DUAL FUNCTION COMPOSITE OXYGEN TRANSPORT MEMBRANE

Abstract

A dual function composite oxygen transport membrane having a layered structure of mixed conducting oxygen transport materials on a first side of a porous substrate and a reforming catalyst layer on an opposing second side of the porous substrate. The layered structure of the mixed conducting oxygen transport materials contains an intermediate porous layer of mixed conducting oxygen transport materials formed on the porous substrate with a dense impervious layer of mixed conducting oxygen transport materials over the intermediate porous layer, and an optional surface exchange layer of mixed conducting oxygen transport materials over the dense impervious layer. The layered structure and the reforming catalyst layer are formed in separate steps.

Claims

1-10. (canceled)

11. A method of forming a dual function composite oxygen transport membrane, said method comprising: providing a porous substrate having a first side and an opposing second side; forming a layered structure of mixed conducting materials in a sintered state on the first side of the porous substrate; coating a catalyst layer on the opposing second side of the porous substrate for catalyzing endothermic reactions.

12. The method of claim 11 wherein the layered structure of mixed conducting materials comprises an intermediate porous layer, a dense layer, and an optional surface exchange layer, and the forming of the dense layer and the forming of the catalyst layer is carried out in separate steps.

13. A method of forming a dual function composite oxygen transport membrane, said method comprising: providing a porous substrate having a first side and an opposing second side; forming an intermediate porous layer on the first side of the porous substrate; forming a dense layer over the intermediate porous layer; forming a surface exchange layer over the dense layer; and forming a catalyst layer on the opposing second side of the porous substrate.

14. The method of claim 13 wherein the forming of the catalyst layer is carried out after the forming of the surface exchange layer.

15. The method of claim 13 wherein a catalyst layer coating step in the forming of the catalyst layer is carried out prior to a high temperature sintering step in the forming of the surface exchange layer.

16. The method of claim 13 wherein a catalyst layer coating step in the forming of the catalyst layer is carried out prior to a coating step in the forming of the surface exchange layer.

17. The method of claim 13 wherein a catalyst layer coating step in the forming of the catalyst layer is a wash-coating technique.

Description

BRIEF DESCRIPTION OF THE DRAWING

[0021] While the specification concludes with claims distinctly pointing out the subject matter that applicants regard as their invention, it is believed that the invention would be better understood when taken in connection with the accompanying figures wherein like numbers denote same features throughout and wherein:

[0022] FIG. 1 is a cross-sectional schematic view of a dual function composite oxygen transport membrane;

[0023] FIG. 2 is a process flow diagram for the production of the dual function composite oxygen transport membrane of the present invention;

[0024] FIG. 3 is an alternate process flow diagram for the production of the dual function composite oxygen transport membrane of the present invention;

[0025] FIG. 4 is an alternate process flow diagram for the production of the dual function composite oxygen transport membrane of the present invention;

[0026] FIG. 5 thru FIG. 8 show SEM micrographs of cross-sections of internal surfaces of catalyst layers formed according to present invention.

DETAILED DESCRIPTION

[0027] Dual Function Composite Oxygen Transport Membrane

[0028] With reference to FIG. 1, a sectional, schematic view of a dual function composite oxygen transport membrane 1 of the present invention is illustrated. Dual function composite oxygen transport membrane 1 has a porous substrate 10 that has a first side 18 and an opposing second side 22. The porous substrate serves as a building block of the dual function composite oxygen transport membrane that supports layers of different functional materials located on either side of the substrate. As could be appreciated by those skilled in the art, such dual function composite oxygen transport membrane 1 could be configured as a dual function composite oxygen transport membrane element in the form of a tube or a flat plate. Such composite oxygen transport membrane tube or plate would be one of a series of such elements situated within a device to carry out chemical conversions such as converting a hydrocarbon gas into syngas by endothermic reforming reactions. In an application such as desiring syngas as the product, the dual function composite oxygen transport membrane can be configured as a tube made up of a porous substrate (also referred to as porous support) 10 with a plurality of oxygen transport mixed conducting layers on the first side (outside surface also referred to as exterior surface of the tube) 18, and a reforming catalyst layer on the opposing second side (inside surface also referred to as interior surface of the tube) 22.

[0029] Porous Support

[0030] The porous substrate 10 could be formed from partially stabilized zirconia oxide e.g. 3, 4 or 5 mole % yttria stabilized zirconia or fully stabilized zirconia. Alternatively the porous substrate can be formed from a mixture of MgO and MgAl.sub.2O.sub.4. Alternatively the porous substrate could be a porous metal, although not part of the present invention. As would be appreciated by those skilled in the art, porous substrate 10 also referred to as porous support or porous support layer should provide as open an area as possible while still being able to be structurally sound in its supporting function. Porous support structures for application in composite oxygen transport membranes are best characterized in terms of their porosity, strength and effective oxygen diffusivity. The porous support forms the mechanical support for the active membranes layers, so should have sufficient strength at high temperatures. A typical support structure in this application would have total porosity in the range of about 20 to about 50%. An important property of the porous substrate is the ability to allow gaseous species such as H.sub.2, CO, CH.sub.4, H.sub.2O and CO.sub.2 to readily move through the porous support structure to and from the membrane active layers. The ability of the substrate to allow gaseous transport can be characterized by effective oxygen diffusivity, D.sub.eff O2-N2. For this application it has been determined that a D.sub.eff O2-N2 more than 0.005 cm.sup.2/s measured at room temperature is preferred. The porous substrate should also possess a thermal expansion coefficient not more than 10% different from that of the membrane active layers between room temperature and membrane operation temperature.

