MXPA98003329A - Separator-integrated conductor cooler ionicode electrolito sol - Google Patents

Abstract

A process for producing an oxygen gas stream, a gas stream enriched with oxygen, or a stream of reaction products such as a permeate stream and a gas stream exhausted in oxygen by first separating oxygen from a feed gas stream and then cool at least the permeated stream. The production and cooling of the permeate stream occurs within a single apparatus that has at least one ion transport membrane

Description

- & SEPARATOR-INTEGRATED COOLER OF IONIC CONDUCTOR OF SOLID ELECTROLYTE FIELD OF THE INVENTION The invention relates to a solid electrolyte ion conductor device designed for use in gas separation systems. In particular, the invention relates to solid electrolyte ion conductor systems in which the functions of gas separation, possible reaction and cooling are integrated within a single apparatus. 10 RIGHTS OF THE GOVERNMENT OF THE U. This invention was made with the support of the Government of the United States under the Cooperation Agreement Nb. 70 ANB5H1065 granted by the National Institute of Standards and Technology. The Government of the United States has certain rights in the invention. 15 CROSS REFERENCE The application entitled "Design of Ionic Conductor Reactor of Solid Electrolyte", from E.U. Series No. (Attorney Docket No. D-20352), filed concurrently with this, is incorporated herein by reference. BACKGROUND OF THE INVENTION Non-cryogenic systems for mass oxygen separation, for example, organic polymer membrane systems, have been used to separate selected gases from the air and from other gas mixtures. Air is a mixture of gases that can contain varying amounts of water vapor and, at sea level, has the following approximate composition in volume: Oxygen (20.9%), Nitrogen (78%), Argon (0.94%), with the rest consisting of traces of other gases. However, a completely different type of membrane can be made from certain inorganic oxides. These solid electrolyte membranes are made from inorganic oxides, typified by zirconium oxides and analogs stabilized with calcium or yttrium having a fluorite or perovskite structure. Although the potential of these oxide ceramic materials as gas separation membranes is great, there are certain problems in their use. The most obvious difficulty is that all known oxide oxide ceramics exhibit appreciable oxygen ion conductivity only at elevated temperatures. They usually must be operated above 500 ° C, generally in the range of 600 ° C-900 ° C. This limitation remains despite the great research to find materials that work well at lower temperatures. The solid electrolyte ion conductor technology is described in more detail in the U.S. Patent. No. 5,547,494 to Prasad et al., Entitled "Staged Electrolyte Membrane", which is incorporated herein by reference to more fully describe the state of the art. Recent developments have produced solid oxides that have the ability to conduct oxygen ions at elevated temperatures if a chemical or electrical driving potential is applied. These pressure-driven ionic conductive materials can be used for oxygen stripping of oxygen-containing gas streams if a partial pressure ratio of oxygen sufficient to provide the chemical potential is applied. Since the selectivity of these materials for oxygen is infinite and oxygen flows can be obtained several times greater in magnitude than with polymer membranes, attractive opportunities are created for the production of oxygen as well as for oxidation processes that require oxygen, especially with applications that involve high temperatures. A prominent example is that of gas turbine cycles that typically process a significant amount of excess air, to keep the inlet temperature of the turbine within the capacities of the available materials and therefore have excess available oxygen to recover it I have a sub-product. Advances in the state of the air separation art using ionic conductors of solid electrolyte have been presented in the technical literature. For example, Mazanec et al-, in the U.S. Patent. No. 5,306,411 entitled "Solid Multi-Copiponent Membranes, Electrochemical Reactor Components, Electrochemical Reactors and Membrane Usage, Reactor Components and Reactor for Oxidation Reactions", refers to electrochemical reactors for reacting an oxygen-containing gas with a gas that consumes oxygen and describes a shell and tube reactor with the oxygen-containing gas flowing on one side of the solid electrolytic membrane and the gas that consumes oxygen on the other side. Mazanec et al., However, does not mention publications related to the administration of heat to maintain the membrane surfaces at desired uniform temperatures, flow dynamics to achieve an effective mass transfer or the need to balance the reaction kinetics with conductivity of oxygen ions to maintain the oxygen partial pressure appropriate for the stability of the materials. Kang et al., In Patent No. 5,565,017 of E.U. entitled "Production of Oxygen at High Temperature with Steam Generation and Ehergy", refers to a system that integrates an ion transport membrane with a gas turbine to recover energy from the retained gas stream after it is heated and has been added steam. Kang et al-, in Patent NO. 5,516,359 from E.U. entitled "Integrated High Temperature Method for Oxygen Production", refers to the use of inert gases and gases as sweeping gases for membrane separators. None of the Patents of Kang et al. , describe the design of the enabling device or contemplate the use of ion transport reactors that, by excluding nitrogen from the gas stream reaction products, allow their association as generators of purge or sweep gas streams for transport separators of ions. A tubular solid-state membrane module is described in US Patent No. 5,599,383. from Dyer et al., having a plurality of tubular membrane units, each unit having a porous support of free channels and a dense mixed conductive oxide layer supported thereon. The porous support of each unit is in flow communication with one or more collectors or conduits for discharging oxygen that has penetrated through the dense layer and the porous support. Westinghouse has developed solid fuel cells that have a tubular design, such as that described in the publication presented at PowerGen 1995-Americas Conference in Anaheim, California, on December 5-7, 1995 by Frank P. Bvec and Walter G. Parker , "Solid Oxide Fuel Cell Integrated Power Plants for SureCEL 115 Distributed Energy Applications". This publication relates to tubular solid oxide fuel systems with geometries that have a surface similarity to some of the geometries of the present invention but, nevertheless, the geometries are not related to the functions performed by the solid electrolyte reactors of the invention of the moment. Bvec and Parker disclose a closed odd fuel cell element in which air is supplied to the side of the internal cathode of the solid electrolyte membrane by an internal coaxial tube that results in preheating the air before entering the cathode passage in where oxygen transfer takes place. Bvec and Parker, however, do not mention publications on heat management and flow dynamics. In addition, the Westinghouse device, unlike the present invention, is not a reactor to produce heat or a desired product from the anode side but a fuel cell to produce electrical energy and therefore can not employ mixed or dual conductors. face as the electrolyte. Mens, Westinghouse solid oxide fuel cell designs (see Fig. 4) are also low pressure devices while the reactors of the present invention would typically be high pressure on at least one side of the solid electrolyte membrane . Since the pressure differential between the two sides is small, the subject of sealing is not mentioned, even though it is a significant part of the present invention. The Westinghouse fuel cell designs also highlight a concentric inner tube for the supply air, however, regardless of the practical design problems of the apparatus faced by an ion transport oxygen separator. OBJECTIVES OF THE INVENTION It is therefore an objective of the invention to provide an efficient process using solid electrolyte ion conductor systems in which the functions of gas separation, possible reaction and cooling are integrated into a single apparatus to optimize the use of conventional materials and conventional construction methods. It is also an object of the invention to have the solid electrolyte ion transport systems of the invention integratable to a high temperature cycle such as a gas turbine. It is a further object of the invention to provide the ability to employ a purge stream for the permeate side or anode of the ion transport separator to improve oxygen recovery without interfering with the previously mentioned advantages. It is still another object of the invention to integrate a reaction section in the apparatus which generates a purge stream, consisting of reaction products, within the same tubular passage upstream of the separating section to purge the permeate side, anode of the separator to improve oxygen recovery without interfering with the previously discussed advantages and thus integrate most of the unit operations required