MXPA98003328A - Method for producing oxidized product and generating energy using a membrane of solid electrolyte integrated with a turbine of - Google Patents

Abstract

A process to produce an oxidized product together with a turbine to generate energy. This process comprises contacting a compressed and heated oxygen containing gas stream with at least one solid electrolyte oxygen ion transport membrane in a membrane reactor. A reagent is passed into the reactor to generate an oxidized product therefrom. The non-oxygen retentate stream from the reactor is added to a gas turbine combustion chamber and expanded in a gas turbine to generate energy

Description

METHOD TO PRODUCE OXIDIZED PRODUCT AND GENERATE ENERGY USING A SOLID ELECTROLYTE MEMBRANE INTEGRATED WITH A GAS TURBINE FIELD OF THE INVENTION This invention relates to methods for producing oxidized products and generating energy using an ionic solid electrolyte or mixed conductor membrane. In particular, this invention is directed to methods for producing synthesis gas and generating energy using a solid electrolyte or mixed conductor ion membrane with a gas turbine.

CROSS REFERENCE U.S. Patent Application Serial No. (Proxy Case No. 20288) entitled "Method of Producing Hydrogen Using Solid Electrolyte Membrane", presented concurrently with the present, is incorporated herein by reference.

BACKGROUND OF THE INVENTION In gas turbine systems to generate energy, the air fed is compressed and burned with a reagent to raise its temperature and subsequently it expands through a turbine to produce energy. The oxygen production equipment has been combined with some of those gas turbine systems to produce oxygen at an increased cost Gas turbine energy systems have also been combined with steam power generation systems to generate additional energy, where the expanded hot gas can be used to generate steam. Oxygen production equipment uses a solid electrolyte ion transport membrane The ion transport system operates at a significantly higher temperature, on the scale from about 500 ° C to about 1200 ° C, than the compressor discharge of a gas turbine system, whose operating temperature rarely reaches 375 ° C Now there are two types of membr Solid electrolyte ion transport rings in development These include ion conductors that conduct only ions through the membrane and mixed conductors that conduct both ions and electrons through the membrane An ion transport membrane that exhibits mixed conduction characteristics can transport Oxygen when subjected to a ratio of partial pressures of oxygen through the membrane without the need for an applied electric field or external electrodes that would be necessary with ion-only conductors. As used herein, "solid electrolyte ion transport system" or, simply, "solid electrolyte" or "ion transport membrane" is used to designate either a system that uses an ionic type system (electrically driven). ) or a mixed conductor type system (pressure driven) unless otherwise specified Mixed conductors are materials that, at elevated temperatures, contain mobile oxygen ion voids that provide conduction sites for selective ion transport. Oxygen through the material Transport is driven by the ratio of oxygen activities, that is, the partial pressures of oxygen (p02) across the membrane, such as oxygen ions flowing from the side with higher partial pressures of oxygen higher than those with lower partial pressure of oxygen The ionization of the oxygen molecules to oxygen ions takes place on the cathode side (or the area of the retentate) of the membrane Oxygen ions recombine over the infiltrated zone delivering electrons For materials that exhibit only ionic conductivity, the external electrodes are placed on the surfaces of the electrolyte and the electrons are returned to the cathode in an external circuit the mixed conduction materials, the electrons are transported to the cathode internally, thus completing the circuit and obviating the need for external electrons. It is considered that the reaction of the oxygen infiltrated with the fuel takes place on the surface or in the boundary layers instead of the volume phase on the anode side (or the infiltrated zone). Partial oxidation reactions (Pox) that involve carbonaceous supplies are common methods for producing synthesis gas. Partial oxidation is also used to produce ethylene oxide, acrylonitrile and other chemical products. Syngas, comprised of carbon monoxide and hydrogen, is a valuable industrial gas and an important presure for the production of chemical products including ammonia, alcohols (including methanol and higher carbon alcolohes), synthesis fuels, aldehydes, ethers and others. Supplies that include natural gas, coal, naphtha and fuel oils are commonly used to produce synthesis gas through partial oxidation or steam reforming reactions. The partial oxidation reactions can be represented as follows: CmHn + m / 2 02 = m CO + n / 2 H2, where CmHn is a hydrocarbon supply. To a lesser degree, steam reforming can also take place, as depicted below.

CmHn + m H20 = m CO + (m + n / 2) H2. where CmHn is a hydrocarbon supply Conventional POx processes frequently use the oxygen molecules produced by traditional gas separation processes (eg, pressure twist adsorption, cryogenic distillation) that typically operate at a temperature below 100 ° C. Since the POx itself typically requires a high operating temperature of more than 800 ° C, the integration between the partial oxidation reaction and the traditional oxygen separation is not effected by the conventional process. As a result, conventional partial oxidation has frequently been characterized by low feed conversion, low ratio of hydrogen to carbon monoxide and low selectivities of hydrogen and carbon monoxide. Additionally, the external oxygen supply typically required in a partial oxidation reaction adds significantly to the capital and operating costs, which can add up to as much as 40% of the total production cost of synthesis gas. It should be noted that the use of a solid electrolyte membrane for POx in an electrochemical reactor has been described in U.S. Patents 5,160,713 and 5,306,411 both to Mazanec et al., Although none of those patents describe processes for making an oxidized product together with a synergistic use of a gas turbine system. Two of the most attractive features of the ion transport membrane system are the infinite selectivity of the membrane for oxygen transport and its ability to transport oxygen from a low pressure stream to a high pressure stream while there is a relationship of partial pressure of oxygen of more than 1, as it is the case when the infiltrated oxygen reacts with a combustible gas. For the purpose of this invention, ion transport membrane materials that transport oxygen ions are considered useful for the separation of oxygen from gas mixtures containing oxygen. The types of membrane materials efficient in the transport of oxygen ions are described in commonly assigned US Patent Application Serial No. 08 / 490,362, entitled "Method for Producing Oxygen and Generating Power Using Solid Electrolyte "Integrated with a Gas Turbine Membrane", filed June 4, 1995, and the concurrently filed No. 1 application, entitled "Method of Producing Hydrogen Using Solid Electrolyte Membrane," which are incorporated herein by reference. U.S. Patent Application Serial No. 08 / 490,362 discloses methods for utilizing the high combustion chamber temperatures achieved by a power generation system to drive an oxygen production system at acceptable operating temperatures for both systems . That application also describes a method that efficiently produces oxygen and energy as the products. U.S. Patent Nos. 5,516,359, 5,562,754. 5,565,017 and European Patent Publication No. 0 658 366 produce oxygen in processes that are integrated with a gas turbine. It is not considered that ion transport systems have been previously used efficiently to produce other chemical gas products in conjunction with the gas turbine power generation capabilities. Although the concept of integrating a gas separation unit with gas turbine systems is not known, it has not been considered that synergistic use has been made of the energy integration between the air separation unit where the oxidized products are processed together with the gas turbine systems with which the oxygen transport separation membrane is integrated.

OBJECTS OF THE INVENTION It is therefore an object of the invention to provide an improved process for making efficient use of an ion transport membran reactor to produce oxidized products, such as synthesis gas, in which the reactor is integrated with a generation system. energy to produce both energy and the oxidized product It is another object of the invention to provide a synergistic use of high temperature gas discharge from the ion transport system to feed a gas turbine combustion chamber in a synergistic manner, in where an oxidized product such as a synthesis gas is generated using a solid electrolyte membrane. It is another object of the invention to provide a process that efficiently uses the oxygen-free retentate gas that arises from an ion transport membrane reactor by feeding it into a power generation system. It is another object of the invention to provide a process that efficiently uses the combination of oxygen-infiltrate gas and reagent (and, optionally, a moderator) to make oxidized products, such as synthesis gas, in an ion transport membrane reactor. It is a further object of this invention to provide the process systems that use the high combustion temperatures achieved by a power generation system for generating energy and for facilitating the laser tranmsport in an ion transport membrane reactor.

