 parts by weight of SrCO 3 , 2.92 parts by weight of CoCO 3 , 1.96 parts by weight of Fe 2 O 3 and 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was ball milled to about 1-5 micrometers particle size and combined with a plasticizer, binder and toluene solvent to form a slip suitable for tape casting. EXAMPLE 4 PREPARATION OF La 0.3 Sr 0.7 Co 0.82 Fe 0.11 Cu 0.11 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from La 0.3 Sr 0.7 Co 0.82 Fe 0.11 Cu 0.11 O 3-z . This composition was prepared by a powder preparation technique wherein 5.59 parts by weight of La 2 O 3 , 11.81 parts by weight of SrCO 3 , 11.15 parts by weight of CoCO 3 , 1.00 part by weight of Fe 2 O 3 and 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was air milled to about 1-5 micrometers particle size and combined with a plasticizer, binder and toluene solvent to form a slip suitable for tape casting. EXAMPLE 5 PREPARATION OF La 0.2 Sr 0.8 Co 0.42 Fe 0.42 Cu 0.21 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from La 0.2 Sr 0.8 Co 0.42 Fe 0.42 Cu 0.21 O 3-z . This composition was prepared by a powder preparation technique wherein 1.95 parts by weight of La 2 O 3 , 7.07 parts by weight of SrCO 3 , 1.88 parts by weight of CoO, 2.01 parts by weight of Fe 2 O 3 and 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was ball milled to about 1-5 micrometers particle size and combined with a plasticizer, binder and toluene solvent to form a slip suitable for tape casting. EXAMPLE 6 PREPARATION OF SrCo 0.42 Fe 0.42 Cu 0.21 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from SrCo 0.42 Fe 0.42 Cu 0.21 O 3-z . This composition was prepared by a powder preparation technique wherein 8.84 parts by weight of SrCO 3 , 2.99 parts by weight of CoCO 3 , 2.01 parts by weight of Fe 2 O 3 and 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was air milled to about 1-5 micrometers particle size and combined with a plasticizer, binder and toluene solvent to form a slip suitable for tape casting. EXAMPLE 7 (Comparison) PREPARATION OF La 0.2 Sr 0.8 Co 0.4 Fe 0.4 Cu 0.2 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from La 0.2 Sr 0.8 Co 0.4 Fe 0.4 Cu 0.2 O 3-z . The ratio of. (y+y'+y")/(x+x') equals 1.0 which is the example of a stoichiometric compound. This composition was prepared by a powder preparation technique wherein 2.05 parts by weight of La 2 O 3 , 7.42 parts by weight of SrCO 3 , 1.88 parts by weight of CoO, 2.01 parts by weight of Fe 2 O 3 and 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was air milled to about 1-5 micrometers particle size. EXAMPLE 8 (Comparison) PREPARATION OF La 0.2 Sr 0.79 Co 0.39 Fe 0.31 Cu 0.27 O 3-z A membrane module may be fabricated wherein the dense multicomponent metallic oxide layer of each membrane unit is formed from La 0.2 Sr 0.79 Co 0.39 Fe 0.31 Cu 0.27 O 3-z . The ratio of (y+y'+y")/(x+x') is now less than 1.0 and represents an example of the so-called A-site rich composition. This composition was prepared by a powder preparation technique wherein 1.52 parts by weight of La 2 O 3 , 5.43 parts by weight of SrCO 3 , 2.16 parts by weight of CoCO 3 , 1.15 parts by weight of Fe 2 O 3 and 1.00 part by weight of CuO were ball milled for 12 hours. The mixture was then fired in air to 1000°C for 24 hours followed by cooling to room temperature. The mixture was then ground by ball milling, remixed and refired in air to 1000°C for 24 hours followed by cooling to room temperature. The material possessed a perovskite crystal structure as determined by X-ray diffraction. The perovskite was air milled to about 1-5 micrometers particle size. The multicomponent metallic oxide was combined with a plasticizer, binder and toluene solvent to form a slip suitable for tape casting The slip was cast into a tape and dried using standard methods. Disk shaped membranes were cut from the tape using standard methods. The disks were fired in air in a controlled manner to remove the ptasticizer, binder and toluene solvent and to sinter the tape into a dense membrane. EXAMPLE 9 REACTIVITY OF MULTICOMPONENT METALLIC OXIDE POWDERS WITH ELEVATED PARTIAL PRESSURES OF CARBON DIOXIDE AT HIGH TEMPERATURES The reactivity of the multicomponent metallic oxides prepared in examples 2, 7 and 8 with carbon dioxide was examined by placing powder samples of each composition in a retort inside a furnace. The retort was pressurized to 300 psig with a gas mixture such that the partial pressure of carbon dioxide was 10 psia, the partial pressure of oxygen was 45 psia and the balance was nitrogen. The retort was heated to 850°C and the pressure maintained at 300 psig with constant partial pressures of carbon dioxide and oxygen. The samples were annealed at this condition for 1 week. At the end of the one week period, the samples were cooled to room temperature and examined using x-ray diffraction. X-ray diffraction revealed that all of the samples contained some strontium carbonate. This is shown in Fig. 8 where the most intense SrCO 3 peaks are marked with an asterisk ("*"). Figure 8 illustrates that the multicomponent metallic oxide of Example 2 (so-called B-site rich) had the least strontium carbonate. The multicomponent metallic oxide of Example 8 (so-called A-site rich) had the most strontium carbonate. The amount of reaction between carbon dioxide and the multicomponent metallic oxide is demonstrated by the amount of strontium carbonate identified in each sample by x-ray diffraction. EXAMPLE 10 RATE OF OXYGEN TRANSPORT DEMONSTRATED BY "A-SITE-RICH" AND "B-SITE-RICH" MULTICOMPONENT