for the separation of gases by ion transport membranes in a single apparatus to significantly simplify the process arrangements. SUMMARY OF THE INVENTION The invention comprises a process for producing an oxygen gas stream or an oxygen enriched gas stream as a permeate stream and a gas stream exhausted in oxygen or a retained stream by first separating oxygen from a gas stream of feed containing elemental oxygen and then cooling the oxygen gas stream or the gas stream enriched with oxygen obtained therefrom, within a single separator-cooler apparatus. The separator-cooler apparatus has a separation section and a cooling section and an oxygen product outlet port, wherein the separation section includes an ion transport membrane having a retentate side and a permeate side. The process comprises the steps of: (a) prespressing the feed gas stream; (b) dividing the compressed stream of feed gas into a larger portion of gas stream and a smaller portion of gas stream; (c) heating the largest portion of the gas stream; (d) introducing the largest portion of the gas stream to the separation section of the apparatus; (e) introducing the minor portion of the gas stream to the cooling section of the apparatus near the oxygen product outlet port; (f) removing oxygen from the heated higher portion of the gas stream through the ion transport membrane of the separation section to obtain a stream of hot gas enriched with oxygen on the permeate side of the membrane and a stream of oxygen depleted gas on the retentate side of the membrane; and (g) transferring heat from the gas stream enriched with oxygen to the smaller portion of the gas stream to produce the oxygen gas stream or the product gas stream enriched with oxygen and a minor portion of the heated gas stream, in where the minor portion of the gas stream leaves the apparatus or is cannulated with the hottest portion of the gas stream before the larger portion of hot gas is introduced to the separating portion of the apparatus, and where the gas stream exhausted in oxygen leaves the apparatus. In a preferred embodiment of the invention the separator-cooler apparatus further comprises a reactor section, which includes an ion transport membrane having a retentate side and a permeate side to establish a single reactor-cooler apparatus or a single reactor apparatus -separator-cooler. In the reactor-separator-cooler apparatus, a stream of reactive gas is introduced into the permeate side of the ion transport membrane in the reactor section of the apparatus, to react with a second stream of oxygen gas penetrating through the ion transport membrane near the permeate side of the ion transport membrane, to produce a gas stream reaction products which is used to purge the permeate side of the ion transport membrane in the separation section of the apparatus, and the stream of gases reaction products and the first stream of oxygen gas and any unreacted oxygen from the second stream of oxygen gas combine as the gas stream enriched with oxygen which exits the apparatus, and where the gas stream exhausted in oxygen comes out separately from the appliance. The ion transport membrane of the separation section of the apparatus and the ion transport membrane of the reactor section of the apparatus can be formed integrally, and more preferably, the ion transport membrane of the separation section of the apparatus includes a porous substrate of support and comprises an ion transport material having a high oxygen conductivity at a high oxygen partial pressure and the ion transport membrane of the reactor section of the apparatus comprises a mixed conductive layer having optimum stability at low pressures partial oxygen. The invention also comprises a process for producing a gas stream exhausted in oxygen and a stream of gases reaction products as a permeate stream by first separating oxygen from a stream of feed gas containing elemental oxygen to produce the exhausted gas stream in oxygen and the hot gas stream reaction products and then cool the gas stream reaction products, within a single reactor-cooler apparatus, to obtain the gas stream reaction products. The reactor-cooler apparatus has a reactor section and a cooling section and an output port of reaction products, and the reactor section includes an ion transport membrane having a retentate side and a permeate side. The process involves the steps of: (a) compressing the feed gas stream; (b) dividing the compressed stream of feed gas into a larger portion of gas stream and a smaller portion of gas stream; (c) introducing the largest portion of gas stream into the reactor section of the apparatus; (d) introducing the smaller portion of gas stream to the cooling section of the apparatus near the reaction product outlet port; (e) removing oxygen from the larger portion of gas stream through the ion transport membrane of the reactor section, by introducing a stream of reactive gas to the permeate side of the ion transport membrane in the reactor section of the apparatus to react with the oxygen gas stream that penetrates through the ion transport membrane near the permeate side of the ion transport membrane, to produce the stream of hot gases of reaction products on the permeate side of the ion transport membrane and the gas stream exhausted in oxygen on the retentate side of the ion transport membrane; and (f) transferring heat from the stream of hot gases of reaction products to the smaller portion of gas stream to produce the stream of reaction product gases and the smaller portion of heated gas stream, wherein the smaller portion of The gas stream flows out of the apparatus or is combined with the larger portion of heated gas stream before the larger portion of heated gas is introduced to the reactor portion of the apparatus, and where the gas stream depleted in oxygen also comes out of the gas stream. The invention is applicable to any oxidation or partial oxidation reaction on the permeate side of the ion transport reactor Examples of such applications include burners, dissociation devices, syngas production or other oxidation processes. In the invention, the larger portion of gas stream is heated to an intermediate temperature before being introduced to the reactor section of the In another preferred embodiment of the invention, the gas stream of reaction products is essentially devoid of nitrogen. In another preferred embodiment of the invention, the ion transport membrane of the reactor section of the apparatus and a conduit for carrying the stream of gases reaction products through the chiller section of the apparatus are integrally formed. The invention also comprises a process for producing a gas stream enriched with oxygen and a gas stream exhausted in oxygen by separating oxygen from a stream of feed gas containing elemental oxygen within a reactor-separator apparatus. The reactor-separator apparatus has a separation section and a reactor section, wherein the separation and reaction sections include at least one ion transport membrane having a retentate side and a permeate side. The process comprises the steps of: (a) compressing the feed gas stream; (b) introducing the feed gas stream compressed to the apparatus and transferring heat from a stream of gases reaction products; (c) removing oxygen from the hot feed gas stream through the ion transport membrane in the reactor section of the apparatus to produce a gas stream reaction products on the permeate side of the membrane and the gas stream oxygen depleted on the retentate side of the membrane; and (d) removing additional oxygen from the partially exhausted gas stream in oxygen by transport through the ion transport membrane in the separation section of the apparatus to produce the oxygen-depleted gas stream on the retentate side of the membrane . A stream of reactive gas is introduced into the permeate side of the ion transport membrane in the reactor section of the apparatus to react with the oxygen carried through the ion transport membrane near the permeate side of the membrane to produce the current of gases reaction products which is used to purge the permeate side of the ion transport membrane in the separation section of the apparatus, and the gas stream reaction products and the unreacted transported oxygen are combined as the gas stream enriched with oxygen leaving the apparatus. Preferably, the gas stream exhausted in oxygen comes out separately from the apparatus. In a preferred embodiment of the invention, the ion transport membrane of the separation section of the apparatus and the ion transporting bushing of the reactor section of the apparatus are integrally formed. In another preferred embodiment of the invention, the ion transport membrane of the separation section of the apparatus includes a porous support substrate and comprises an ion transport material having high oxygen ion conductivity at a high oxygen partial pressure and The ion transport membrane of the reactor section of the apparatus comprises a mixed conductive layer having optimum stability at partial pressure of low oxygen. In still another preferred embodiment of the invention, the reactive gas is heated before being introduced into the reactor section of the apparatus.