BRIEF DESCRIPTION OF THE INVENTION This invention comprises a process for producing oxidized products, such as a synthesis gas, together with a gas turbine system for generating energy. This process includes contacting a gas stream containing compressed and heated oxygen, typically air, with at least one solid electrolyte oxygen ion transport membrane in a reactor. The reactor has a retentate zone and an infiltrated zone separated by the membrane, wherein at least a portion of oxygen is transported through the retentate zone to the infiltrated zone to generate an infiltrated stream and a retentate stream devoid of oxygen. A reagent such as a hydrocarbon is passed into the infiltrated zone to react with the transported oxygen to generate the oxidized product. The retentate stream lacking oxygen is added to a gas turbine combustion chamber where it is heated by combustion reactions with a fuel and forms a gas stream devoid of burned oxygen, which is recovered from the turbine combustion chamber of gas and expanded in a turbine expander to generate energy. In an alternative embodiment, the substantially sulfur-free synthesis gas is produced together with a turbine to generate energy. A gas stream containing heated and compressed oxygen is contacted with at least one oxygen selective ion transport membrane of solid electrolyte in a membrane reactor. This reactor has an aliemntation zone and an infiltrated zone separated by the membrane, where at least a portion of the oxygen is transported through the membrane from the zone of inflow to the infiltrated zone to generate an infiltrated stream and a stream of oxygen. retained oxygen lacking The current and fuel are passed into the infiltrated zone to react with the oxygen transported to generate the synthesis gas. The synthesis gas is passed into an acid gas remover to recover the sulfur to form a synthesis gas substantially free of acid. The oxygen-free retentate stream is fed to a gas turbine combustion chamber and the gas stream devoid of burned oxygen recovered from the gas turbine combustion chamber is expanded in a turbine expander to generate power. In a preferred embodiment, the gas stream containing compressed oxygen is extracted from the air compressor of the gas turbine. The process further comprises obtaining a gas stream lacking oxygen, expanded from the turbine and recovering the heat from the gas stream lacking expanded oxygen. A moderator is charged to the gas stream containing reagent before contacting the membrane.

BRIEF DESCRIPTION OF THE DRAWINGS Other objects, features and advantages will be devised by those with experience in the art from the following description of the preferred embodiments and the accompanying drawings, in which: Figure 1 is a schematic representation of the main components of a system to elaborate an oxidized product and generate energy in accordance with this invention; Fig. 2 is a schematic representation of a system for producing synthesis gas and generating energy in accordance with this invention in which heat is recovered from the infiltrated product and / or exhaust from the gas turbine to form steam for subsequent use , where in addition only a portion of the gas containing oxygen is directed towards the transport membrane of Figure 3 is a schematic representation of a system similar to that of Fig 2 where only a portion of the oxygen-containing gas is directed towards the ion transport membrane in a countercurrent direction of the flow against the reagent and the moderator and, the vapor generated from the esacpe of the gas turbine is not recovered for use in the ion transport membrane as the moderator, Figure 4 is a schematic representation of another confomity system with the present invention wherein the infiltrated product enters to an acid gas unit for purifying the synthesis gas resulting from sulfur and other impurities, the gas cycle unit is passed to the gas turbine combustion chamber and the gas containing complementary oxygen is used. the complementary air compression / interengaging units, Figure 5 is a schematic representation of a system according to this invention where the oxygen-containing gas is directed towards the ion transport membrane in a countercurrent direction of flow against the reagent and the moderator and a portion of the oxygen-containing gas is used to cool the product gas and the gas containing complementary oxygen; Fig. 6 is a schematic representation of another system in which the oxygen-free retentate gas is partially cooled by heat exchange before being fed to the gas cycle and where the complementary oxygen-containing gas is used; and Figures 7a and 7b are schematic representations of a comparative system for producing synthesis gas and an independent gas cycle for generating energy respectively.