[0031] Oxygen Transport Mixed Conducting Layers

[0032] The oxygen transport mixed conducting layers comprise a first mixed conducting layer 12 also referred to as first layer or intermediate porous layer or innermost mixed conducting layer, a second mixed conducting layer 14 also referred to as second layer or dense layer or impervious dense layer, and a third mixed conducting layer 16 also referred to as third layer or surface exchange layer or outermost mixed conducting layer. These layers are formed on the first side 18 of the porous substrate 10. A catalyst layer is formed on the opposing second side 22 of the porous substrate. The dual function composite oxygen transport membrane is specifically designed to function in an environment in which air or oxygen containing stream is introduced and contacted with the outermost mixed conducting layer on the first side 18, and a fuel or other combustible substance is introduced and contacted with the catalyst layer on the opposing second side 22 of the porous substrate 10. The fuel is subjected to combustion supported by permeated oxygen to provide the partial pressure difference necessary to drive oxygen transport and also to heat the membrane to an operational temperature at which oxygen transport will occur. As such, the first layer 12, which, as will be discussed, serves as a porous fuel oxidation layer at which fuel combusts with permeated oxygen. This porous oxidation layer may optionally include a combustion catalyst to promote combustion reactions. In this regard, the term fuel when used in connection with this layer, both herein and in the claims, is not intended to be limiting, but rather, to indicate and include any substance that can be oxidized through permeation of oxygen through the membrane. The second layer 14 is a gas tight active dense layer that is impervious to gas and allows only ion transport, in this case principally oxygen ions, and is commonly referred to as dense layer or dense separation layer. The third layer 16 serves to initially reduce the oxygen in oxygen containing gas such as air contacting the third layer into oxygen ions and thus serves as a porous surface activation layer. Each of the first layer 12, the second layer 14 and the third layer 16 after heating and sintering will preferably each have a thickness of about 10 m to about 100 m.

[0033] Turning attention to the composition of the oxygen transport mixed conducting layers, a stabilized zirconia, namely, Zr.sub.1-x-yA.sub.xB.sub.yO.sub.2- is a common material in all three active membrane layers, namely, the first layer 12, the second layer 14 and the third layer 16. As mentioned above in all of these layers oxygen transport occurs and as such, are active. In order to generate industrially relevant levels of oxygen ion conductivity, A and B are typically Sc, Y, Ce, Al or Ca. Preferably, such stabilized zirconia has a composition given by formula: Zr.sub.0.802Sc.sub.0.180Y.sub.0.018O.sub.2-, often noted as 10Sc1YSZ in literature associated with this class of membrane. However it should be noted that many different combinations of Sc, Y, Ce, Al, Ca or other elements can be substituted to achieve the same end. The first layer 12, intermediate porous layer is configured to have a high surface area where fuel can react with oxygen or oxygen ions that recombine and become available. The second layer 14, the dense layer, functions to separate oxygen from an oxygen containing feed in contact with the third layer, porous surface exchange layer 16 and contains an electronic and ionic conducting phases. As discussed above, the electronic phase of (La.sub.1-xSr.sub.x).sub.wCr.sub.1-y-zFe.sub.yM.sub.zO.sub.3-, where M is a metal: Co, Ni, Ru, x is from about 0.1 to about 0.5, w is from about 0.90 to about 1.0, y is from 0.00 to 1, z is from about 0.00 to about 0.2, and renders the compound charge neutral. The ionic phase is Zr.sub.1-x-ySc.sub.xA.sub.y, O.sub.2-, where x is from about 0.1 to about 0.22, y is from about 0.01 to about 0.04 and A is Y or Ce or a mixture of Y and Ce. The porous support layer 10 is formed of Zr.sub.1-xA.sub.xO.sub.2-, where x is from about 0.05 to about 0.13, A is Y or Sc or Al or Ce or mixtures thereof. The third layer 16, a surface exchange layer is formed from a mixture of particles of (Ln.sub.1-xA.sub.x).sub.wCr.sub.1-yB.sub.yO.sub.3- and 10Sc1YSZ and optionally pore formers. In this layer, Ln is La, Y, Pr, Ce or Sm, A is Ca, Sr, Ba, B can be Mn, Fe, Co Al, Ti or combinations thereof; w is 0.9 to 1.1, x is 0.1 to 0.4 and y is 0.1 to 0.6. The (Ln.sub.1-xA.sub.x).sub.wCr.sub.1-yB.sub.yO.sub.3- and 10Sc1YSZ of this layer after sintering should be present within a first volume ratio of between 2 to 3 and 4 to 1 on a volume percentage basis.