Cone is used herein the term "elemental oxygen" means any oxygen that is not combined with any other element of the Periodic Table. Although typically found in diatomic form, elemental oxygen includes simple oxygen atoms, triatomic ozone, and other forms without combining with other elements. Coto is used here, the term "reactor" means a separator in which the transported oxygen is subjected to a chemical reaction and the oxygen is consumed thereby. Although the terms "reactor" and "separator" are sometimes used herein to describe different sections of an apparatus in accordance with the present invention, the term "separator" is also used herein to broadly describe the reactor and / or separator sections. BRIEF DESCRIPTION OF THE DRAWINGS Other objects, aspects and advantages of the invention will occur to those skilled in the art of the following description of preferred embodiments of the invention and the accompanying drawings, in which: Fig. IA is a diagram schematic of one embodiment of the invention showing a basic design of a solid electrolyte ion conductor conductor-separator-cooler featuring an ion transport tube with a closed end and free floating; Fig. IB is a schematic diagram showing a detail of how the ion transport tube of the separation section of the apparatus can be connected with = 1 metal tube of the chiller section of the apparatus by welding or mechanically joining the tubes to make a stamp; Fig. 2 is a schematic diagram of another embodiment of the invention showing a basic design of a solid electrolyte ion conductor conductor-separator-cooler that highlights an ion transport through the tube with a sliding seal; Fig. 3 is a schematic diagram of one embodiment of the invention showing a basic design of a solid electrolyte ion conductor-conductive separator-cooler that highlights an ion transport tube with a closed and free-floating extraneous; Fig. 4 is a schematic diagram of another embodiment of the invention showing a basic design of a solid electrolyte ion conductor conductor-separator-cooler that features an ion transport tube with a closed and free-floating extraneous; Fig. 5 is a schematic diagram of one embodiment of the invention showing a basic design of a solid electrolyte ion conductor reactor-cooler that highlights an ion transport through a tube with a sliding seal and having the ability to to cool both retained and permeated streams thereof; Fig. 6 is a schematic diagram of another embodiment of the invention showing a basic design of a solid electrolyte ion conductor reactor-cooler that features an ion transport tube with a closed end and free floating; Fig. 7 is a cross-sectional diagram showing an ion transport tube wherein the ion transport membrane of the reactor section of the apparatus, the ion transport membrane of the separation section of the apparatus, and the ion transport pipe. the cooling section of the apparatus are integrally formed; Fig. 8 is a schematic diagram showing a complete oxygen / nitrogen separation cycle using a reactor-separator-cooler of the present invention; and Fig. 9 is a schematic diagram showing an ion transport reactor-separator-cooler of the present invention integrated into a gas turbine cycle. DETAILED DESCRIPTION OF THE INVENTION Some of the key problems that are mentioned by the present invention involve minimizing resistance to gaseous diffusion, avoiding excessive stresses derived from expansion and thermal and compositional contraction and sealing the ion transport elements within the apparatus of ion transport. The problem is ultimately aggravated by the fact that the operating temperature of the ion transport hose is in the range of 500 ° C to 1, 100 ° C. The invention, which in preferred embodiments employs ion transport elements in the form of tubes, eliminates the aforementioned efforts using tubes that are closed end and free floating in that extraneous. The seal prob- lem is also substantially alleviated by combining the functions of separation and / or ion transport reaction with the cooling of oxygen in a single apparatus. As discussed below, this preferably allows tube-to-tube plate joints to be maintained in a temperature range of 180 ° C to 300 ° C and allows the use of conventional techniques such as welding or mechanical means to effect a seal. In the preferred approach, part of the feed air does not pass through the quanator or heater and serves as a heat sink to cool the gas stream of oxygen product or reaction products that exit. The resistance to diffusion in high pressure gas is minimized by an array of deflectors that provide high transverse flow speeds or small hydraulic radii of the flow passages. Other functions, such as indirect heating of a third gas stream or separation of a stream of oxygen product by a suitable solid electrolyte membrane, are integrated to achieve optimum simplicity satisfying even the operational requirements discussed in the previous paragraph. This invention provides all the functional requirements that solid electrolyte reactors have to meet to be feasible and practical and describes how the reactor function can be advantageously combined with other operations. Specifically, the invention incorporates heat transfer means such that the heat of reaction is removed from the solid electrolyte ion conductor elements, thereby maintaining the ionic conductor elements of solid electrolyte at sufficiently constant temperature. This is achieved by varying the local heat transfer coefficients as necessary by selecting the appropriate heat transfer surface geometry and the appropriate local flow rates. At the same time, the transfer of efficient mass of oxygen to the surface of the cathode and of reactant to the surface of the anode of the manbrana is ensured either by high turbulence or by narrow dimensions of the passage. In addition, attention is paid to the need to maintain the partial pressure of oxygen at or near the anode surface at a sufficiently high level for a long life of the specific mixed or double-sided conductor employed by the balance of local oxygen flow and the reaction kinetics. This is achieved by selecting a manbrana with thickness and conductivity of appropriate ions on the one hand and controlling the catalytic activity by catalyst material and / or surface area on the other. Cano was mentioned before, the present invention uses many fundamental approaches to reduce or eliminate the problances found in an ion transport separating apparatus. The major advantages present in at least some of the various embodiments of the invention presented in the figures are as follows: I (i) closed tube ends and free float avoid stresses due to differential or compositional thermal expansion; (ii) the incorporation of the cooler in the ion transport separator apparatus avoids the need for a separate and expensive high temperature oxygen cooler with additional tube and cover plates; (iii) the combination of the separator with the cooler in the same apparatus allows the tube plates to remain at a moderate temperature, allowing reasonably high design efforts with relatively inexpensive materials and conventional tube-to-tube plate joints; (iv) an insulated container allows the use of cheap building materials in the roof; (v) the use of deflectors and high gas velocities improve the transfer of mass and heat; (vi) the use of a portion of the oxygen-containing feed gas provides a heat sink to cool the gas stream of oxygen product; and (vii) the installation and the pipeline are simplified. The solid electrolyte ion-conducting tubes used in the embodiments of the invention usually consist of either a double-sided or solid-oxide mixed-oxide thick-walled conductor or of a double-sided or mixed thin-film solid oxide conductor supported by a porous substrate. The solid electrolyte ion conductor material must have sufficient ability to conduct oxygen and electron ions in the temperature range of 500 ° C to 1,100 ° C at the partial oxygen pressures prevailing when a chemical potential difference across the surface is maintained of the solid electrolyte ion conductor membrane caused by a ratio of partial pressures of oxygen through the solid electrolyte ionic conductive manuene. Suitable solid electrolyte ionic conductive materials are the perovskites and combinations of metal-metal double-face oxides as listed in Table I. Since the reactive environment on the anode side of the solid electrolyte ionic conductive manbena in many applications it creates very low partial pressures of oxygen, the cyano-containing perovskites of Table I may be the preferred material since they tend to be stable in this environment, ie they do not decompose chemically at very low partial pressures of oxygen. porous catalyst layers can be added to increase chemical reactions and / or achieve greater area of exchange surface on both sides of the electrolyte conductive solid electrolyte manbrane to increase chemical reactions on these surfaces when necessary. , without anbargo, it can be the same electrolyte perovskite material or solid cone used in the ion transport tubes. Alternatively, the surface layer of the solid electrolyte ionic conductive sleeve may be embedded, for example, with cobalt, to incise the surface exchange kinetics.