DETAILED DESCRIPTION OF THE INVENTION The invention can be carried out using the heat generated by the partial oxidation reactions to provide at least a part of the energy needed to generate energy from a gas turbine. Unproductive air (retention gas devoid of oxygen) is heated by thermal energy, conducted through the ion transport membrane, from partial oxidation reactions. The unproductive heated air is then introduced into the gas turbine system to convert the heat from the chemical reactions into mechanical energy while the oxidized product is generated in the infiltrated zone of the ion transport membrane. The present invention integrates the combination of reactor (seprator) systems of partial oxidation of ion transport membrane with gas turbines. Partial oxidation is the main reaction in the reactor and is highly exothermic. The steam reforming reaction, an endothermic reaction, may take place, although preferably, in a smaller amount. This invention is directed to the production of an oxidized product such as a synthesis gas, as well as to the production of numerous other chemical products, including but not limited to methanol, ammonia and urea, or for the production of hydrogen and / or monoxide of carbon for use in the chemical, petrochemical and refining industries. As used in this, the term "retentate zone" is defined as the area within the ion transport membrane reatcor confined by the reactor walls, the gas inlet / outlets and the ion transport membrane, in which the gas that it contains oxygen, usually air fed, traverses and from which oxygen was transported to a separate area through the membrane. The resulting gas stream in the retentate zone is at least partially oxygen depleted. As used herein, the term "infiltrated zone" refers to the area within the ion transport membrane reactor in which it has been transported. oxygen from the retentate zone through the ion transport membrane. Due to the infinitely selective oxygen nature of the ion transport membrane, the resulting gas that emerges from the membrane in the infiltrated zone is pure oxygen gas. As used herein, "oxidized product" refers to products that have been partially or completely oxidized within the infiltrated zone of the reactor. It should be noted that various embodiments of this invention are directed to retrofit systems having certain existing components or incorporation into existing gas turbine designs. The gas containing complementary oxygen and the complementary gas compressors and / or intercooling units are used to provide the oxygen necessary for the production of oxidized products such as synthesis gas and / or for pre-turbine combustion. The methods of this invention can be used with a variety of modifications to the system described herein. Fig. 1 describes a general modality thereof. As shown in System 100, Fig. 1, the oxygen-containing gas stream 105 passes through the retentate zone 101 of the gas reactor 115, which comprises at least one solid electrolyte ion transport membrane. The reactor 115 is integrated with a gas turbine system 150, which comprises a gas compressor 130. a gas turbine combustion chamber 140 and a gas turbine 120. A retentate portion of the gas stream containing Oxygen 105 passing through the reactor 115 emerges as the retentate gas stream lacking oxygen 112, which is directed towards the combustion chamber of the gas turbine 140. The reactive stream 110 is combined with the oxygen infiltrated gas which it has transported through the solid electrolyte ion transport membrane 103 within the infiltrated zone 102, emerges as the partial oxidation product stream 125 therefrom. In one embodiment, the heater 111 is a heat exchanger and the partial oxidation product stream 125 (125a) and optionally the stream 112, are passed through the heat exchanger 111. The partial oxidation product stream 125 is passed to through the heat exchanger 111 to emerge as the chilling partial oxidation product stream 127 In a preferred embodiment, the partial oxidation product stream 125 is derived from the oxygen-containing gas stream 128 which passes through the compressor 130 to emerge as the gas stream containing compressed oxygen 135. A first portion 134 of stream 135 passes through heater 111 to form the gas stream containing compressed oxygen, heated 105 before entering reactor 115 and optionally second portion 136. of the stream 135 is directed towards the combustion chamber of the gas turbine 140 The portion 136 of the stream of g The compressed oxygen 135 enters the combustion chamber of the gas turbine 140, as does the gas stream lacking oxygen. The compressed stream 137 containing combustion products and oxygen-depleted gas is directed into the turbine 120 to generate power 145, as well as to activate the compressor 130 by arrow 142. Emerging from the gas turbine 120 is the exhaust of turbine 139, which may optionally be passed as waste, or for a steam cycle, or for other uses known to those skilled in the art. It is important (in the current state of material technology) to limit the temperature rise of the membrane elements in the reactor to about 1250 ° C, preferably 1100 ° C, to avoid significant degradation of the membrane material by loss of oxygen from the material to the reduction side (anode). This can be achieved by balancing the exothermic heat of the partial oxidation reaction with the endothermic vapor reforming reaction and the sensible heat from the temperature rise of the gases fed into the ion transport reactor. This consideration may favor maximizing the mass flow of the oxygen-containing gas through the system. Special consideration is given to the internal heat transfer design of the reactor to avoid excessive reduction of the temperature of the membrane element (must be greater than 700 ° C to 800 ° C). The design should provide high heat transfer coefficients where the difference of temperature between the reactor element and the oxygen-containing gas is small and small coefficients where the temperature difference is large. Typically, fluid inlet temperatures should be between 300 ° C and 700 ° C. In system 220, Fig. 2, a reactor containing ion transport membrane 205 is integrated with a gas turbine for production of synthesis gas and power generation in accordance with this invention. A stream of compressed gas is heated by passing through a heat exchanger in countercurrent flow against the exhaust from the ion transport membrane stage. A source of water from a Rankine energy generator is heated by indirect heat exchange against the synthesis gas to form steam from it, where the current is recycled to the Rankine energy generator for addition of additional heat and subsequent energization of the steam turbine in the Rankine power generator. In this embodiment, the gas stream containing oxygen 201 is compressed by the compressor 202, forming a gas stream containing compressed oxygen 209. A portion 206 of the air stream 209 is fed directly into the combustion chamber 208. Generally, a significant volume of compressed gas is necessary to operate a gas turbine system. As used herein, the amount of gas containing compressed oxygen that is fed to operate a turbine varies up to about 95% of the total gas containing compressed oxygen. In order to maintain sufficient oxygen-containing gas to support the synthesis gas production in reactor 205 so that the gas turbine system operates at its output or maximum efficiency, the gas containing complementary oxygen is used. The supplemental oxygen containing gas 203 is fed through the compressor to form the compressed complementary oxygen containing gas 524. A portion 212 of the gas stream containing compressed oxygen 206 is combined with the gas stream containing compressed complementary oxygen 254 forming the gas stream containing compressed oxygen 251. It should be noted that the gas containing complementary oxygen is generally used with existing gas turbine designs. This is because the pre-existing turbine designs may not contain sufficient sources of oxygen-containing gas to support the reactions within the reactor 205 For gas turbines designed for the process of this invention, sufficient gas containing oxygen and the supplemental oxygen containing gas would not be necessary The gas stream 251 is heated in the heat exchanger 211 against the flow of product heated from the reactor 205 After emerging from the heat exchanger 211, the heated compressed gas stream 270 has a temperature in the range from about 300 to about 800 ° C, preferably from 400 to about 650 ° C. Further heating of the gas stream containing compressed oxygen 270 may be required for the required high temperature operation in the reactor 205. This is especially true if significant amounts of current are fed to the reactor to maximize the reforming reaction of the reactor. steam and achieve the high hydrogen ratio: carbon monoxide for the synthesis gas. The heated compressed oxygen-containing gas stream 208 then enters the combustion chamber 229 to form the stream of burnt compressed gas 250, which emerges from the combustion chamber and enters the retentate zone 298 of the reactor 205. The current of burnt compressed gas emerging from the combustion chamber is then hot enough to effect the ion transport as it enters the retentate zone 298 of the reactor 205. In the retentate zone 298, oxygen is typically removed from the gas stream 250 within the range of about 2% to 50% of the oxygen contained in the stream 250. The flow fed to the reactor 205 must be within that percentage ratio of the feed flowing into the aforementioned gas turbine. The resulting oxygen separated through the ion membrane 297 is reacted with reagent 225 and steam 231 within the infiltrated zone 298 of the reactor 205.

Reagent 225 is heated in heat exchanger 221 prior to feeding into reactor 205. Reagent 225 can be any hydrocarbon reagent capable of combining with oxygen gas to produce synthesis gas. Preferably, the reagent is a lower chain saturated hydrocarbon gas similar to methane, ethane or propane. Steam 231 serves as the moderator to optimize the temperature and the reaction condition to generate the synthesis gas using the oxygen gas and a reagent through the water-gas bypass reaction. The vapor 231 is preheated through the heat exchanger 211 before the feed into the reactor 205 The oxygen is removed from the compressed gas stream 250 through the ion transport membrane 297 in the reactor 205. The oxygen permeate is it reacts with the reagent 225 and the vapor 231 in the infiltrated zone 299 of the reactor 205 The reagent 225 and the vapor 231 are prepared and preheated before reacting in the infiltrated zone 299. The synthesis gas product 213 is produced by the reaction of oxygen infiltrated with reagent 225 and steam 231 The synthesis gas product 213 is produced by the reaction of the oxygen gas infiltrated in the infiltrated zone 299 of reactor 205 with reagent 225 and steam 231, which enters the infiltrated area 299 of the reactor 205 The resulting product emerging from the reactor 205 is the hot synthesis gas 213, generally between the operating temperature range of the membrane from about 500 ° C to about 1200 ° C, with the temperature scale from about 900 ° C to approximately 1100 ° C being the most preferred. The temperature of the membrane is maintained between approximately 500 ° C and 1200 ° C by balancing the integral heats of reaction and the sensible heat derived from the rise in temperature of the internal gas streams to the reactor. See U.S. Patent Application No. of the Series entitled "Integrated Solid Electrolyte lonic Conductor Separator Cooler" (Proxy Case No. D-20356), and the patent application of the States Unidos No de Sene titled "Solid Electrolyte lonic conductor Reactor Design" (Case of Attorney No. D-20352), both presented herewith and both incorporated herein by reference. The synthesis gas product 213 emerges from reactor 205 at a high level. temperature A number of devices can be used to transfer the heat energy from the synthesis gas product 223 to other components of the heat container in the system 210 The temperature of the synthesis gas stream 213 can initially be reduced optionally by the use of an attenuator 265 to form synthesis gas stream 218 at an ordinarily manageable temperature to transfer heat in conventional devices. The attenuator is preferably water, although it can be any refrigerant known to those skilled in the art. The synthesis gas stream 218 is then passed through the burner device 216 against the water stream 241, so that the water stream 241 is converted to the steam 242 and forms the stream of the synthesis gas 219. The synthesis gas 219 retains sufficient heat so that the synthesis gas stream 219 transfers the heat against the gas stream containing compressed oxygen 251, the reagent 225 and a portion of the stream 211 emerging as moderator gas stream 231. The resulting temperature of the stream of the synthesis gas 220 is high enough to transfer the energy to the water 261 in another heat transfer device 217, thereby forming the final product of synthesis synthesis gas 227 and the conversion of the cooling water 261 to water hot 241. The oxygen-free compressed retentate exhaust stream 222 emerges from the retentate zone 298 of the reactor 205 and is added to the chamber. turbine combustion unit 208, which decouples the operating temperature of the reactor 205 from that of the turbine 293. The compressed gas stream lacking heated oxygen 247 emerges from the combustion chamber 208 and enters the expansion turbine 215 to produce the total energy 230. The Arrow energy can be used to produce electricity through a generator or energize another device such as a compressor.