[0034] Reforming Catalyst Layer

[0035] A reforming catalyst layer 30 is located on the second side 22 of the porous substrate 10, separated (spaced apart) from the first layer 12 located on the first side 18 of the porous substrate 10. The formation of this catalyst layer on the second side 22 of the substrate is carried out as a separate step after formation of at least the dense layer 14 on the first side of the substrate. Highly porous reforming catalyst layer accelerates the endothermic hydrocarbon reforming to produce syngas. The separation between the oxygen transport layer and the reforming catalyst layer protects the metal catalysts from exposure to both oxidative and reducing environments and avoids catalyst redox cycles and internal stress buildup.

[0036] Common catalyst coating techniques such as wash-coating, dip-coating, spray deposition, and tape-casting of suspension or sol-gel catalyst slurry can be applied to form the catalyst layer 30. The ingredients of a coating slurry can include one or more of the following: catalyst in the form of metal or metal oxide or metal precursors such as metal nitrate, ceramic support oxides as catalyst carriers, high temperature stabilizers and promoters, organic binders such as polyvinyl butyral (PVB), and optionally one or more pore formers (e.g., carbon black, walnut shell, and Poly-methyl methacrylate with either aqueous or alcohol or toluene solvents. Alternately mixtures of catalyst metal and ceramic carrier powders or commercially available supported catalyst powders can be milled down to desired particle size to prepare the slurry for coating on the substrate layer. Yet another alternate is to pre-coat the porous ceramic composites such as Al.sub.2O.sub.3, YSZ, CeO.sub.2 on the substrate layer of the dual function composite oxygen transport membrane and then impregnate the coated porous ceramic composite with catalyst metal precursors.

[0037] The preferred reforming catalysts include nickel, cobalt, rhenium, iridium, rhodium, ruthenium, palladium, platinum, or their combinations. The catalyst carrier candidates could be high surface area ceramic materials such as Al.sub.2O.sub.3, ZnO.sub.2, CeO.sub.2, TiO.sub.2, pervoskite, pyrochlore, hexaaluminate supports, or mixtures of these materials. The high temperature promoters may include CaO, La.sub.2O.sub.3, MgO, BaO, SrO, Y.sub.2O.sub.3, K.sub.2O, spinel structured materials, or mixtures of these materials. Organic binders not only determine the coating layer adhesion, but also affect the micro-tunnels in the catalyst layer. So it is preferred to be pre-mixed with alcohol solvent (e.g., 12 wt. % PVB in IPA) to enhance its homogenous mix before adding into other ingredients.

[0038] If included, the pore former particle size and loading are preferably in the ranges of 0.5 to 8 m and 15 wt % to 35 wt %, respectively. These pore formers are determined to develop a highly porous network of catalyst coating layer on the porous substrate and prevent blockage of gas flow paths in both catalyst layer and porous substrate. They facilitate desired porosity (preferably 55% to 70% porosity). The particle size of ceramic oxides is preferred to be close to or greater than the diameter of the support layer microchannel to minimize particle impregnation into the support layer and blockage of gas flow through the channel. Thickness of porous catalyst coating can be controlled by slurry viscosity and coating times and is preferred to be greater than about 5 microns, more preferably in the range of about 40 microns to about 150 microns to provide a mechanically stable catalyst layer having sufficient surface area to obtain desired methane conversion. Catalyst layers that are thicker, for example greater than 200 microns, may be structurally less stable, developing cracks and/or delaminate. It is preferred to have thermal shrinkage rate of the catalyst layer to be the same or as close as possible to that of the porous substrate to prevent layer delamination and/or cracking; this can be achieved for example by proper choice of composition and/or thickness of catalyst layer.

[0039] The catalyst coating process can be implemented at different steps in the manufacturing of the dual function composite oxygen transport membrane. As shown in FIG. 2, first all three oxygen transport mixed conducting layers, namely intermediate porous layer, dense layer, and surface exchange layer are formed and then catalyst layer is coated. FIG. 3 show another approach in which only intermediate porous layer and dense layer are first formed, then catalyst layer coated on the inside of the tube followed by surface exchange layer formation over the dense layer to complete the oxygen transport membrane architecture on the outside of the tube. Preferably the catalyst coating step should be introduced after at least dense layer was formed to avoid adverse effects of exposure for long periods of time to high temperatures required to sinter the dense layer; formation of inactive spinel structure of transitional metals such as NiAl.sub.2O.sub.4 in the catalyst layer could be accelerated; the catalyst layer could lose porosity, pore structures as well as surface area, and result in significant catalyst activity reduction.

[0040] It is preferred to integrate catalyst coating right before or after the surface exchange (cathode) layer coating, because these two coating layers are on the opposite side of the membrane and could be sintered by co-firing at the same time. The thicknesses of intermediate mixed conducting porous (anode) layer, dense layer, and surface exchange porous (cathode) layer of a dual function composite oxygen transport membrane can be about 10 m to 100 m each, while the catalyst layer with porosity of 70% and pore size of 6 m can have a thickness of about 20 m to 200 m. Highly porous catalyst surface geometry offers reduced diffusional resistance and provides significantly more catalytic surface area.

[0041] Yet another approach, shown in FIG. 4 is to first form a reactor element comprising at least a first porous support tube (or some other geometry) with mixed conducting oxygen transport layers on the outside surface and a second porous tube (or some other geometry) also with mixed conducting oxygen transport layers on the outside, that are coupled together to provide a continuous flow path to a fluid introduced at one end of the first tube to exit at the other end of the second tube. The catalyst layer is then deposited on the inside surface of the porous support tubes that already have undergone formation of the three oxygen transport mixed conducting layers in a layered structure, namely intermediate porous layer, dense layer, and surface exchange layer on the outside surface of the substrate tube. Such reactor elements are discussed in pending U.S. Patent Publication 2015/0098872, which is incorporated herein by reference.