In the design it is also important to balance the local oxygen flow and the reaction kinetics to ensure that the local partial pressures of oxygen are at a level that ensures the stability of the material, ie, above 10 - * atm. for currently known materials. The oxygen flow will be a canplex function dependent on the ionic conductivity of the. material, the wall thickness of the solid electrolyte, the reaction kinetics, the partial pressure of the fuel, and the catalytic activity, which can be influenced by the selection of the catalyst and the extension of the catalyst area. The gas flow on the reaction side of the solid electrolyte tubes can be countercurrent or concurrent. The direction of gas flow may be important under certain circumstances since it will affect the local reaction kinetics and oxygen partial pressure environments. The last aspect has an effect on oxygen flow, material stability and canonical stresses. In general, the largest portion of gas stream is heated to an intermediate temperature before being introduced to the reactor section of the apparatus, which increases the efficiency of the process. If, however, the apparatus includes a reactor section and it is desired to maximize the reactor capacity to generate heat from the reaction of the penetrating gas stream and the reactant gas stream, the larger portion of the gas stream is not heated before being introduced to the appliance. Fig. IA shows a schematic drawing of an ion transport separator-cooler. Generally, a stream of feed gas containing elemental oxygen is compressed and divided into two portions to be fed to the separator-cooler apparatus. While the smaller portion of gas stream from the cold feed gas stream 2 is fed directly to the apparatus, the larger portion of the gas stream is usually heated to produce the hot feed gas stream 1 before being used. During operation, the hot feed gas stream 1 is introduced to the separation section 30 and the cold feed gas stream 2, at a temperature preferably in the range of 80 ° C to 250 ° C, is fed to the chiller section 32. Since the pressures of the gas streams are essentially the same in the separator section 30 and the chiller section 32 of the apparatus, only the baffle 11 is needed to separate the two sections. Deflector 11 does not need to be isolated, but may be insulated. The ion transport separator-cooler tubes 5 traverse both sections 30 and 32. The tubes 5 of the ion transport separator-cooler are capped and free floating at the upper end of the cone apparatus shown and are attached and sealed to the tube plate 4 at the bottom of the cone apparatus is shown - Since the tube plate 4 will be at a temperature of less than 300 ° C, normal bonding techniques such as welding or local tube expansion (rolling) can be employed , "o" rings or other mechanical means for effecting the joint of tube 5 of the ion transport separator-cooler with the tube plate 4. The ion transport tubes 5 must be capable of freely expanding to accommodate the resulting axial increase of thermal and canonical expansion. The insulation 15 insulates the structural walls 16 containing pressure from the apparatus to allow the use of normal building materials, for example, stainless steel or carbon steel. The tube 5 can be used in the separation section 30 and the chiller section 32 of the apparatus. Because the material constituting the tubes 5 of the ion transport separator-coolant will conduct oxygen ions at a high temperature but will be essentially impermeable to lower temperatures, it can act as a separation bushing in the separation section 30 and a surface of heat transfer in the chiller section 32. To achieve the high oxygen fluxes required, the separator-cooler tubes 5 are preferred which consist of a thin dense separation layer supported by a porous substrate. The dense separation layer of such tubes 5 of the separator-cooler is made of a material having high oxygen ion conductivity at high partial oxygen pressures. Coro was previously noted, suitable materials are the mixed and double-sided conductors of Table I. A preferred material is The porous substrate may be made of the same material or be sewn from one or several layers of other materials that are chemically compatible with materials adjacent to operating temperatures. Possible alternate materials may be less expensive oxides such as zirconia, ceria, yttria, alumina or metals such as chrome-nickel superalloys. Optionally, the separator-cooler tubes 5 may be coated with a porous catalyst layer on the retentate side and the permeate side of the ion transport section to respectively increase the dissociation and reccmbination of the oxygen. On the anode side (permeate), the catalytic function is best performed by a porous layer adjacent to or contiguous with the dense separation layer. Since an ion transport separation pipe will possibly be more expensive than a cooler pipe it may be appropriate to use a metal cooler pipe which is attached to the ion transport spacer pipe by welding with the gasket located in the upper section of the cooler . A detail of such a joint is shown in Fig. IB. The separator-cooler tubes 5 illustrated in Fig. IB have three parts: the ion transport tube 48 having a strange metallization, the sleeve 49, and the cooling tube 50. The tube ends of the ion transport tube 48 and the cooler tube 50 are welded to the sleeve 49. Another option is to use the same substrate tube for the separator section 30 and the chiller section 32 but to replace a cheap dense sealant layer with the ion transport layer in the backing portion. the tubes 5 of the separator-cooler in the cooling section 32. This is especially attractive if a metal porous substrate is poured. Returning to FIG. 1A, the hot feed gas stream 1 flows past the outer surface of the tubes 5 of the separator-cooler directed by the deflectors 10. The oxygen of the hot feed gas stream 1 penetrates through of the separator-cooler tubes 5 to provide the hot oxygen gas stream 8 inside the separator-cooler tubes 5. The stream of hot feed gas 1, depleted in oxygen, is converted into the gas stream 12 exhausted in oxygen and leaves the separating portion 30 of the apparatus. As the cold feed gas stream 2 flows generally counter-current to the stream of hot oxygen gas 8 within the tubes 5 of the separator-cooler directed by the baffles 10, the hot oxygen gas stream 8 flows from the separating section 30 towards the chiller section 32 and thus is cooled by heat transfer with the cold feed gas stream 2 to become the oxygen product gas stream 18 which leaves the apparatus through the product outlet port 20 . The cold feed gas stream 2, now at a high temperature, is extracted by the hot gas stream 17 and can be added to the hot gas feed stream 1. Alternatively, the hot gas stream 17 can be attached to the hot gas stream 17. stream of hot gas feed 1 inside the apparatus, for example, by means of a conduit 34 through the baffle 11. Before the hot gas stream 1, increased by the hot gas stream 17, flows through of the separating section 30 in cross-transverse flow to the hot oxygen gas stream 8 while the oxygen penetrates through the separator-cooler tubes 5. Fig. 2 is a schematic diagram of another embodiment of the invention showing a basic design of a solid electrolyte ion conductor conductor-separator-cooler that includes transport of ions through a tube with a sliding seal 54. As in FIG. Fig. ÍA, a stream of feed gas containing elemental oxygen is compressed and divided into two portions to be fed to the apparatus. reactor-separator-cooler. During operation, the feed gas stream 61 is introduced to the reactor section 51 and the cold feed gas stream 62 is fed to the chiller section 53. The tube 55 of the ion transport reactor-separator-cooler passes through all sections 51, 52 and 53. The tube 55 of the ion transport reactor-separator-cooler is attached to the tube plate 64 in the uppermost stranger of the apparatus by means of the slg seal 54 or a fixed seal with a bellows and it is attached and sealed to the tube plate 65 at the bottom of the apparatus. Since the tube plate 65 will be at a temperature of less than 300 ° C, normal joining techniques such as welding or local expansion of the tube (coiled), "o" rings or other mechanical means for effecting the union of the tube can be used. tube 55 of the ion transport reactor-separator-cooler to the tube plate 65. The tube plates 64 and 65, however, are at a higher temperature and different methods are generally employed to effect a seal. Although not shown, an insulation isolates the structural walls 70 containing pressure from the apparatus to allow the use of normal building materials, for example, stainless steel or carbon steel. The tube 55 can be used in the reactor section 51, the separator section 52 and the chiller section 53 of the apparatus. Cone was mentioned in relation to Figs. ÍA and IB, an ion transport separation and reaction tube will possibly be more expensive than a cooling tube and it may be appropriate to use a metal cooling tube which is attached to the ion transport separator tube and the ion transport reactor tube by welding with the union located in the upper section of the cooler. Alternatively, a single composite tube having a different cannulation can be employed in each of the various sections 51, 52 and 53, optimized for the particular function to be performed in each section. A cross section of such a composite tube is shown in Fig. 7. In these composite tubes, a porous substrate 251 supports a thin dense layer of separation. The reactor section of the tube is coated with a mixed conductive layer 252 having optimum stability at partial pressure of low oxygen, the separating section with a material 253 having high conductivity at high partial pressures of oxygen, and the chiller section * of the tube with a cheap sealing layer 254. With Fig. IB, the chill section of the tube can also be made of a different material (eg, metal) and be attached to the composite ion transport tube comprising the reactor and separation sections. Therefore, a single tube arranged in the reactor section 51, the separator section 52 and the chiller section 53 of the apparatus can be employed. Returning to FIG. 2, the feed gas stream 61 flows past the outer surface of the jacket tube 56 directed by the deflectors 60 and is heat-set by heat transfer with the jacket tube 56 and flows in the concentric annular passage 68 formed between the outer surface of the reactor-separator-cooler pipe 55 and the inner surface of the jacket tube 56. The jacket tube 56 extends beyond the