Optionally, the gas stream lacking expanded oxygen 214 operates a Rankine energy generation cycle. The hot gas stream 214 enters a plurality of heat exchangers 234, 236 and 245 to produce the boiling gas stream 235, hot gas stream 244 and waste stream 224, respectively. The pump 221 drives the water 240, which comprises the accumulated water 239 and the water 238 from the condenser 223, sequentially through the heat exchangers 245, 236 and 234 against the gas stream lacking expanded oxygen 214 emerging from the gas turbine 293 In this embodiment, the Water driven by the motor 240 passes through a plurality of heat exchangers 245, 236 and 234, which emerge as the current 255, 256 and 258 respectively. The feed steam turbine 260 with the steam 258 generates the total energy 259 for driving an electric generator or other devices that need energy such as a compressor, as well as the water pump 221 The condenser 223 converts the vapor 237 into water 238 A portion of water 240, before entering heat exchanger 245, is diverted by forming water stream 261 and heated through heat exchanger 217 against hot synthesis gas stream 220 to emerge through heat exchanger 217 as a current water 241 Additional heating of the water stream 241 in the heat exchanger 216 against the synthesis gas stream 213 emerges as steam 242 The steam 242 is further heated in the heat exchanger against the synthesis gas stream 219, which emerges as superheated steam 231, which is the moderator for the reaction with the infiltrated oxygen and reagent 225 in the infiltrated zone 299 of reactor 205. A portion of the gas stream containing oxygen 206 is preferably fed into the combustion chamber 208 to provide more oxygen-containing gas to the combustion chamber. In an alternative embodiment of Fig. 2, as shown in shading and by dashed lines, the intercooler 233 and the compressor 207 are provided. The gas stream 251 enters the intercooler 233 to cool the gas before it enters the compressor 207. to reduce the power of the compressor. The compressor 207 is used to raise the pressure of the combined gas stream 251. The intercooler is optional. The gas emerging from the gas compressor 207 enters the heat exchanger 211. The steam from the Rankine cycle can be recycled A portion of the steam 242, before entering the heat exchanger 211, is separated into the steam 267. The steam 267 is diverted for recycling and combination with the stream 256 in the Rankine cycle In this embodiment, a portion of the steam 261 generated by the water from the Rankine cycle and the heat against the streams of the synthesis gas product 218 and 22o, is recycled to generate the energy 259 through the steam turbine 260 The system 310, Fig. 3, presents a preferred embodiment for an ion transport membrane containing the reactor which is integrated with a gas turbine for the production of the gas synthesis and power generation according to the invention. In this embodiment, the oxygen containing gas for use in the ion exchange reactor is fed into the reactor in a countercurrent direction of the flow of that of the reactant and the vapor. The heat generated in the oxygen infiltrated zone of the reactor is sufficient to maintain the ion transport membrane at a suitably high temperature so that continuous transport of oxygen through the ion transport membrane is possible without raising the gas that It contains oxygen up to a temperature before entering the reactor. The required inlet temperature depends on the heat balance and the internal heat transfer to the reactor, and the requirement that the membrane temperature has to be maintained at approximately 1250 ° C. As a result, the oxygen-containing gas fed into the reactor does not require the gas containing compressed oxygen to rise to the temperature scale of about 600 ° C to 900 ° C, as is the case when the gas is heated by a gas chamber. combustion; instead, the gas containing compressed oxygen to be fed into the reactor requires only that the gas stream be at a temperature above about 200 ° C to 400 ° C, like those of a conventional heat exchanger for recovery known to those skilled in the art. Alternatively, the necessary heat transfer can be added internally to the reactor. It should be noted that in the starting phase of a process employing the transport membrane, a gas supply having a sufficiently high temperature effective to initiate the oxygen infiltration reaction through the capacity of the membrane may be required. Once the reaction between the infiltrated oxygen with the reagent and the moderator has begun, the resulting heat generates a temperature sufficient to sustain the continued reaction by the use of a gas containing compressed oxygen and other materials of lower temperature. so that the heated gas having high temperature from a combustion source would not be required. In detail, this embodiment uses only a portion of the oxygen-containing gas stream 301, to feed it through the ion transport membrane 397. As used herein, the amount of oxygen-containing gas stream directed toward The ion transport membrane is generally a limitation of the machinery in the current state of the art. Currently, the gas turbine compressors available for use herein limit the air that can be extracted from the compressors to about 25%. The remaining portion of the gas is directed to the combustion chamber 308. The remaining portion of the gas is directed toward the combustion chamber 308 As a result, the compressed gas stream 348 is divided so that one portion 345 is directed towards the reactor 305, and another portion is directed towards the combustion chamber 308 to drive the gas turbine 315. The gas stream containing oxygen 345 is directed to the intercooler 333 and the riser compressor 307 which forms the oxygen-containing gas stream 355, which is subsequently heated with reagent 302 and moderator 331, preferably vapor, all heated against the gas stream of synthesis 326 in the heater 311. The resulting oxygen-containing gas stream 323 is then fed into the the retentate zone 398 of the reactor 305 in a countercurrent direction of the reagent flow 325 and the moderator 331. A portion of the oxygen-containing gas stream 32 is transported through the ion transport membrane 397 resulting in a gas of infiltrated oxygen, which reacts with reagent 325 and moderator 331 introduced into infiltrated zone 399 of reactor 305. A partial oxidation (and steam reforming) reaction takes place within infiltrated zone 399 of reactor 305 between the oxygen-containing gas infiltrated, the reagent 325 and the moderator 331 to the produced synthesis gas product 313 emerging from the reactor 305. The synthesis gas product 313 is at a high temperature as a result of the exothermic reactions in the Infiltrated zone 399 of membrane 397 of reactor 305. The temperature must be kept below 1250 ° C to avoid exceeding the temperature tolerance limit. to the membrane material by means of the appropriate heat balance and the heat transfer media inside the reactor. The temperature of the synthesis gas product 313 can optionally be reduced by the attenuator 339, preferably water, which results in the synthesis gas stream 328. The hot synthesis gas product 328 passes through a plurality of heat exchangers. 316, 311 and 317, emerging from each heat exchanger as the refrigerant gas streams 326, 303 and 327 respectively. The non-oxygen retained gas stream 351 emerging from the retentate zone 398 of the reactor 305 is combined with the fuel 343 to the combustion chamber 308. The fuel can be any convenient fuel., including hydrocarbons such as natural gas, a fuel oil or fuel gas generated from coal. The portion of the gas containing compressed oxygen 348 that is not directed to the reactor 305 is the gas stream 346, which is fed to the combustion chamber 308, providing the majority of the oxygen for combustion and forming the combination with the streams 343 and 346, which results in a gas stream containing oxygen 347. The gas stream lacking expanded oxygen 314 is used to operate a Rankine energy generation cycle. The hot gas stream 314 is subjected to a plurality of heat exchanger devices. heat to lower the temperature of the gas stream through each heat exchanger The hot gas stream 314 emerges from the gas turbine 315 and then passes through a plurality of heat exchangers 319, 321 and 326 to successively produce cooling water streams 320, 322 and 324 respectively. The water stream 352 is partially separated in stream 332 for use with a moderator in reactor 305 and stream 349 for driving steam turbine 329. Water stream 349 is heated against the flow of gas flow through the stream. heat exchangers 326, 321 and 319 to successively produce hotter streams 353, 354 and 336. Steam turbine 329 operates to produce total energy 330 from steam 336. Steam 334 is condensed in water by condenser 335 emerging as condensed water 357, which combines with the accumulated water 358. A pump 338 extracts the condensed water 357 and the accumulated water 358 together forming the water 352 for recycling In addition to providing water, as a steam source for the steam turbine 329 , steam 352 is deflected in stream 332 which is heated through a plurality of heat exchangers 317, 316 and 311, as described above, to produce the current 331 as the moderator for the reaction in the reactor 305 As an alternative embodiment, the water stream 332 from the Rankine cycle is not provided as a moderator for the production of the synthesis gas in the reactor 305 Instead, the water stream 332 is derived from an independent source of the Rankine cycle. The control valve 360 is also provided as an alternative mode for regulating the flow of the oxygen-free retentate gas stream 351 emerging from the reactor 305 to feed the combustion chamber 308. fig. 4 provides System 410, which is directed to a reactor that contains an ion transport membrane integrated with a gas turbine to produce an oxidized product and power generation and also combined with a gasification apparatus. This embodiment illustrates a more efficient use of the ion transport membrane in combination with an energy generating apparatus. In this embodiment, as in System 310, Fig. 3, the gas stream containing compressed oxygen for use in the ion exchange reactor is fed into the ion transport reactor in a flow direction countercurrent to the flow of the ion. reactive and vapor. The heat generated in the oxygen infiltrated zone of the reactor is sufficiently high to maintain the temperatures that ensure the continuous transport of oxygen through the ion transport membrane without raising the oxygen-containing gas to a high temperature before entering the reactor. gas inside the reactor. In general, the internal heat generation due to the partial oxidation reaction in the reactor 405 will be sufficient so that the oxygen-containing gas 425 does not have to be above 650 ° C. This eliminates the need for an additional combustion chamber in the stream 423 The oxygen-containing gas 401 is fed into the air compressor 404, emerging as the gas containing compressed oxygen 448, which is divided into gas stream 446 for feed to combustion chamber 408 and gas stream 445 for feed to ion transport membrane reactor 405. The gas stream containing compressed oxygen 445 is cooled in the heat exchanger 459 against water stream 461, emerging as a gas stream 462. The complementary oxygen-containing gas stream 463 passes through a plurality of compressor stages 495 and 494 probes, to produce the gas stream that contains compressed and intercooled oxygen 464. The gas streams 462 and 464 combine to form gas stream containing compressed and intercoolled oxygen 465, which passes through the intercooler 433, the compressor 407 and the heat exchanger 411 (against the stream of oxidized product 406) to emerge as gas stream containing compressed oxygen, burned 423 to feed reactor 405. The stream of gas containing compressed oxygen, burned 423 is passed within the retentate zone 498 of the reactor 405 so that oxygen is transported through the ion transport membrane 497 towards the infiltrated zone 499 of the reactor 405 Reagent 402 passes through the heat exchanger 411 against stream 406, emerging as reagent 425 together with moderator 431 (vapor), also emerging from heat exchanger 411 against stream 406, are fed into infiltrated zone 