[0042] Catalyst Layer Benefits

[0043] The dual function composite oxygen transport membrane is operated at relatively high temperature (above 950 C.) and can advantageously produce high quality of syngas while sustaining high oxygen flux performance. Furthermore, the catalytic reforming of hydrocarbon fuels by the dual function composite oxygen transport membrane enhances syngas yield, considerably lowers methane slip and could facilitate elimination of downstream methane removal depending on syngas end use process.

[0044] The endothermic reforming of methane catalyzed by the dual function composite oxygen transport membrane catalyst layer produces hydrogen and carbon monoxide. Some of the hydrogen and/or carbon monoxide produced can diffuse into the porous substrate that is an integral part of the dual function composite oxygen transport membrane, and react with oxygen permeating the dense layer within the dual function composite oxygen transport membrane. The exothermic oxidation reactions consume permeated oxygen, facilitating a difference in partial pressure of oxygen across the membrane.

[0045] The dual function composite oxygen transport membrane can advantageously manage the heat released from oxy-combustion of fuel species with permeated oxygen that occurs in and near the intermediate porous layer. These exothermic reactions generate a considerable amount of heat, some of which supports endothermic reactions such as hydrocarbon reforming catalyzed by the catalyst layer located on the porous substrate. The porous substrate separating the intermediate porous layer and the catalyst layer may have a thickness several orders in magnitude to that of any of these layers. A temperature gradient exists with heat flowing from the oxy-combustion reaction region to the endothermic reforming region. This helps prevent dual function composite oxygen transport membrane oxygen flux reduction due to over cooling from catalytic reforming.

[0046] Fabrication Method

[0047] With reference to FIG. 2, the process flow for producing a dual function composite oxygen transport membrane in accordance with one aspect of the present invention is provided.

[0048] The porous substrate 10 is first formed in a manner known in the art. For example, using an extrusion process the porous substrate could be formed into a tube in a green state and then subjected to a bisque firing at 1050 C. for 4 hours to achieve reasonable strength for further handling. After firing, the resulting porous substrate tube can be checked for porosity and permeability. Then oxygen transport mixed conducting layers, namely intermediate porous layer 12, dense layer 14 and surface exchange layer 16 can be formed on the porous substrate, for example as discussed in U.S. Pat. No. 8,795,417.

[0049] Table 1 lists the ingredients used to form the oxygen transport mixed conducting layers on a tubular porous substrate in the examples described below. The ionic conductive and electronic conductive materials used to form intermediate porous layer and dense layer in the examples are same, however this need not be the case. Zr.sub.0.802Sc.sub.0.180Y.sub.0.018O.sub.2-(d50<0.6 m; from Daiichi Kigenso Kagaku Kogyo Co., Ltd.) was used as ionic conductive material and (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.5Fe.sub.0.5O.sub.3- perovskite powder (d50 in the range of about 0.30 m to about 0.35 m; Praxair Specialty Ceramics) was used as electronic conductive material.

TABLE-US-00001 TABLE 1 Oxygen transport mixed conducting Ionic conductive Electronic conductive Pore layer composite composite Binder Solvent former Intermediate Zr.sub.0.802Sc.sub.0.18Y.sub.0.018O.sub.2 (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.5Fe.sub.0.5O.sub.3 Ferro Toluene Carbon porous B73210 black layer Dense Zr.sub.0.802Sc.sub.0.18Y.sub.0.018O.sub.2 (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.5Fe.sub.0.5O.sub.3 Ferro Toluene N/A layer B73210 Surface Zr.sub.0.802Sc.sub.0.18Y.sub.0.018O.sub.2 (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.3Fe.sub.0.7O.sub.3 Ferro Toluene Carbon exchange B73210 black layer

[0050] For the dense layer, a 120 g batch of slurry was prepared using 51 g of (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.5Fe.sub.0.5O.sub.3- mixed with 69 g of Zr.sub.0.802Sc.sub.0.180Y.sub.0.018O.sub.2-, 60 g Ferro B73210 binder, 255 g Toluene and 1200 g of 1.5 mm diameter YSZ milling media in a 32 oz NALGENE bottle. The mixture was milled for about 2.25 hours or until the particle size of the mixture was in the range 0.3-0.35 m. For the intermediate layer, slurry was prepared by adding 18 g of carbon black (pore former) to the dense layer recipe.

[0051] For the surface exchange layer 16, 51 g of electronic conductive material (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.3Fe.sub.0.7O.sub.3- perovskite powder (from Praxair Specialty Ceramics) was mixed with 69 g of ionic conductive material Zr.sub.0.802Sc.sub.0.180Y.sub.0.018O.sub.2-, 60 g Ferro B73210 binder, 255 g Toluene, 18 g carbon black and 1200 g of 1.5 mm diameter YSZ milling media in a 32 oz NALGENE bottle. The mixture was milled for about 2.25 hours or until the particle size of the mixture was in the range 0.3-0.35 m.