reactor section 51 through the separator section 52 of the apparatus. Reactive gas stream 72, for example. methane optionally diluted with steam flows down the reactor-separator-cooler tube and reacts with the oxygen that enters the feed gas stream 61 through the reactor-separator-cooler tube 55 to provide the gas stream of reaction products 73 inside the tube 55. When the reactant gas stream 72 consists of methane or another hydrocarbon, the gas stream reaction products 73 is mainly carbon dioxide and water, the normal products of combustion, and fuel without react, if there is an excess of fuel, or oxygen, if the process is poor in fuel. Preferably, an excess of fuel is not present in the spacer section 52 when the reactive conditions are unfavorable for the ion transport material in that section. The heat generated by the reaction of the reactive gas stream 72 with the oxygen that penetrates is transferred from the reactor section 51 to the reactor-separator-cooler tube 55 to the jacket tube 56 by convection and radiation processes and from there to the current of feed gas 61 flowing on the outside of the jacket tube 56. The local heat transfer coefficients are adjusted by the variable spacing of deflectors or insulation to create a reasonably uniform reactor-separator-cooler tube temperature. At the same time, the cold feed gas stream 62, directed by the deflectors 60, flows in the chiller section 53 of the apparatus, cools the gas stream inside the reactor-separator-cooler pipe 55, and the gas stream The resultant, now at elevated temperature, flows in the concentric annular passage 68 together with the feed gas stream 61. The gas stream reaction products 73 flows to the separation section 52 of the apparatus and purges the separator section 52 of the reactor tube -separator-cooler 55 to increase the chemical driving potential through the manuena such that oxygen penetrates through the tube 55 to supply the gas stream of oxygen product 74 which is cooled by the flow of the cold gas stream of feed 62 and containing oxygen as well as the reaction products produced in the reactor section 51 of the apparatus. the gas stream of enriched oxygen product 74 exits the apparatus through the product outlet port 76. A product gas stream 78 exhausted in high pressure oxygen can also be recovered. The embodiment of the invention shown in Fig. 2 illustrates a possible use of a purge gas stream, such as steam cone or reaction products of an ion transport reactor (carbon dioxide and water), to purge the anode from the ion transport membrane and thus lower the partial pressure of oxygen at the anode and increase the driving force for oxygen separation, leading to a smaller area of the separator and / or recovery of a greater quantity of the oxygen contained in the feed gas . Figs.2 and 3 show modifications to the basic separator-cooler apparatus that allow the use of such a purge gas while maintaining all the advantages previously mentioned for the separator-cooler. The embodiment of the invention shown in Fig. 3, discussed below, differs from that of Fig. 2 in that the embodiment of Fig. 2 generates the purge gas in a reactor section within the apparatus, while the gas The purge used in Fig. 3 can be generated anywhere or supplied by an external source. Fig. 3 is a schematic diagram of one embodiment of the invention showing a basic design of a solid electrolyte electrically conductive separator-cooler that features a tube with a free floating end and an internal purge feed tube for a fuel or an externally generated purge gas stream. As in Fig. IA, a stream of feed gas containing elemental oxygen is compressed and divided into two portions to be fed to the reactor-separator-cooler apparatus and a portion is heated. During operation, the hot feed gas stream 91 is introduced into the reactor section 100 and the cold feed gas stream 92 is fed to the chiller section 101. The ion transport tubes 95 of the separator-cooler traverse the separating section 100 and chiller section 101 of the apparatus. The ion transport tubes 95 of the separator-cooler are capped and free floating in the strange upper of the apparatus as shown and are attached to the tube plate 94 at the bottom of the apparatus. Like before, since the tube plate 94 will be at a temperature of less than 300 ° C, normal joining techniques can be used to effect the separator-cooler pipe 95-tube plate 94. Similarly, the insulation 105 insulates the structural walls 106 containing pressure from the apparatus to allow the use of normal construction materials. As in Fig. 1A, the same tube 95 can be employed in the separator section 100 and the chiller section 101 of the apparatus and can be constructed as discussed above.

The hot feed gas stream 91 flows past the outer surface of the separator-cooler tubes 95 directed by the baffles 120. At the same time, the purge gas stream 108 flows into the apparatus and is directed by the tubes 110. of purge feed attached to the tube plate 96. the purge gas stream 108 is substantially at the same temperature (100 ° C to 300 ° C) of the cold air stream 92, when it enters the apparatus and is warmed by heat transfer with the hot product gas stream in the annular passage 112. The purge gas stream 108 then flows into the concentric annular passages 112 formed between the inner surface of the separator-cooler tubes 95 and the outer surface of the tubes purge feed 110. Purge feed tubes 110 extend almost the entire length of spacer-cooler tubes 95. Purge gas stream 108 purges the permeate side of the separator-cooler tubes 95 and increase the extraction of oxygen from the hot feed gas stream 91 as it flows past the outer surface of the spacer-cooler tubes 95 and out of the apparatus cone the gas stream 114 depleted in oxygen , which can. be recovered as a product. At the same time, the hot feed gas stream 92, directed by the baffles 120, flows into the chiller section 101 of the apparatus, cools the mixed gas stream inside the separator-cooler tube 95, and the resulting gas stream, now at elevated temperature, it leaves the apparatus as the heated gas stream 116. The heated gas stream 116 may be added to the feed gas stream 91 before it enters the apparatus or, although not shown, may be added to the feed gas stream 91 after doing so. The purge gas stream 108, now mixed with permeated oxygen, and cooled by the flow of the cold feed gas stream 92, exits the apparatus with the product gas stream 118 through the product outlet port 119. You can easily see all the advantages of the Fig. AY mode. They are preserved since all the strangers of tubes are free floating and the flow arrangement for the cooling air stream is unchanged. It is desirable to have the inlet of the purge gas stream at a sufficiently low temperature to facilitate sealing at the tube-to-tube plate seal and to heat the purge gas stream to the operating temperature of the ion carrier membrane putting it in a counter-flow arrangement with the purge gas-product oxygen outgoing mixture. The "Fig. 4 is a schematic diagram of another embodiment of the invention showing a basic design of a solid electrolyte ion-conductor reactor-separator-cooler.Can in Fig. IA, an oxygen-containing feed gas stream. It is compressed and divided into two portions to be fed to the reactor-separator-cooler apparatus.The apparatus uses three concentric tubes: the jacket tubes 149 connected to the upper tube plate 150 and open at the bottom of the separator section 131, the tubes ion transporter 145 of the reactor-separator-cooler closed at the top and attached to the intermediate pipe plate 144, and the inner feed pipes 154 open at the top and attached to the bottom plate 155. Insulation 165 insulates the structural walls 166 containing pressure from the apparatus to allow the use of normal building materials The tube plates 144 and 155 will be at a tanperator ura of less than 300 ° C and normal joining techniques can be used to effect all tube-to-tube plate joints. The tube plate 150 will be at a higher temperature but the seal is less critical than with the other gaskets because there is only a small pressure difference across the seal. The ion transport tube 145 of the reactor-separator-cooler passes through the reactor section 130, the separating section 131 and the cooler 132 of the apparatus. Sections 130, 131 and 132 operate in effect as separate stages performing different functions under different operating conditions. Modifications similar to the reactor-separator-cooler tube 145 to which they were mentioned with respect to the embodiment of Fig. 2 can be used for the embodiment of Fig. 4. The chiller section 132 is separated from the separator section 131 by the deflector 158 with flow openings 157. During operation, the feed gas stream 135 is introduced to the reactor section 130 and the cold feed gas stream 142 is fed to the chiller section 132. the reactant gas stream 160 , with or without a diluent, is fed through the internal feed tubes 154. The feed gas stream 135 flows past the outer surface of the shell tube 149 directed by the baffles 168 and is heat-set by heat transfer. the envelope tube 149 and flows into the concentric annular passage 164 formed between the outer surface of the reactor-separator-cooler tube 145 and the internal surface of the tube. bo envelope 149. Optionally, the first portion of reactor-separator-cooler tubes 145 can be operated with a non-reactive purge gas stream, creating, in effect, a three-stage separator wherein a non-reactivated purged section. precedes the reactive purged section which is followed by a second non-reactive purged portion. This option is illustrated in the central tubes of the reactor-separator-cooler 145 of the apparatus and is performed by adding a small flow-limiting orifice 182 of a predetermined size at the upper end of the ion transport tube 145, thus introducing a purge stream. product and finishing the internal feeding tube 154a at a previous point. If such an arrangement is used, there should also be a baffle 184 at the upper end of the inner tube for diverting the reactant gas stream 160 as it exits the internal feed tube 154a. The motivation for choosing this option would be to avoid exposing the closed end of the ion transport tube to a highly reducing environment, which exists with a reactive purged anode and a highly pure nitrogen product at the cathode, and threats to the stability of the material. Alternatively, a small amount of the feed gas stream can be added to the reactant gas stream 160 to substantially raise the partial pressure of oxygen in the purge