499 of reactor 405 on the opposite side and the direction of flow from the gas stream containing compressed oxygen 423. Reagent 425 and moderator 431 react with the oxygen infiltrated by a partial oxidation reaction and synthesis gas 413 emerges from reactor 405 therefrom. The temperature of the stream of oxidized product 413 can optionally be reduced by combining with an attenuator 439, preferably water, resulting in synthesis stream 428. The stream of oxidized product 428 can then pass through a plurality of heat exchangers 416 , 411 and 417 to successively produce the refrigerant synthesis gas streams 406, 423 and 427. The oxidized product stream 427 passes through the cooler 440. Emerging as the oxidized product 470. The acid gas removal apparatus 471 removes a gas stream 472 containing sulfur and other impurities from the oxidized product stream 470 for further treatment, i.e., sulfur recovery Sulfur-free synthesis gas 473 emerges from the acid gas stripping apparatus 471 and is used as a fuel and is combined with the gas stream lacking oxygen 451 and the gas stream containing oxygen 446 in the chamber of ombustión 408 to drive the expansion turbine 415. The gas 447 emerging from the combustion chamber 408 passes through the turbine 415 to generate the energy 418 and to drive the compressor 404 through the arrow 412 The gas stream 414 emerges from the gas turbine 415 and enters into a Rankine power generation cycle. The gas stream 414 passes through a plurality of heat exchangers 480, 482 and 484 in the Rankine cycle to successively produce the refrigerant waste gas streams 481, 483 and 424 A portion 491 of water 490 is fed into the exchangers heat 484, 482 and 480 against the flow of gas streams 414, 481 and 483 to successively produce the hottest currents 485, 486 and 436 The resulting superheated steam 436 is fed into the steam turbine 429 to generate the energy 430 The condenser 435 condenses the water vapor 434 to water 457 The pump 489 extracts the water 457 to form the water 490 to be recycled for use in the steam turbine 429, or alternatively, to be used as water 432 for the eventual conversion in the steam moderator 431 A portion of the water stream 432 can also be divided to form the water stream 461, which then passes through the heat exchanger 459 to emerge as the hot water stream 475 The hot water stream 475 can be recycled and combined with the hot water stream 485 before passing through the heat exchanger 482 to emerge as steam 436 to feed the steam turbine 429. System 510 in Fig. 5 provides a mode wherein the oxygen-containing gas is fed into an ion membrane reactor in the same flow direction as the reagent and the vapor. The outgoing synthesis gas product is maintained at a lower temperature by the heat sink provided by the air. This gas containing oxygen fed is used to cool the product stream when carbon dioxide is used as an optional moderator. The oxygen-containing gas 501 is fed into the compressor 504 emerging as the gas stream containing compressed oxygen 548, which is divided into the gas stream 540 for feeding into the combustion chamber 508 and as the gas stream 549 directed towards the interpreamer 533. The complementary oxygen-containing gas 577 passes through the compressor 506 to emerge as the current of compressed, complementary oxygen-containing gas 554 The gas stream 554 is combined with the gas stream 549, forming the compressed compressed oxygen-containing gas stream 551, which passes successively through the cross-fertilizer 533, the compressor 507 and the heat exchanger 511 to emerge as the gas stream containing compressed oxygen 555 Current 555 is greater than that required to provide the oxidant in reactor 505 Therefore, a portion of this gas stream can be diverted into the combustion chamber of the gas turbine. The fuel 552 is added to the combustion chamber 529 wherein the preheated compressed oxygen containing gas 555 is burned, emerging as the burned oxygen containing gas 550 for feed into the retentate zone 598 of the reactor 505. The flow direction of the gas containing compressed burnt oxygen 550 is in a countercurrent direction of flow with reagent 525 and moderator 531, which is fed into infiltrated zone 599 of reactor 505. Oxygen from the gas stream containing burnt oxygen Compressed 550 is transported through the ion transport membrane 597, resulting in oxygen transported in the infiltrated zone 599. The transported oxygen then reacts by partial oxidation with the reagent 252 and the moderator 531 to emerge from the infiltrated zone 599 of the reactor 505 as synthesis gas 513. Optionally, attenuator 539, preferably water, can be added to the gas synthesis 513, resulting in the synthesis gas stream 527, to reduce the temperature thereof before emerging as the synthesis gas 527. The attenuated synthesis gas passes through the heat exchanger 511, and emerges from it. as the synthesis gas stream 503. Air is used to reduce the temperature of the synthesis gas stream 503. The heat exchange device 517 can be used to reduce the temperature of the synthesis product stream 503, to emerge as the product of crude synthesis gas 527. Reagent 502 is passed through heat exchanger 511 emerging as heated reagent 525. Water stream 542 from a Rankine power generation cycle is used as the moderator and heated also in * the heat exchanger 511, emerging as the water stream 531. As noted above, both reagent 525 and moderator 531 enter through the infiltrated zone 599 of the actor 505. Emerging from retentate zone 598 of reactor 505 is the retentate gas stream lacking compressed oxygen 522, which together with the gas stream containing compressed oxygen 555 and fuel 543 are passed into the combustion chamber of the gas turbine 508 as noted above. Emerging therefrom is a burned gas stream to drive the gas turbine 590 The expansion turbine 515 is linked to the compressor 504 by the arrow 512, which drives the compressor 504 and generates the energy 518 The gas stream containing burnt oxygen 547 emerges from the combustion chamber 508 and feeds the expansion turbine 515, to emerge as the gas stream 514. A Rankine power generation cycle is employed to use the hot gas stream 514. The gas stream 514 is fed into the a plurality of heat exchangers 580, 582 and 584 in the Rankine cycle to successively emerge as the refrigerant waste gas streams 581, 583 and 524. The water 590 is fed into the heat exchangers 584, 582 and 580 against the flow of gas heated warheads 583, 581 and 514 to successively produce the hottest streams 585, 586 and the vapor stream 558, which is fed into the steam turbine 529. The operation of the steam turbine 529 generates the energy 530 and results in the current 537. The condenser 555 can be used to condense the water vapor in the current 537 to water 557. The pump 589 facilitates the accumulated water 558 to be combined with the water 557, forming the water 559 as an optional means to heat the water 559 for use in the steam turbine 529 is achieved by diverting a portion 591 thereof through the heat exchanger 517 against the synthesis gas stream 503 before combining the heated water 559 with the water stream 585 emerging from the heat exchanger 584 A portion of the saturated steam 586 emerging from the heat exchanger 582 is divided into the current 542 for use as the moderator for the reactor 505 As noted above, the current 542 is heated in the int heat exchanger 511, emerging as superheated steam 531 before entering reactor 505 System 610, as shown schematically in Fig 6, provides an alternative embodiment to System 210 of Fig 2 In this embodiment, the retentate gas devoid of oxygen from the reactor is partially cooled before entering a gas cycle. The oxygen-containing gas 601 passes through the compressor 603, resulting in the compressed oxygen-containing gas 606. The complementary oxygen-containing gas 607 is passed through the compressor 618, emerging as the complementary compressed oxygen containing gas 654. A portion of the gas stream containing compressed oxygen 606 is combined with the gas stream containing compressed oxygen 654 forming the gas stream containing compressed oxygen 651 of gas containing compressed oxygen is treated successively in the interendapter 633, the compressor 607 and the exchanged r of heat 611 before passing through combustion chamber 629, emerging as compressed burnt oxygen containing gas 650 A combustion chamber fuel 652, such as any suitable fuel, including hydrocarbons such as natural gas fuel oils or fuel gas generated from the coal can be used to feed the combustion chamber 629 The temperature of the reagent 602 is raised by the heat exchanger 611, forming the reagent 625 The stream 644 is also treated in the heat exchanger 611, forming the steam 631 The gas stream containing compressed combusted oxygen 650 is fed into the retentate zone 698 of reactor 605 resulting in oxygen infiltrated through the ion transport membrane 697 into the infiltrated zone 699. The introduction of reagent 25 and moderator 631 within the infiltrated zone 699 of reactor 605 promotes partial oxidation in the infiltr zone 699 of reactor 605, emerging as synthesis gas stream 613 therefrom. The temperature of synthesis gas 613 can optionally be reduced by the addition of attenuator 639, such as water, where synthesis gas 628 emerges therefrom. The temperature of the synthesis gas is reduced by successively passing it through the heat exchangers 616, 611 and 617, emerging from them in sequence order! the synthetic synthesis gas streams 626, 620 and 627 as the crude synthesis gas product. The oxygen-depleted gas stream 622 emerges from the retentate zone 698 of the reactor 605 and passes through the heat exchanger 611 and emerges as the refrigerant oxygen retention gas stream 651. Synthesis gas 629 transfers heat to the water stream for use in reactor 605 and also for recycling in the Rankine power generation cycle. Water 661 emerging from the Rankine cycle passes through heat exchangers 617 and 616, emerging from them successively as the hottest 641 water and steam 642. Steam 642 is divided into steam 644 and 645 Steam 644 is further heated in the 611 heat exchanger emerging as superheated steam 631 Alternatively, the vapor 645 is recycled into the Rankine cycle to be combined with the vapor 686. The gas stream 622 that has been fed through the heater 611 emerges as the refrigerant gas stream 651. The fuel 643, which can be any suitable fuel, including hydrocarbons, such as natural gas, fuel oils or gas generated from coal and, gas stream 651 and a portion 691 of stream 606 are used to generate heat in combustion chamber 608. gas stream 647 passes through the expansion turbine 615 to drive the air compressor 603 by the arrow 612 and to generate the energy 630 Emerging from the turbine d 615 gas is the expanded oxygen containing gas 614. A Rankine power generation cycle uses the gas stream 614 from the gas turbine 615 The gas stream 614 is fed through a plurality of heat exchangers 680, 682 and 684, successively emerges therefrom as cooling waste streams 681, 683 and 624 A portion of the water 661 is fed into the heat exchange devices of the Rankine cycle 681, 683 and 624 in the heat exchangers 684, 682 and 680, emerging successively therefrom as the hottest water stream 685 and steam 686 and superheated steam 658, respectively As mentioned before the steam 645 recycled from the Rankine cycle and heated indirectly by synthesis gas 628 and 620 is combined with Steam 686 Steam 658 emerging from the 680 heat exchanger drives the 665 steam turbine, resulting in 666 power and 637 condenser 667 current The water vapor 637 is fed into the water 668, which is combined with the accumulated water 669 to form the water 661. The pump 670 pressurizes the water streams 668 and 669 into the water stream 670 into the Rankine cycle. An alternative embodiment is the source independently of moderator 644 Here, the water stream 642 is not divided Instead, the water streams 642 and 645 are the same current and are recycled in the Rankine cycle The moderator 644, which can be water, dioxide carbon, argon or other type of moderator known to the person skilled in the art, comes from a source different from that of System 610 and is passed through heat exchanger 611 before entering infiltrated zone 699 of reactor 605 A comparison