METALLIC OXIDES UNDER ELEVATED CARBON DIOXIDE AND WATER PARTIAL PRESSURES The oxygen transport performance of the multicomponent metallic oxides membranes prepared in Examples 2 and 8 in the presence a feedstream containing elevated carbon dioxide and water partial pressures was examined in the following experiments. The experiment was initiated by heating the membranes to 850°C and passing air past a first surface of the membrane and purging the second surface of the membrane with helium gas. The pressure on both sides of the membrane was atmospheric. Oxygen was transported though the membrane and mixed with the helium purge stream. The oxygen/helium mixture was analyzed using an oxygen analyzer to determine the oxygen transport rate. During the same experiment, carbon dioxide, oxygen and water vapor were added to the oxygen-containing feedstream placed in contact with the first surface of the membrane. The gases added to the oxygen-containing feedstream were blended such that the ratio of oxygen to water was maintained at 2.4 and the ratio of carbon dioxide to water was maintained at 0.5 The water partial pressure was increased step-wise from 0.09 atm to 0.26 atm with consequent proportional increases in carbon dioxide and oxygen partial pressures. The oxygen flux through the membrane was monitored as a function of the feed gas composition using a oxygen analyzer. FIG. 9 illustrates that the oxygen flux provided by the so-called B-site rich membrane prepared according to Example 2 increases with increasing partial pressures of oxygen, water and carbon dioxide. The oxygen flux provided by the membrane prepared according to Example 8 (the so-called A-site rich membrane) did not change with increasing partial pressures of oxygen, water and carbon dioxide. Those of ordinary skill in the art recognize that increasing the oxygen partial pressure increases the driving force for oxygen transport across the membrane. Therefore, the oxygen flux provided by a multicomponent metallic oxide membrane should increase as the oxygen partial pressure is increased in the feedstream, unless the water and carbon dioxide interfere with the transport of oxygen through the membrane. These experiments demonstrate that membranes prepared from the so-called B-site rich multicomponent metallic oxides provide superior flux performance over membranes prepared from the so-called A-site rich multicomponent metallic oxides when contacted with gaseous mixtures containing elevated partial pressures of carbon dioxide and water. Those skilled in the art will appreciate that the claimed multicomponent metallic oxides of the perovskite-type are suitable for use in solid-state oxygen-producing devices and overcome problems associated with prior art materials which exhibit poor resistance to degradation by process feedstreams containing elevated carbon dioxide and water partial pressures. Thus, the compositions of the present invention are particularly suited toward use in oxygen separation devices wherein high carbon dioxide and water partial pressures shall be employed Applicants set forth their invention as described in the claims which are appended hereto.

Claims: A composition of matter represented by the formula Ln x A' x' A" x" B y B' y' B" y" O 3-z , wherein Ln is an element selected from the f block lanthanides, A' is selected from Group 2, A" is selected from Groups 1, 2 and 3 and the f block lanthanides, and B,B',B" are independently selected from the d block transition metals, excluding titanium and chromium, wherein 0≤x<1, 0<x'<1, 0≤x"<1, 0<y<1.1, 0<y'<1.1, 0<y"<1.1, x+x'+x"=1.0, 1.1>y+y'+y">1.0 and z is a number which renders the compound charge neutral wherein such elements are represented according to the Periodic Table of the Elements adopted by IUPAC. The composition according to Claim 1 wherein Ln is a mixture of lanthanum and at least one element other than lanthanum which is selected from the f block lanthanides. A composition of matter represented by the formula La x A' x' A" x" Co y Fe y' Cu y" O 3-z wherein A' is selected from strontium, barium, calcium or magnesium, A" is selected from Groups 1, 2 and 3 and the f block lanthanides, wherein 0≤x<1, 0<x'<1, 0≤x"<1, 0<y<1.1, 0<y'<1.1, 0<y"<1.1, x+x'+x"=1.0 , 1.1>y+y'+y">1.0 and z is a number which renders the composition charge neutral. The composition of matter according to Claim 3 wherein A' is barium, x is 0.2, x' is 0.8, x" is 0, y is 0.62, y' is 0.21 and y" is 0.21. The composition of matter according to Claim 3 wherein A' is strontium. x is 0.2, x' is 0.8, x" is 0, y is 0.41, y' is 0.41 and y" is 0.21. The composition of matter according to Claim 3 wherein A' is strontium, x is 0.4, x' is 0.6, x" is 0, y is 0.41, y' is 0.41 and y" is 0.21. The composition of matter according to Claim 3 wherein 1 wherein A' is strontium x is 0.3, x' is 0.7, x" is 0, y is 0.82, y' is 0.11 and y" is 0.11. The composition of matter according to Claim 3 wherein A' is strontium, x is 0.2, x' is 0.8, x" is 0, y is 0.42, y' is 0.42 and y" is 0.21. The composition of matter according to Claim 3 wherein A' is strontium, x is 0, x' is 1.0, x" is 0, y is 0.42, y' is 0.42 and y" is 0.21.

Inventors: ALBA PATRICK BENJAMIN, CAROLAN MICHAEL FRANCIS, DYER PAUL NIGEL, MOTIKA STEPHEN ANDREW, ALBA, PATRICK BENJAMIN, CAROLAN, MICHAEL FRANCIS, DYER, PAUL NIGEL, MOTIKA, STEPHEN ANDREW
Applicants: AIR PROD & CHEM, AIR PRODUCTS AND CHEMICALS, INC.
Application year: 1996
Main classification: C01G51
IPC codes: B01D53, C04B35, C01G51, C01B13, B01D71