[0052] The tubular porous substrate structure was first coated with the intermediate porous layer by contacting the outside surface of the tubular porous substrate structure with the intermediate layer slurry, at least twice to ensure final thickness was in the range of about 10 to about 30 The dried intermediate layer was then coated by contacting with a dense layer slurry, at least two times to ensure final thickness was in the range of about 10 m to about 30 Resulting coated tubular structure was then dried at room temperature for about 1 to 2 hours before sintering at an elevated temperature above 1350 C.1400 C. for 6 hours in a nitrogen environment. The sintered dense layer was then subjected to a surface exchange layer coating step by contacting the sintered dense layer with a surface exchange layer slurry. This was followed by a drying step (at room temperature for 1 to 2 hours), and a high temperature sintering step (air fired at 1250 C. for half an hour) to complete the surface exchange layer formation.

[0053] Catalyst layer 30 can be formed preferably by a wash-coating technique. As shown in FIG. 2, the catalyst layer formation step can be introduced into the manufacturing process after surface exchange layer formation. The catalyst formation step comprises a catalyst layer coating step, followed by optional air drying and organics burn-off. The catalyst layer coating step comprises contacting the inside surface of the tubular porous substrate structure with a catalyst layer slurry also referred to as catalyst coating layer slurry. The air drying and organics burn-off can be carried out as separate steps or combined into a single step. FIG. 3 shows an alternate process flow for producing a dual function composite oxygen transport membrane wherein the catalyst layer coating step is carried out prior to the surface exchange layer high temperature sintering step, and preferably prior to the surface exchange layer coating step. The catalyst layer organics burn-off step and the surface exchange layer high temperature sintering step can be merged into a single step or can be carried out simultaneously while providing atmospheres and operating conditions (temperatures, pressures, and flows) to the catalyst layer that are appropriate for organics burn-off, and to the surface exchange layer that are appropriate for high temperature sintering. This way process efficiency gains, as well as capital and operating cost savings can be achieved. FIG. 4 shows yet another process flow wherein a plurality of oxygen transport membrane elements having mixed conducting oxygen transport layers on the outside surface are treated to form a catalyst layer on the inside surface of each element, thereby transforming them into dual function composite oxygen transport membrane reactor elements.

[0054] Table 2 lists the ingredients used to form catalyst layer in the dual function composite oxygen transport membrane examples described below.

TABLE-US-00002 TABLE 2 Active Metal Ceramic Pore Dispersant metal precursor Promoter carrier Binder Solvent former agent NiRh Ni(NO.sub.3).sub.26H.sub.2O, TZ-4YS Alpha- 12 wt. % Ethanol PMMA KD-2 Rh(NO.sub.3).sub.3 Al.sub.2O.sub.3 PVB in ethanol Ru (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.8Fe.sub.0.15Ru.sub.0.05O.sub.3- N/A N/A Ferro Toluene Carbon KD-1 B73210 black

Example 1: Nickel-Rhodium Based Catalyst Layer after Surface Exchange Layer Sintering (FIG. 2)

[0055] 25 g of Alpha-phase aluminum oxide (1 m average particle size, 8 to 10 m.sup.2/g surface area, from Alfa Aesar) and 8.5 g of TZ-4YS with 4 mole % yttria stabilized zirconia powder (0.5 m average particle size, from Tosoh Corporation) were dispersed in 200 mL of ethanol and 7 mL of KD-2 dispersant agent (Hypermer). Adding 500 g of 1.5 mm diameter YSZ milling media into the container, the mixture was milled on the roller mill (170 to 175 rpm) for 2 hours. The final particle size of the slurry was in the range of about 0.5 to about 0.8 m. Along with 10 g of pore former poly(methyl methacrylate) PMMA with average particle size of 6 m, 30 g of nickel nitrate hexahydrate Ni(NO.sub.3).sub.2.6H.sub.2O and 0.5 g of Rh(NO.sub.3).sub.3 (both from Sigma-Aldrich) were added into the mixture and mixed for additional one hour. 12% by weight of plastic binder polyvinyl butyral powder was first dissolved in ethanol solvent to enhance its homogenous mixing and then 150 mL of resulting binder solution was slowly added into the slurry mixture. The resulting mixture was further milled for 1.5 hours to form sol-gel slurry.

[0056] The above prepared sol-gel slurry can be used to form a catalyst layer containing Ni and Rh as active metals. Alternately the sol-gel slurry can be prepared without the addition of Rh(NO.sub.3).sub.3 to form a catalyst layer containing Ni as the active metal. The Ni and Rh containing, as well as, Ni only catalyst layer can be formed on the inside of a tubular composite oxygen transport membrane.