of two operating systems demonstrating some of the advantages of this invention are provided by the embodiment of Fig 3 (in its alternative mode) and 7 The system mode 710 Figs 7a and 7b are compared with that of the alternative embodiment of the system 310 fig 3 System 710 provides an example where the heat results from the ion transport membrane reactor that is not integrated with gas turbine and power generation devices Consequently, Fig. 7a provides a schematic representation of the ion transport membrane reactor process and FIG. 7b provides a schematic representation of a gas cycle and a vapor cycle, both independent of the ion transport membrane reactor. The system includes a gas turbine, the Brayton 793 cycle and the Rankine 794 cycle includes a current turbine. The advantages of the present invention, wherein the ion transport membrane reactor is integrated with gas cycle and steam cycle power generation, will be evident by comparing the reduction in the energy requirement and the cost of capital associated with the present invention. In the system 710, the oxygen-containing gas for use in the ion exchange reactor 705 is fed in a countercurrent direction of the reagent flow 725 and the moderator 731. The heat generated in the infiltrated zone 799 of the reactor 705 is a a temperature high enough so that the continuous transport of oxygen through the ion transport membrane 797 is available without burning the oxygen-containing gas before subjecting the gas inside the reactor 705. In Fig. 7a, the oxygen-containing gas stream 701 is directed to the ion transport membrane 798 The gas stream 701 passes through the compressor 704 and the heat exchanger 711 to emerge as the heated, compressed oxygen-containing gas 723, the which is fed into the retentate zone 799 of the reactor 705 in a countercurrent direction of the flow from the reagent stream 725 and the moderator (vapor) stream 731. Both reagent stream 725 and steam stream 731 are fed into of the infiltrated zone 799 of the reactor 705. The oxygen permeated through the ion transport membrane 797 in the infiltrated zone 799 of the reactor 705 is reacted with the reagent 725 and the vapor 731. The partial oxidation reaction is presented and results in synthesis gas 713, which emerges from infiltrated zone 799 of reactor 705. The temperature of synthesis gas 713 can optionally be reduced by an attenuator 739, preferably water, thereby forming the stream of synthesis gas 728. The resulting synthesis gas stream 728 passes through a plurality of heat exchangers 716, 711 and 717 to successively produce refrigerant synthesis gas streams 726, 703 and the raw synthesis gas product 727 The water 728 passes through a plurality of heat exchangers 717, 716 and 711 to successively produce the hottest water 741 and the steam 742 and the superheated steam 731 The reactive gas stream 702 is heated in the heat exchanger 711 emerging as the heated reagent 725 The oxygen-free retentate gas stream 751 emerging from the retentate zone 798 of the reactor 705 can optionally be cooled by attenuator 780, preferably a stream of water, before going through the expander 781, thereby producing the stream 782 and the energy 783. Separately, in fig. 7b, the oxygen-containing gas 760 is compressed in the compressor 761. The gas containing compressed oxygen 762 emerges from it and passes through the combustion chamber 764. The fuel 763 is burned in the combustion chamber 764 and emerges the gas containing burnt oxygen, compressed 765 therefrom. The gas stream 765 passes into the expansion turbine 766, producing the energy 767 and drives the air compressor 761 via the arrow 768. The gas stream 769 emerging from the gas turbine 766 is used to operate a Rankine power generation cycle. The hot gas stream 769 is subjected to a plurality of heat exchangers 719, 721 and 759 to successively produce the refrigerant waste streams 720, 722 and 724, which emerge from the heat exchangers, respectively. The water stream 749 is fed into the plurality of heat exchangers 759, 721 and 719 in the Rankine power generation cycle, so that hot water 753 and steam 754 and superheated steam 736 emerge successively from the heat exchangers respectively. Steam 736 is used to drive steam turbine 729, generate energy 730 and water vapor 734. Condenser 735 condenses water vapor 734 into water 752 for recycling through the plurality of heat exchangers by motorized means 738. Table 1 provides a summary of energy generation through the production of synthesis gas using the ion transport membrane. This Table provides a comparison of the integrated and non-integrated energy cycle and partial oxidation through an ion transport membrane reactor.Table 1 Comparison of integrated and non-integrated energy cycle and partial oxidation through the ion transport membrane reactor Base Case: Present Invention: No generation integration of energy and energy cycle integration by synthesis gas in steam reforming through a gas base by partial oxidation ln transport membrane reactor Combustible energy plant (natural gas in Ib-mol / h) Combustible (natural gas in Ib-mol / h) 473 9 505 66 Total utb / h in fuel 191,095,135 Total utb / h in fuel 203,902,017 Fuel (POx) in lb-moi / h) 1000 GT simulation, hp 54,384 Total fuel utb / h 403,239,365 GT energy (xO 98), kw 39,759 GT simulation, hp 57, 833 Comp GT, hp 26,645 GT energy (xO 98), 42 kw, 281 Comp GT, kW 19,877 Comp GT, hp 29, 776 Water pump, hp 55 Comp GT, kW 22, 213 Water pump, kW 41 Comp promoter hp 325 ST at 85% efficiency 10,021 Promoter comp kW 242 Total energy from ST 7139 Water pump hp 57 Total energy from the energy cycle, Water pump kW 43 kW 27,021 Transport membrane of lón / POx ST to 85% effic 10,, 532 Combustible (natural gas in Ib-mol / h) Total energy from ST 7, 511 1000 Total utb / h in fuel 403,239,365 Total energy, kW 27,336 Air Compressor, hp 7,708 Air Comp, kW 5,750 Heat Scale utb / kwh (based on ai) Expander, hp 7,654 8 fuel used in the Expander cycle, kW 5,596 energy only) 6 991 Heat scale utb / kwh (based on the Steam Cycle, kW or fuel used in the Total Energy cycle -154 energy and POx) 21 742 Total Energy, kW 26,867 Heat Scale, utb / kWh (based on the fuel used in the energy cycle only) 7,589 Scale Heat, utb / kwh (based on the fuel used in the energy cycle and POx) 22 598 Entries Higher than 5c / kWh, $ / year 187,706 Fuel Savings, $ / year 224.987 Capital savings in compressor and expander 2 000 000 Base Operation -8,000 h / year Fuel (HHV) at $ 2 20 / MMutb Comparing the summary for energy cycle integration and partial oxidation through ion transport membrane separators, the integrated system of the present invention provides clearly an economic advantage over the non-integrated system. In the alternative mode of System 310 and System 710, the same amount of synthesis gas is produced from 1000 Ib-mol / h of natural gas. However, in the integrated process of the present invention, more energy is produced due to the better heat integration. As a result, the total energy produced from an integrated process is 27,336 kW compared to 26,867 kW in the base case (not integrated). For equal power output from the gas turbines in the two modes, the integrated process uses approximately 6% less fuel. Based on the conventional operation of 8000 hours / year and the cost of natural gas (HHV) at $ 2.20 / MMutb, the integrated system of the present invention can expect significantly higher inputs of approximately $ 188,000 annually at 5c / Kwh, as well as a fuel cost savings of $ 225,000 annually. Additionally, the previous capital savings for the elimination of separate use of compressor and expander for the production of synthesis gas total up to approximately $ 2,000,000. Existing gas turbine power generation systems can be re-filled with an ion transport system in accordance with the present invention. Those systems may include those available from General Electric Co., Schenectady. New York, Siemens, Germany or ABB, Switzerland. The modifications to these gas turbine systems are minimal, including the addition of a gas stream fed to the ion transport stage and an ion transport exhaust feed to a combustion chamber that supplies the gas for the turbine expansion. The ion transport membranes employed herein are constructed of dense ceramic oxides or mixtures of oxides, characterized by oxygen gaps in its glass grid caused by defects or the introduction of dopants (such as Y, Sr, Ba, Ca and the like). A gap diffusion mechanism is the means by which oxygen ions are transported through the glass grid. In general, elevated temperatures (400 ° C to 1250 ° C, such as within the range from about 500 ° C to about 1200 ° C, preferably within the range of about 900 ° C to about 1100 ° C) should be maintained during the operation to reach high mobilities of the holes. Large concentrations of gap combined with high void mobilities from the base for rapid transport of oxygen ion through the materials from which the ion transport membranes are constructed. Since only oxygen atoms can occupy the glass grid, the ideal transport membranes have infinite oxygen selectivity. Ion transport membranes suitable for use herein can be constructed from materials that are mixed conductors and that do not require an external circuit to facilitate electron movement. Examples include double phase membranes. The uses of different combinations of ion transport membranes are described in United States Serial No. 08 / 444,354, filed May 18, 1995, entitled "Pressure Driven Solid Electrolyte Membrane Gas Separation Method", which is incorporated to the present by reference. Different types of ion transport materials can be employed which maintain the spirit of the present invention. For example, the ion transport membrane can be comprised of a material that is primarily an oxygen ion conductor, such as zirconia stabilized with triazole. ("YZY"), sandwiched between two porous electrodes In practice, oxygen molecules diffuse through one of the porous electrodes to the electrolyte surface, at which point dissociation occurs in oxygen ions that first porous electrode provides electrons for the process Oxygen ions are diffused through the electrolyte and reach the second porous electrode, where the combination occurs forming oxygen molecules in this way and releasing electrons in the process The electrons are returned to the first porous electrode for oxygen ionization by an external circuit As an alternative, the ion transport membrane uses The present invention may be comprised of a material that conducts both oxygen ions and electrons. Such materials are often referred to as mixed conductors. For the mixed conductor ion transport membranes, the electrons are returned to the side of high oxygen partial pressure. the ion transport membrane by electronic conduction through the ion transport membrane itself thus eliminating the need for an external circuit. The ion transport membranes themselves are not commercially available so far. However, the materials used to prepare the ion transport membranes are obtained from Praxair Specialty Chemicals, Woodinville, Washington, for example. The commercially available materials used to prepare the ion transport membranes can be manufactured by conventional techniques, such as extrusion, slide coating, satin coating, dip coating, spin coating and the like on thick self-supporting films, thin films supported on a porous substrate. suitable, in disk-like and tubular configurations. The thickness of the ion transport membrane should be less than about 5000 μm, with less preferred than 500 μm and below about 50 μm being most preferred. If the thickness of the film is large (for example, approximately 1000 μm), the ion transport membrane can be self-supporting. Alternatively, the ion transport membranes may be in the form of a thin film, which may be supported on a porous support, having a thickness within the range of about 500 μm to about 5000 μm. Such porous substrates may be constructed of the same or different materials as the ion transport membrane itself. The ion transport membranes of the mixed conductor type can be prepared from a variety of materials including those listed in Table 2 below. In Table 2, d is the deviation from the oxygen stoichiometry. In addition, the values x and y may vary with the material composition.