gas stream at the end of the product nitrogen gas stream while maintaining still low enough to maintain adequate driving force for oxygen transport. Typically, the partial pressure of oxygen in the purge gas can be elevated from 10- ^ to 10"- * - ^ atm In the absence of this modification, the reactant gas stream 160 flows through the annular passage 162 formed between the internal surface of the reactor-separator-cooler tube 145 and the external surface of the internal feed tube 154 down the tube 145 of the reactor-separator-cooler and reacts with the oxygen permeating the feed gas stream 135 through the tube 145 of the reactor-separator-cooler for supplying the hot stream of gases of reaction products inside the tube 145. An appropriate proportioning of flows of gas streams ensures that the fuel in the reactant gas stream 160 will be exhausted in a point partially down the annular passage 162. The heat generated by the reaction of reactive gas stream 160 with the penetrating oxygen is transferred from the tube 145 of the rector-separator-cooled to surround tube 149 by covection and radiation processes. At the same time, the cold feed gas stream 142, directed by the baffles 168, flows into the chiller section 132 of the apparatus, cools the gas stream inside the tube 145 of the reactor-separator-cooler, and the resulting gas stream now at elevated temperature, flows through the flow openings 157 in the deflector 158 to join the gas stream of feed 135 to rise through the annular passage 164. Thus, the hot stream of gases reaction products 170 flows into the separation section 131 of the apparatus and purges the tube 145 from the reactor-separator-cooler to increase the chemical potential driving through of the membrane for oxygen to penetrate through the tube 145 to provide the gas stream of enriched oxygen product 180 which has been cooled by the flow of the cold stream of feed gas 142, directed by the baffles 133, and the which contains oxygen as well as the reaction products produced in the reactor section 130 of the apparatus. The enriched stream of oxygen product gas 180 leaves the apparatus through product outlet port 181. If the reactant gas stream 160 consists of methane or another hydrocarbon, the gas stream of enriched oxygen product 180 will contain mainly oxygen, carbon dioxide and water. As in the previous modes discussed, the cold feed gas stream 142, which is the minor portion of the original feed gas stream, enters the bottom of the chiller section 132, passes through the flow openings 157 and is recuperatively heated by the permeate product flow counter-current and thus performs the chiller function. The function of the reactor, cone is illustrated in Fig. 4 and previously, it heats the feed gas stream 135, which is the largest portion of the original feed gas stream, as it flows downward in counter-transverse flow through the reaction that occurs in the wall of the tube 145 of the reactor-separator-cooler. How in Figs. ÍA and 3, all the strangers of tubes are free-floating to avoid efforts of the thermal and canposiional dimensional changes and the bottom plate of tubes is cold to facilitate joints and seals of tube-to-tube plates. The quality of this seal is related in some way to the purity requirements for the nitrogen stream. Cone in all the modalities, the side of the cover of the apparatus is equipped with deflectors 168 to increase the heat transfer. If the reactor section 130, baffles 168 have variable spacing: wider where the temperature difference between the gas stream next to the cover and the shell tubes 149 is high and smaller where this difference is small. The purpose of this variable spacing of the deflectors 168 is to maintain a constant heat flow in the reactor section 130 and to minimize temperature variations in the ion transport elements. Cone was previously mentioned, the envelope tubes 149 enjoy a heat transfer coupling by favorable radiation with the surface of the ion transport tube of the reactor. Although not shown, the design may also require insulation of the enclosing tube in the vicinity of the power inlet where the T's can be very large. The embodiment of the invention shown in Fig. 4, with all the modalities provided, can be used for many functions. For example, the apparatus may be used for a two-stage Deoxo apparatus with the first stage purged by reaction and the second stage purged under pressure with purge of combustion products, or with a separator to extract oxygen from the feed air and produce dioxide. of carbon from combustion products of an integrated gas turbine cycle, or cut off a device to separate air in a stream of nitrogen gas and a gas stream of product oxygen which contains something d? carbon dioxide and vapor which has to be separated downstream from the apparatus.

Fig. 5 is a schematic diagram of another embodiment of the invention showing a basic design of a solid electrolyte ion-conductive reactor-cooler. As in Fig. IA, a feeding gas stream containing elemental oxygen is compressed and divided into at least two portions to be fed to the reactor-cooler apparatus. During operation, the feed gas stream 205 is introduced to the reactor section 201 and the cold feed gas stream 207 is fed to the chiller section 202 of reaction products. Optionally, a second cold stream of feed gas 208 is fed to the chiller section 200 of nitrogen product. The ion transport tube 210 of the reactor-cooler passes through all sections 200, 201 and 202 of the reactor-cooler. The ion transport tube 210 of the reactor-cooler is attached to the tube plate 211 in the uppermost bizarre of the apparatus by means of a sliding seal or a fixed seal with a bellows and is attached and sealed to the tube plate 212 in the bottom of the device. Cone above, since the tube plate 212 will be at a temperature of less than 300 ° C, normal joining techniques can be employed to effect the 212-to-tube 210 tuto plate connection of the reactor-cooler. Similarly, an insulation (not shown) insulates the structural walls 206 containing pressure from the apparatus to allow the use of normal building materials. As in the previous figures, the same tube 210 can be used in the reactor section 201 and in the chiller sections 200 and 202 of the apparatus and can be constructed as discussed above. Only the central part 210a of the reactor 210 cooler tube needs to have an active ion transport membrane. Cone above, a composite tube consisting of a porous support tube and a mixed conductive film in the reactor section 201 and a sealing film in the chiller sections 200 and 202 can be used. The feed gas stream 205 flows past the outer surface of the jacket tube 215 directed by the baffles 214 and is heat-set by heat transfer with the jacket tube 215 and flows to the concentric annular passage 216 formed between the external surface of the tube 210 of the reactor-cooler and the inner surface of the jacket tube 215. The jacket tube 215 extends slightly beyond the reactor section 210 to the chiller section 202 of reaction products of the apparatus. the reactant gas stream 218, for example methane, flows down the tube 210 of the reactor-cooler and, once the surface of the ion transport tube has reached the operating temperature of the ion transport tube, it reacts with the oxygen penetrating the feed gas stream 205 through the reactor 210-cooler tube 210 to supply the gas stream 221 of reaction products within the pipe 210. If the reactant gas stream 218 consisted of methane or other hydrocarbon, the 221 gas stream of reaction products would be mainly carbon dioxide and water, the normal products of combustion, and unreacted fuel if there was an excess of fuel, or oxygen, if the process had been run poor in fuel. The heat generated by the reaction of the reactant gas stream 218 with the permeate oxygen is transferred from the tube 210 of the reactor-cooler to the shell tube 215 by convection and radiation processes. At the same time, the cold stream of feed gas 207, directed by the deflectors 214, flows in the chiller section 202 of reaction products of the apparatus, cools the gas stream inside the reactor 210-cooler tube 210, and the resulting gas stream, now at elevated tepersaturation, flows the concentric annular passage 216 together with the supply gas stream 205. Thus, the gas sorbent 221 of reaction products is cooled by the flow of the cold stream of feed gas 207 and exits the apparatus through the product exit port 222. The product gas stream 220 (nitrogen) depleted in high pressure oxygen can also be recovered. If this is the case, it is advantageous to use the second cold stream of optional feed gas 208 to cool the gas stream in the chiller section 200 of nitrogen product in a manner similar to the chiller section 202 of reaction products. Fig. 6 is a schematic diagram of another embodiment of the invention showing a basic design of another solid ion electrolyte ion-conducting cooler reactor. In Fig. IA, a stream of feed gas containing elanental oxygen is compressed and divided into at least two portions to be fed to the reactor-cooler apparatus. During operation, the feed gas stream 233 is introduced to the active reactor section 231 and the cold feed gas stream 234 is fed to the chiller section 232 of reaction products. Optionally, a second cold stream of feed gas 235 is fed to the chiller section 230 of nitrogen product. The ion transport tube 236 of the reactor-cooler extends through the reactor section 231 and the chiller section 232 of the reactor-cooler. The apparatus uses three concentric tubes: the jacket tube 240 connected to the upper tube plate 241 and open at the bottom of the reactor section 231, the ion transport tube 236 of the reactor-cooler closed at the top and attached to the the intermediate pipe plate 237; and the internal feeding tube 238 open at the top and attached to the tube plate 239 from the bottom. As before, since the tube plates 237, 239 and 241 will be at a temperature of less than 300 ° C, nl joining techniques can be employed to effect the joints as necessary. Similarly, an insulation (not shown) insulates the structural walls 242 containing pressure from the apparatus to allow the use of nl construction materials. With the foregoing figures, the same tube 236 may be employed in the reactor section 231 and the chiller section 232 of reactor products of the apparatus and may be constructed as discussed above. Only the upper part 236a of the tube 236 of the reactor-cooler needs to have an active ion transport membrane. The feed gas stream 233 flows past the outer surface of the jacket tube 240 