[0057] The sol-gel slurry prepared as described above and having a viscosity preferably in the range of about 25 centipoise to about 50 centipoise was used to wash-coat a catalyst layer on the inside surface of a yttria-stabilized zirconia (YSZ) porous substrate tube already coated with oxygen transport mixed conducting layers on the outside surface. The tube, 7 mm ID and 24 inches long had been made from a YSZ paste by a conventional extrusion process followed by bisque firing at elevated temperature. Tubes made this way can have a wall thickness in the range of about 0.7 mm to about 2.5 mm, sufficient to operate at elevated temperatures and pressures. The particular tube used in this example had a wall thickness of 1 mm. The porosity of tube is preferred to be within the range of 25 to 45% for this application. The particular tube used in this example had a porosity of 34%. Oxygen transport mixed conducting layers, namely: surface exchange layer, dense layer, and intermediate porous layer formed on the outside surface of the porous support (YSZ) tube contained mixed ionic and electronic conductive (MIEC) dual-phase materials. After forming the intermediate layer and dense layer on the YSZ support tube, the tube was dried at room temperature and then sintered at an elevated temperature of about 1350 C. to about 1400 C. to have a thickness in the range of about 10 microns to about 30 microns. Then after treating the tube with surface exchange layer slurry, the tube was sintered at an elevated temperature of about 1250 C. to complete the formation of surface exchange layer. The composite oxygen transport membrane tubes prepared in this manner are preferred to have a thickness in the range of about 10 microns to about 30 microns. The particular tube used in this example had an intermediate layer about 15 microns thick, a dense layer about 15 microns thick, and a surface exchange layer about 10 microns thick. Prior to wash-coating, the tube was inspected and appropriate measures taken to remove any dust on the inside surface of the tube, for example by blowing air through the tube. The tube vertically positioned and with one end plugged was gradually filled with sol-gel slurry until the inside of the tube was completely filled. The liquid level slightly dropped due to potential migration of liquid into the porous substrate by capillary action; as needed slurry was added to keep the tube completely filled. After waiting for about a minute the slurry was slowly drained out of the tube, and the tube dried at room temperature by flowing air for about 30 minutes at a low flow rate, in the range of about 10 scfh to about 40 scfh. An inert dry gas can be used instead of air for drying. The organic binder and pore former in the catalyst layer were burned off by vertically fixing the catalyst coated tube in a furnace and heating at a ramp rate of 2 C./min to 600 C. and holding at that temperature for one hour. After the burn-off procedure the tube was cooled to ambient temperature. Catalyst loading in the resulting dual function composite oxygen transport membrane was 0.48 g, as calculated by weighing the tube before wash-coating and after cool down. The SEM microstructure of a cross-section of this catalyst layer shown in FIG. 5 suggests catalyst layer thickness to be about 75 m.

Example 2: Thinner Nickel-Rhodium Based Catalyst Layer after Surface Exchange Layer Sintering (FIG. 2)

[0058] Another porous tube with oxygen transport mixed conducting layers formed on the outside was inspected, cleaned off any dust and filled with catalyst layer sol-gel slurry prepared as described above in Example 1. In this instance the sol-gel inside the tube was held for about 5 seconds rather than for about one minute prior to initiating the draining process. The tube was then subjected to the same steps and conditions of: air drying, organic binder and pore former burn off and cool down as described above. Catalyst loading in the resulting dual function composite oxygen transport membrane was 0.11 g, as calculated by weighing the tube before wash-coating and after cool down. The SEM microstructure of a cross-section of this catalyst layer shown in FIG. 6 suggests catalyst layer thickness to be about 15 m. The sol-gel slurry holding time in the tube prior to draining appears to be an important factor in determining the catalyst layer thickness.

Example 3: Ru-Pervoskite Based Catalyst Layer after Surface Exchange Layer Sintering (FIG. 2)

[0059] 25.5 g of (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.8Fe.sub.0.15Ru.sub.0.05O.sub.3- (particles ranging from 0.2 microns to 0.4 microns, obtained from Praxair Specialty Ceramics) was dispersed in 25 g of toluene solvent (purity>99.5%) along with 5 g of plastic Ferrobinder. Adding 200 g of 1.5 mm YSZ media into the slurry container, the mixture was milled on the roller mill (170 to 175 rpm) for 2 hours. The final particle size of the slurry was about 0.35 microns. Then 4.5 g of pore former such as carbon black (particle size ranging from 0.5 microns to 1.0 micron) was added and milling of the mixture continued for 1 hour. Finally 0.3 g of dispersant (KD-1) dissolved in 15 g of solvent was added to the slurry mixture and milling continued for additional 1 hour. The resulting sol-gel slurry was then used to wash coat a 7 mm ID, 24 inches long YSZ porous tube already coated with oxygen transport mixed conducting layers following similar steps of inspecting, plugging one end, filling, adding slurry to keep the tube completely filled, waiting for about one minute, then draining liquid from the tube, air drying, burning off of organic binder and pore former material, and cool down. In this instance the catalyst loading was 0.6 g. The SEM microstructure of a cross-section of this catalyst layer suggested catalyst layer thickness to be about 62 m.