Table 2: One of the materials of the La-i xSrxCu family? yMy03 d, where M represents Fe or Co, x equal from zero to approximately 1, and equal from zero to approximately 1, d equal to a number that satisfies the valences of La, Sr, Cu and M in formula 11 One of the materials of the Ce? -xAx? 2-d family, where A represents a lanthanide, Ru or Y, or a mixture of the same, x equal from zero to about 1, and equal from zero to about 1, d equal to one number that satisfies the valences of Ce and A in the formula 12 One of the materials of the Sr? -xBi? Fe03-d family, where A represents a lanthanide or Y, or a mixture thereof, x equal from zero to about 1, and equal from zero to about 1, d equal to a number that satisfies the valences of Ce and A in the formula 13 One of the materials of the SrxFeyCoSOw family, where x equal from zero to approximately 1, and equal from zero to approximately 1, z equal from zero to approximately 1 w equal to a number that satisfies the valences of Sr, Fe and Co in the formula 14 Mixed double phase conductors (electronic / ionic) (Pd) os / (YSZ) os (Pt) os / ((YSZ) 05 (B-MgLaCrO?) os (YSZ) 0. (ln9o% Pt10%) or 6 / (YSZ) os (ln9o% Pt? o%) or 5 / (YSZ) os (ln95 Pr25% Zr2 s%) os / (YSZ) 05 Any of the materials described in 1-13 to which is added a high temperature metal phase (for example Pd.Pt, Ag, Au, T ?, Ta, W) The electronic / ionic mixed conductors of Article 14 in Table 2 are dual-phase mixed conductors that are composed of physical mixtures of an ionically conductive phase and an electronically conductive phase. For the application of the reduction at the anode, chromium is preferred. contains mixed conductive material due to better stability at low partial pressure of hydrogen Electrically driven transport membranes based on ionic conductors can be selected from the following materials in Table 3 Table 3 Conductor Ion Transport Materials lomeo 15 ( B? 203)? (My? Oy2)? x where M can be selected from Sr, Ba, Y, Gd, Nb, Ta, Mo, W, Cd, Er and combinations thereof and x is greater than or equal to 0 and less than or equal to 1 16 CaTio 7AI03O3 x where x is greater than or equal to 0 and less than or equal to 1 17 CaTio 5AI05? 3 d where d is determined by stoichiometry 18 CaTio 9dMgo os03 x where d is determined by stoichiomepa 19 Zr02-Tb407 20 Zr02-Y203-B? 203 21 BaCeOs Gd 22 BaCe03 BaCeOs Y, BaCe03, Nd 23 LaxSr1 -xGayMg1 -y03-d 'where x is greater than or equal to 0 and less than or equal to 1, and is greater than or equal to 0 and less than or equal to 1 and d is determined by stoichiometpa For a given application, the size of the Selected ion transport membrane is typically linked to the flow (i.e., the amount of oxygen per unit area per unit time) of oxygen through it. High oxygen flow values are desirable so that a small ion transport membrane area to efficiently remove oxygen from the compressed and heated gas entering the ion transport reactor The smaller ion transport membrane area reduces the cost of capital The oxygen flow at any location on the membrane The ion transport depends on many factors, including the electrolyte ionic conductivity, the thickness of the membrane and the difference of chemical potential of oxygen The selection of material for a membrane type gas reaction favors a material of optimum stability with adequate conductivity A compromise can be made on the conductivity due to the driving force of high oxygen pressure ratio. Maintaining the ion transport membrane at a sufficiently high temperature (typically around 400 ° C, more typically above 600 ° C) contributes to the optimization of the performance in the process and system of this invention since the membrane The conductivity of the ion possesses appreciable oxygen ion conductivity at elevated temperatures and the conductivity increases with increasing temperatures. Higher temperatures can improve the kinetics of surface exchange processes on the surfaces of the ion transport membrane. The specific features of the invention are shown in one or more of the drawings for convenience only, since each feature can be combined with other features according to the invention. Those skilled in the art will recognize the alternative embodiments and are intended to be included within the scope of the claims.