directed by the baffles 243 and is heat-transferred by heat transfer with the jacket tube 240 flowing to the concentric annular passage 244 fd between the outer surface of the tube 236 of the reactor-cooler and the inner surface of the jacket tube 240. The jacket tube 240 extends slightly beyond the reactor section 231 to the chiller section 232 of reaction products of the apparatus. The reactant gas stream 245, for example methane, optionally diluted with steam, rises through the inner feed tube 238, lowers through the annular passage 246 fd between the inner surface of the reactor-cooler tube 236 and the outer surface of the shell tube. 240, and reacts with the oxygen that enters the feed gas stream 233 through the tube 236 of the reactor-cooler to supply the gas stream 247 of reaction products inside the tube 236. If the reactant gas stream 245 consisted of methane or another hydrocarbon, the gas stream 247 reaction products would be mainly carbon dioxide and water, nl combustion products, and unreacted fuel, if there was an excess of fuel, or oxygen, if the process had been effected poor in fuel. The heat generated by the reaction of the reactive gas stream 245 with the oxygen that penetrates is transferred from the tube 236 of the reactor-cooler to the shell 240 and to the inner pipe 238 by convection and radiation processes. At the same time, the cold stream of feed gas 234, directed by baffles 243, flows into the chiller section 232 of reaction products of the apparatus, cools the gas stream inside the tube 236 of the reactor-cooler, and the resulting gas stream, now at elevated temperature, flows the concentric annular passage 244 together with the feed gas stream 233. Thus, the gas stream 247 of reaction products is cooled by the flow of the cold stream of feed gas 234 and exits the apparatus through the product exit port 248. The product gas stream 249 (nitrogen) depleted in high pressure oxygen can also be recovered. If this is the case, it is advantageous to use the second cold stream of optional feed gas 235 to cool the gas stream in the chiller section 230 of nitrogen product in a manner similar to the chiller section 232 of reaction products. Fig. 8 illustrates the simplicity of a complete oxygen / nitrogen separation cycle using a reactor-separator-cooler module 300 according to the present invention. The feed gas stream 260, usually air, is compressed by the compressor 260 to obtain the compressed gas stream 264. The compressed gas stream 264 is divided into the feed gas major stream 268 and the lower gas stream. 266. The feed stream 266 is cooled in the cooler 270 and then continues through the valve 272. The cooled gas stream 274 is introduced into the chiller section 271 of the ion transport node 300. The larger stream of feed gas 268 passes through the valve 301 to become the major gas stream 299 which is introduced to the reactor section 273 of the ion transport reactor 300. __. a modality, the gas stream 286 is a reactive gas stream and the larger gas stream 299 is heated in the reactor section 273 of the ion transport node 300 to about 900 ° C by the reaction of the gas stream 286 and the oxygen on the anode side of the ion transport membrane of the reactor section 273 of the ion transport node 300. In another embodiment, the gas stream 286 is a stream of unreacted diluent gas which is used to purge the anode side of the ion transport membrane of the reactor section 273 and the spacer section 275 of the ion transport module 300. The energy for heating the feed gas stream 274 is supplied by anode product stream to counter current. current. The sistine illustrated in Fig. 8 uses in effect a deoxo reaction booster stage 273 and a pressure-driven oxygen separation stage 275 which is increased by a purge of canbusing products including species such as water cone (steam). and carbon dioxide. The two streams of gases left by the ion transport node 300 are the cold gas stream 284 at low pressure which are oxygen, carbon dioxide and water, and a stream of nitrogen prodrug 276 at high pressure and high temperature. The low pressure gas 284 sorber which is oxygen, carbon dioxide and water vapor is cooled by the cooler 302 to produce the gas sorptive 303. The mass of water held in the gas sorptive 303 is condensed by the condenser 304 to produce water stream 305 and gas stream 306 which primarily contains oxygen and sarbon dioxide. the gas sorbent 306 is sent to the downstream separator by processes of aspersion or absorption by manbrane. Water sorptive 305 may be desorbed as water stream 312 or may be converted to water stream 307 which is pumped by bank 308 to become water stream 309. Water stream 309 is passed through. of the heat exchanger 307 for heating are the gas sorbent 282 to become steam, ie, the gas stream 310. The gas stream 310 is optionally divided into the gas stream 311 and the gas stream 313.

Although it was mentioned before, the gas sorptive 286, whether reactive or non-reactive, is fed to the reactor section 275 of the ion transport module 300. The nitrogen product sorptive 276 is optionally divided into the gas sorptive 277 , shown in dotted line, and gas sorbent 323. If produced, the gas sorbent 277 is joined is the optic gas sorptor 311, shown in dotted line healthy deviated from the sorptive 310, to be converted into the sorptive gas 279. Gas sorbent 279 and reactive gas sorbent 320 are fed to burner 321 for combustion to produce gas sorbent 322. Gas stream 322 joins gas stream 323 to produce gas stream 324 The gas stream 324 in one embodiment is expanded in a gas turbine 280 or the heat energy can be recovered by a Rankine cistern steam system. The Rankine silo steam system introduced additional complexities, but has the advantage of delivering nitrogen product under pressure. In the embodiment shown using the gas turbine 280, there is sufficient heat available in the turbine gas stream 282 from the turbine for the generation of the vapor gas stream 310, the water stream 305 being released in the heat exchanger 307 , for the additional incineration of the oxygen flow in the 300 ion transport module, samo was mentioned earlier. the gas sorbent 282 passes through the salinity separator 307 to be converted into the gas sorbent 283. The gas sorbent 283 passes through the cooler 330 to become the gas stream 329, which is usually discarded. The Fig. 9 illustrates the integration of an ion transport separator-cooler in a gas turbine cycle according to the present invention. The feed gas stream 350, for example air, after being compressed in the compressor 352 to produce the feed gas stream 353, is divided into the largest feed gas sorptive 356 and the lowest sorptive feed gas 355. The smaller stream of feed gas 355 continues through the valve 358 to produce the gas stream 360. The sual is introduced to the chiller session 361 of the separator-cooler module 400 and is then heated and exits the separator-cooler module. 400 the gas stream 368. The larger sorpt of feed gas 356 is optionally divided into the gas stream 364 and the gas sorbent 404. The gas stream 364 is heated to the operating temperature of the ion transporter (approximately 900 ° C) in the burner 362 after the fuel gas sorbent 364 has been added to produce the gas stream 366. An io transport conveyor Either a burner externally to fire may be replaced by the burner 362 without affecting the functionality of the sistine. The gas sorbent 404 passes through the optional heat exchanger 407 to produce the hot gas stream 403, the sual is joined to the gas sorbent 366 to produce the gas sorbent 367. The optional retractive gas sorptive 405 is added to the gas stream. the gas stream 367 to produce the gas stream 370. The gas stream 368 is added to the gas stream 370 to produce the gas stream 372, which is introduced to the separator section 363 of the separator-cooler module 400 in where the 365 oxygen is removed using an ion transport tube 367. Following the removal through the ion transport membrane 367 in the separator section 363 of the separator-cooler module 400 of the portion 365 of the oxygen 365 maintained in the sorptive gas 372, the gas stream 380 leaves the separator-cooler nozzle 400 and is heated to the intake temperature of the turbine in the burner 382 after the gas stream 384 is added. L The resultant gas stream 386 is expanded in the turbine 388 to form the leakage sorbet 420 of the turbine. The gas sorbent 420 is optionally divided into the gas sorbent 402 and the gas stream 421. the gas stream 402, if produced, it is passed through the heat exchanger 407 to produce the gas sorptive 406- The gas stream 406 is added to the gas stream 421 to produce the gas stream 426. In the case shown, the heat waste is recovered by the steam system Rankine 410 coo follows. the oxygen prodrug gas stream 401 leaves the chiller session 361 of the separator-chiller node 400 at a temperature of about 150 ° C to 300 ° C. If the temperature levels allow it, some of the heat contained in the sorptive Oxygen prodrug gas 401 and the turpentine sorptive of turbine 426 is recovered by the Rankine 410 steam silo. A resumer can be used in place of the Rankine 410 steam system to recover the excess of salty solution in the sorbate sorbate. 426 of the turbine and the gas sorbent 401 of produsto oxigene. The Rankine 410 steam system produced the waste gas stream 412, the sual is usually unused, and the oxygen gas sorptive 411. The oxygen gas sorbate 411 is then cooled by the cooler 414 to produce the oxygen gas sorbate 415 the sual is compressed by the compressor 416 to produce the oxygen gas flow 417 the sual is recovered as the produsto. Cone was discussed before, it is possible that different solid ion electrolyte conductive materials will be selected for reactor and separator functions to provide optimum service. The selessioned materials for the reactor service should have maximum stability at low parsial oxygen pressures such healthy the srano-containing perovskites listed in Table I and the materials selected for the oxygen separation service should be those that have high ionic soundness at pressures partial oxygen levels. Species aspects of the invention are shown in one or more of the drawings only by sonveniensia, since sada aspesto can be sanbinado are other aspestos of agreement are the invention. In addition, several changes and modifications can be made to the examples given without departing from the spirit of the invention. Alternate modalities will be recognized by those experts in the art and it is intended that they be included in the alsanse of the claims.