Example 4: Nickel-Rhodium Based Catalyst Layer and Surface Exchange Layer Co-Firing (FIG. 3)

[0060] 25 g of Alpha-phase aluminum oxide (1 m average particle size, 8 to 10 m.sup.2/g surface area, from Alfa Aesar) and 8.5 g of TZ-4YS with 4 mole % yttria stabilized zirconia powder (0.5 m average particle size, from Tosoh Corporation) were dispersed in 200 mL of ethanol and 7 mL of KD-2 dispersant agent (Hypermer). Adding 500 g of 1.5 mm diameter YSZ milling media into the container, the mixture was milled on the roller mill (170 to 175 rpm) for 2 hours. The final particle size of the slurry was in the range of about 0.5 to about 0.8 Along with 10 g of pore former poly(methyl methacrylate) PMMA with average particle size of 6 m, 30 g of nickel nitrate hexahydrate Ni(NO.sub.3).sub.2.6H.sub.2O and 0.5 g of Rh(NO.sub.3).sub.3 (both from Sigma-Aldrich) were added into the mixture and mixed for additional one hour. 12% by weight of plastic binder polyvinyl butyral powder was first dissolved in ethanol solvent to enhance its homogenous mixing and then 150 mL of resulting binder solution was slowly added into the slurry mixture. The resulting mixture was further milled for 1.5 hours to form sol-gel slurry. The resulting sol-gel slurry was then used to wash coat a 7 mm ID, 24 inches long YSZ porous tube already coated with two of the three oxygen transport mixed conducting layers, namely intermediate porous layer and dense layer only. The wash coating steps were similar to that described in Examples 1 and 2 above, namely: inspecting and removing any dust, plugging one end, filling with sol-gel slurry, adding slurry as needed to keep the tube completely filled, waiting for about one minute, then draining liquid from the tube. The tube was then air dried at room temperature for about 5 minutes with air flowing at a low flow rate of 40 SCFH. Next the surface exchange layer slurry prepared in a manner described above was used to coat the outside of (over) the dense layer. To complete the formation of the surface exchange layer as well as to burn off organic binders and pore former materials in the catalyst layer and the surface exchange layer the tube was first dried at room temperature for about one hour to about two hours, then heated at a ramp rate of 2 C./min to 1250 C. in an air fired furnace and held there for half an hour, and allowed to cool down. In this instance the catalyst loading was 0.52 g. The SEM microstructure of a cross-section of this catalyst layer suggested catalyst layer thickness to be about 80 m.

Example 5: Ru-Pervoskite Based Catalyst Layer and Surface Exchange Layer Co-Firing (FIG. 3)

[0061] 25.5 g of (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.8Fe.sub.0.15Ru.sub.0.05O.sub.3- (particle size range from 0.2 microns to 0.4 microns) was dispersed in 25 g of toluene solvent (purity>99.5%) along with 5 g of plastic Ferrobinder. Adding 200 g of 1.5 mm YSZ media into the slurry container, the mixture was milled on the roller mill (170 to 175 rpm) for 2 hours. The final particle size of the slurry was about 0.35 microns. Then 4.5 g of pore former such as carbon black (particle size ranged from 0.5 microns to 1.0 micron) was added and mixture further milled for 1 hour. Finally 0.3 g of dispersant (KD-1) dissolved in 15 g of toluene was added to the slurry mixture and milled for additional 1 hour. Similar to Example 4, the tube used in this example (7 mm ID and 24 inches long YSZ porous tube) had only intermediate porous layer and dense layer formed on it. The catalyst layer formation steps of inspecting, plugging one end, filling, adding slurry to keep the tube completely filled during the entire duration of about one minute, and draining liquid were similar. The tube was then air dried at room temperature for about 5 minutes with air flowing at a low flow rate of 40 SCFH. Next the surface exchange layer slurry prepared in a manner described above was used to coat over the dense layer. To complete the formation of the surface exchange layer as well as to burn off organic binders and pore former materials in the catalyst layer and the surface exchange layer, the tube was first dried at room temperature for about one hour to about two hours, then heated at a ramp rate of 2 C./min to 1250 C. in an air fired furnace and held there for half an hour, and allowed to cool down. In this instance the catalyst loading was 0.62 g. The SEM microstructure of a cross-section of this catalyst layer shown in FIG. 7 suggests catalyst layer thickness to be about 55 m.

Example 6: Thicker Ru-Pervoskite Based Catalyst Layer (FIG. 3)

[0062] 25.5 g of (La.sub.0.8Sr.sub.0.2).sub.0.98Cr.sub.0.8Fe.sub.0.15Ru.sub.0.05O.sub.3- (particle size range from 0.2 microns to 0.4 microns) was dispersed in 25 g of toluene solvent (purity>99.5%) along with 5 g of plastic Ferrobinder. Adding 200 g of 1.5 mm YSZ media into the slurry container, the mixture was milled on the roller mill (170 to 175 rpm) for 2 hours. The final particle size of the slurry was about 0.35 microns. Then 4.5 g of pore former such as carbon black (particle size ranged from 0.5 microns to 1.0 micron) was added and mixture further milled for 1 hour. Finally 0.3 g of dispersant (KD-1) dissolved in 15 g of toluene was added to the slurry mixture and milled for additional 1 hour. Similar to Example 5, the tube used in this example (7 mm ID and 24 inches long YSZ porous tube) had only intermediate porous layer and dense layer formed on it. The tube was subjected to catalyst layer formation steps of inspecting, plugging one end, filling, and adding slurry to keep the tube completely filled during the entire duration of about one minute. The liquid was then drained and the tube was air dried for five minutes and then filled again with sol-gel slurry. The tube was kept completely filled by adding slurry as needed. After waiting for about a minute, the liquid was drained. In a manner similar to that described above for Example 5, the tube was then air dried at room temperature for about 5 minutes with air flowing at a low flow rate of 40 SCFH. Next the surface exchange layer slurry prepared in a manner described above was used to coat the outside of the dense layer. To complete the formation of the surface exchange layer as well as to burn off organic binders and pore former materials in the catalyst layer and the surface exchange layer, the tube was first dried at room temperature for about one hour to about two hours, then heated at a ramp rate of 2 C./min to 1250 C. in an air fired furnace and held there for half an hour, and allowed to cool down. In this instance the catalyst loading was 0.84 g. The SEM microstructure of a cross-section of the catalyst layer shown in FIG. 8 indicates cracking and delamination of catalyst layer, and suggests catalyst layer thickness to be about 225 m where it remained intact. Therefore, it is preferable to control the catalyst thickness within the range of 40 to 150 m.