Claims (10)

1 . A process for producing an oxidized product together with a gas turbine system for generating energy comprising the steps of: a) contacting a gas stream containing compressed and heated oxygen with at least one ion transport membrane solid electrolyte oxygen in a reactor, the reactor having a retentate zone and an infiltrated zone separated by the membrane, wherein at least a portion of the oxygen is transported through the membrane from the retentate zone to the infiltrated zone to generate an infiltrated stream and a retentate stream lacking oxygen; b) passing a reagent into the infiltrated zone to react with the transported oxygen to generate an oxidized product therefrom; c) adding the retentate stream lacking oxygen to a gas turbine combustion chamber; and d) expanding the gas stream devoid of oxygen recovered from the gas turbine combustion chamber into a gas turbine, thereby generating energy. The process of claim 1, wherein the gas containing compressed oxygen is extracted from a gas turbine compressor before step (a).

3. The process of claim 1, further comprising obtaining a gas stream lacking expanded oxygen from the turbine and recovering the heat from the gas stream lacking oxygen-expanded.

The process of claim 1, wherein a portion of the gas stream containing oxygen is compressed by a compressor at least partially driven by the turbine and the gas stream containing complementary oxygen is added to the gas stream which compresses compressed oxygen before it makes contact with the membrane in stage a).

The process of claim 1, wherein the reagent is mixed with a moderator before passing into the infiltrated zone.

The process of claim 1, wherein the infiltrated stream is directed to preheat the stream of oxygen-containing gas and reagent.

The process of claim 1, wherein the oxygen-containing gas stream flows in a countercurrent direction relative to that of the reagent in step b).

The process of claim 1, wherein the operating temperature of the membrane is within the range from about 500 ° C to about 1200 ° C.

9. A process for producing a substantially sulfur-free oxidized product together with a gas turbine for generating energy comprising the steps of: a) contacting a stream of compressed and heated gas with at least one transport membrane of Oxygen of solid electrolyte in a reactor, the reactor having a retentate zone and an infiltrated zone separated by the membrane, wherein at least a portion of the oxygen is transported through the membrane from the retentate zone towards the infiltrated zone to generate an infiltrated stream and a retentate stream lacking oxygen; b) passing a reagent within the infiltrated zone to react with the oxygen transported to generate an oxidized product from the same; c) passing the oxidized product of step b) into an acid gas remover to recover the sulfur resulting in a product with partial oxidation substantially free of sulfur; d) adding the retentate stream lacking oxygen in a gas turbine combustion chamber; e) burning the partially sulfur-free oxidized product in the gas turbine combustion chamber; and d) expanding the gas stream devoid of oxygen quenched from a gas turbine combustion chamber in a gas turbine expander, thereby generating energy.

10. The process of claim 9, wherein a gas stream containing compressed oxygen com plemetary is. added to the gas stream containing compressed oxygen before contacting the membrane in step a).