Claims (10)

1. CLAIMS 1. Uh proceeds to produce a soruent of oxygen gas or a gas sorptive enriched with oxygen and a gas sorptive exhausted in oxygen by first separating oxygen from a feed gas stream containing elemental oxygen and then cooling the gas sorptive Oxygen or the sorriente of enriched gas are oxygen obtained that, within a single apparatus, the apparatus having a separating session and a chilling session and a produsto oxygen outlet port, where the separating session insulates an ion transport membrane that it has one side of retentate and one side of permeate, disho proseso somprendiendo: (a) squeeze the supply gas stream; (b) dividing the supply gas compressed gas stream into a larger gas stream portion and a smaller gas sorptive portion; (c) heating the largest portion of gas stream; (d) introducing the largest heated portion of gas stream to the separating session of the apparatus; (e) introducing the smaller portion of gas soruent to the chiller session of the apparatus near the produsto oxygen outlet port; (f) removing oxygen from the heated greater portion of gas stream through an ion transport membrane of the separating section to obtain a sorptive of enriched gas is oxygen on the permeate side of the membrane and a gas sorptive depleted in oxygen on the retentate side of the membrane; and () transferring salor from the sorbed gas stream is oxygen to the lower portion of the gas stream to produce the oxygen gas sorptive or the sorbed gas dioxide enrusted is oxygen and a smaller heated portion of gas stream, where the A smaller portion of gas is released from the apparatus or is sanded with the larger heated portion of the gas stream before the larger portion of heated gas is introduced to the separating portion of the apparatus, and where the gas stream depleted in oxygen exits. of the device.
2. 2. The process according to claim 1, wherein the apparatus is followed by a reactor session, which includes an ion transport membrane having a retentate side and a permeate side and wherein a retentate gas sorptive is introduced into the reactor. The permeate side of the ion transport membrane in the reactor section of the apparatus, to resuspend is a second sorriente of oxygen gas that penetrates through the sersa ion transport membrane of the permeate side of the ion transport membrane, to produce a stream of gases reaction products which is used to purge the permeate side of the ion transport membrane in the separating section of the apparatus, and where the gas sorptive produces reassessment and the first stream of oxygen gas and any unreacted oxygen of the second sorriente of oxygen gas are combined as the sorriente of gas enriched are oxygen the sual leaves the apparatus, and n where the gas stream exhausted in oxygen comes out separately from the apparatus.
3. 3. The process of agreement is the claim 2 wherein the ion transport membrane of the separating session of the apparatus and the ion transporting manbrana of the reactor session of the apparatus are integrally formed.
4. 4. The process according to claim 3 wherein the ion transport membrane of the separating section of the apparatus includes a porous support substrate and blends an ion transport material having high oxygen conductivity at high oxygen partial pressure and The ion transport membrane of the device's retraction section comprises a mixed conductive web having optimum stability at low oxygen pressure.
5. 5. The process of agreeing with the claim 3 in which the ion transport membrane of the device's recession session and the ion-transporting hose of the separating session of the apparatus are integrally formed are a sondusto to carry the enriched gas stream are oxygen through the chiller section of the apparatus.
6. 6. The process of agreeing with the claim 5 wherein the sonde to carry the flow of enriched gas is oxygen through the chilling session of the apparatus is a metal tube and is attached to the ion-transporting manbrane of the reactor section of the apparatus by welding for union between them.
7. 7. The process of securing is the claim 5 where the sonde to carry the gas sorbent enriched with oxygen through the chiller section of the apparatus bleeds a dense sealant material and is attached to the ion transport membrane of the reactor session of the apparatus by welding for union between them.
8. 8. The process according to claim 2 wherein the reactive gas is heated before being introduced to the reagent session of the apparatus.
9. 9. The sequence of agreement is claim 1 wherein the separating session includes a recessor session and step (f) involves introducing a reactive gas stream on the permeate side of the ion transport membrane to react with at least one porsion of oxygen transported.
10. 10. Uh intended to produce a sorid of enriched gas are oxygen and a soruent of gas depleted in oxygen by separating oxygen from a feed gas sorptive containing elemental oxygen within an apparatus, the apparatus having a recessor session and a spacer section, wherein the spacer and spacer sections each include at least one ion transporter having one side of retentate and one side of permeate, disho proceeding by: (a) squeezing the feed gas stream; (b) introducing the sorptive gas of feed gas into the apparatus and transferring salor from a sorriente of reactive gases to the sorptive of feed gas; (s) removing oxygen from the sorbed outlet of feed gas by means of transport through the ion transporting hose in the recessor session of the apparatus to produce a stream of reuse gases on the permeate side of the membrane and a sorr oxygen depleted gas partially on the retentate side of the membrane. (d) removing addional oxygen from the spent oxygen gas sorptive partially by transport through the ion transporting hose in the separating session of the apparatus to produce the exhausted gas stream in oxygen at the retained side of the membrane; where a retentate gas sorptive is introduced into the permeate side of the ion transport membrane in the recessor session of the apparatus to resuspend are the oxygen transported through the sersa ion transport membrane on the permeate side of the manbrane to produce the stream of gases produced by reassumption the sual is used to purge the permeate side of the ion transport membrane in the separating session of the apparatus; and wherein the sorptive of gases reaction products and the oxygen transported without the reaction are combined with the stream of enriched gas are oxygen leaving the apparatus, and where the sorptive gas exhausted in oxygen leaves the apparatus separately. X í * 55 SUMMARY OF THE INVENTION A process for producing a soruent of oxygen gas, a gas stream enriched with oxygen, or a stream of reaction products with a permeate stream and a retentate gas stream exhausted in oxygen by first separating oxygen from a stream of oxygen. feed gas and then cooling at least the permeate sorptive. The produssion and cooling of the permeate soruent wafts within a single apparatus having at least one ion transporting membrane.