[0063] Dual Function Composite Oxygen Transport Membrane Performance

[0064] The dual function composite oxygen transport membrane tubes made in the examples described above with functional layered structures on the outside surface and the inside surface were tested separately using a standard bench-scale reactor setup. The tube was vertically positioned inside a metal shell embedded in an electrically heated chamber. The dual function composite oxygen transport membrane tube was connected to a source of feed gas and an effluent processing system for safely disposing off syngas product. The tube was heated to an operational temperature of about 950 C. The feed gas was prepared using CH.sub.4, CO, H.sub.2, and CO.sub.2 from gas cylinders and steam from a steam source. The results described below were obtained using a feed gas containing 12 mole % CH.sub.4, 11 mole % CO, 52 mole % H.sub.2, 4 mole % CO.sub.2 and 21 mole % H.sub.2O. The feed gas was preheated to about 350 C. prior to feeding to the tube. The flow rate of the feed gas was controlled at achieve a desired space velocity of about 31,000 per hour. Heated air at about 200 C. with a flow rate of 30 SLPM was introduced into the metal shell to flow on the outside of the dual function composite oxygen transport membrane tube in a direction countercurrent to that of feed gas flowing through the tube. The pressure inside the metal shell, that is on the outside of the dual function membrane tube was maintained around 5 psig, and the pressure inside the dual function membrane tube was maintained at a desired value in the range of about 5 psig to about 200 psig. The effluent containing reaction products and unreacted feed species was cooled, water condensed out. The resulting gas stream was sampled and analyzed using a gas chromatograph (GC). The hot air stream leaving the chamber was also cooled and then analyzed for oxygen content using a real-time resolved oxygen analyzer. Table 3 summarizes the results after 100 hours of operation indicating the dual function membranes to have considerably improved methane conversion relative to a membrane that has only oxygen transport functionality. The oxygen transport functionality as indicated by the oxygen flux after 100 hours of stable operation of dual function composite oxygen transport membrane tubes prepared in Examples 1, 3 thru 5 is similar to that of a reference tube that had mixed conducting oxygen transport layers on the outside surface without a catalyst layer on the inside surface. The wash-coating procedure, standardized wash-coating procedure used for forming catalyst layer in these examples involved filling the tube with a slurry containing catalyst layer ingredients, holding the slurry in the completely filled tube for one minute, then draining the slurry followed by air drying and organics burn-off in air. The tubular dual function composite oxygen transport membrane made in Example 2 has similar oxygen flux performance even though a slightly different procedure was followed; the slurry in the completely filled tube was held for considerably less time than one minute, resulting in a thin catalyst layer. In Example 6, however the tube was again refilled with the slurry, the catalyst layer formed was thicker, and the oxygen flux is considerably lower than those of tubes prepared following standardized wash-coating procedure. The thicker catalyst layer could pose higher diffusional resistance to transport of fuel species through the catalyst layer into the porous substrate towards the intermediate porous layer for reaction with permeated oxygen within the membrane, affecting the driving potential for oxygen transport. The results in Table 3 also indicate that the composite oxygen transport membranes with catalyst layer, that is dual function composite oxygen transport membranes achieved considerably higher methane conversion. The catalyst layer thickness appears to be an important factor. The Example 2 membrane that had a thinner catalyst layer, about 15 microns appears to achieve relatively lower methane conversion compared to those having catalyst layer thicknesses in the range of about 50 microns to about 80 microns. The Example 6 membrane that had a thicker catalyst layer of about 225 microns with cracks and delamination in some cross sections, also had relatively lower methane conversion.

TABLE-US-00003 TABLE 3 Catalyst layer thickness, Normalized O.sub.2 CH.sub.4 Example Catalyst type Fabrication Method microns Flux* conversion, % Reference N/A FIG. 2 without N/A 1.00 4.3% catalyst layer steps 1 NiRh FIG. 2 75 0.98 98.6% 2 NiRh FIG. 2 15 1.00 95.4% 3 Ru-Pervoskite FIG. 2 62 0.99 98.8% 4 NiRh FIG. 3 80 0.99 98.2% 5 Ru-Pervoskite FIG. 3 55 1.01 98.9% 6 Ru-Pervoskite FIG. 3 225 0.83 93.8% *Normalized with respect to reference membrane (without catalyst layer)

[0065] Although the present invention has been described with reference to preferred embodiments, as will occur to those skilled in the art, changes and additions to such embodiment can be made without departing from the spirit and scope of the present invention as set forth in the appended claims. The dual function composite oxygen transport membrane, even though described in the context of syngas production are not limited to such uses.