 Thermally Powered Oxygen/Nitrogen Plant Incorporating an Oxygen Selective Ion Transport Membrane
专利摘要:
The present invention is a low energy cost process for the simultaneous production of oxygen and nitrogen generating gas, the fuel supply tube 506 extending to the oxygen selective ion conductive membrane 424 fuel 440 near the closed end (closed end) It is introduced and flows together with the oxygen containing gas in an oxygen selective ion transport membrane and annulus 510 having a separation portion 436 and a reaction portion 438. The oxygen-containing feedstock 406 is compressed and contacts the cathode side 426 of the separator 436, where some of the oxygen moves to the anode side 428 to form the oxygen generating gas. It is recovered. Substantially, the remaining oxygen moves from the cathode side 426 to the anode side 428 and exothermic with the fuel. The hot nitrogen-rich product gas is expanded in the turbine to generate power to compress the feedstock. The expanded nitrogen rich gas is soon recovered from the turbine exhaust. 公开号:KR20010032208A 申请号:KR1020007005400 申请日:1998-11-13 公开日:2001-04-16 发明作者:크리스티안프리드리히 고쯔만；라비 프라자드；니틴라메쉬 케스카；제임스브레그돈 울프 申请人:조안 엠. 젤사 ; 로버트 지. 호헨스타인 ; 도로시 엠. 보어；프랙스에어 테크놀로지, 인코포레이티드； IPC主号:
专利说明:
Heated Oxygen / Nitrogen Plant Incorporating an Oxygen Selective Ion Transport Membrane with Oxygen Selective Ion Transfer Membrane Related Applications The present invention is a partial continuing application (CIP) of oxygen and power generation (Keskar et al.) Using the solid electrolyte ion conductor of US patent application Ser. No. 08 / 972,020, filed November 18,1997. U.S. Government Rights The present invention was made with the support of the United States Government under the Cooperation Treaty 70NANB5H1065 by National Standards and Technical Studies. The United States government has certain rights in the invention. Well-known Rankine meteorological power cycles or variations thereof (eg reheating and regeneration cycles, dual pressure cycles, co-generation cycles) are often used to produce power. Water vapor in these systems is generally used as a working fluid because of its readily available, chemical stability and relatively low cost. During the cycle, heat is applied to the system to produce water vapor at high pressure, which in turn is expanded through the turbine to produce power. Gas turbine power cycles are similar to gas phase power cycles in that: each process is a stable flow process performed as a separate component. However, the working fluid in gas turbine power cycles is typically air or fuel and combustion products of air. Air is a mixture of gases containing 20.9% by volume of oxygen, 78% by nitrogen, 0.94% by argon and other traces of residual gas containing a fluid amount of water vapor. If fuel is used in such a system, heat is produced in the system as the fuel is burned in the compressed air stream and the combustion gas stream is expanded through the gas turbine to produce power. Metallurgical temperature limits in gas turbine blades require very high air / fuel ratios in gas turbine operation. In conventional gas turbine systems, excess nitrogen present in the feed air and the combustion product gas stream cools the heat and thereby lowers the temperature of the combustion product gas stream. As a result, the gas stream discharged from the gas turbine power cycle contains excess oxygen so that other fuels can be further combusted. The hot gas thus discharged can be used to preheat the compressed feed air or to produce steam for use in steam power cycles. The latter combined power plant is called a COGAS plant. It is also possible to recover some or most of the oxygen without using it to burn from the gas turbine cycle using ion transfer membrane technology. Most oxygen generation systems use cryogenic gas separation methods (high purity, large scale) or diaphragm and adsorptive separation techniques (90-95% pure, small to medium scale). Conventional non-cryogenic bulk oxygen separation systems, such as organic polymer diaphragm systems, are typically applied only to the production of power-intensive, low oxygen-rich air (eg 50% oxygen). These conventional processes deal with some of the power used to produce the product, but they did not produce any net power. In addition, conventional oxygen separation processes are operated at low temperatures (less than 100 ° C.) and do not receive noticeable benefits from the integration of power generation processes. On the other hand, completely different types of diaphragms can be made from certain inorganic oxides. These solid electrolyte diaphragms are prepared from inorganic oxides and are formulated with calcium- or yttrium-stabilized zirconium and similar oxides with fluorspar or perovskite structures. Although the potential of the oxide ceramic material as a gas separation membrane is very good, they have some problems in use. The biggest problem is that all of the known oxide ceramic materials exhibit desirable oxygen ion conductivity only at elevated temperatures, ie they are at temperatures above 700 ° F (370 ° C), typically in the range of 800 ° F to 1850 ° F (425 ° C to 1000 ° C). It must be manipulated in. These limitations are still not overcome despite efforts to find materials that operate well at lower temperatures. The solid electrolyte ion conduction technology is described in detail in the staged electrolyte diaphragm of U.S. Patent No. 5,547,494 (Parasad et al.) And in the pressure-driven solid electrolyte membrane gas separation method of U.S. Patent No. 5,733,435. Cited. Operationally elevated temperatures, however, make the ion transfer process suitable for merging high temperature processes such as vapor-based, gas-based or combined power cycles. US Pat. No. 4,545,787 (Hegarty) 's process for producing off-site from turbine power generation refers to a process for generating pure power using a combustion turbine with the recovery of oxygen-rich gas as a by-product. The air is compressed and heated, at least a portion of the air is combusted and some oxygen is removed from the air or combustion emissions using an air separator. Oxygen-depleted combustion emissions expand through the turbine and produce power. Alternatively, emissions from the turbine may be used to produce water vapor to generate additional power. The type of fuel in this process is limited to clean fuels such as natural gas, oil or syngas. Oxygen extraction from external combustion gas turbines in US Pat. No. 5,035,727 (Chen) refers to a process for recovering high purity oxygen from an external combustion power generation gas turbine cycle. The process is similar to the Hegarty mentioned above, except that Chen uses an external combustion gas turbine and that other types of fuel can be used, such as coal or biomass. Oxygen recovery from turbine discharge flows using solid electrolyte membranes in US Pat. No. 5,174,866 (Chen et al.) And Oxygen recovery from turbine discharge flows using solid electrolyte membranes in US Pat. No. 5,118,395 (Chen et al.) Reference is made to the process of recovering high purity oxygen from the gas turbine exhaust stream by passing the gas turbine exhaust stream over the ion conductive membrane. In these processes, the oxygen separator using the oxygen ion conductive membrane is installed at a part of the gas turbine or downstream of the previous stage, as opposed to the upstream portion of the previous patent. An electrically-driven ion transport unit is provided when the turbine discharge pressure is low. The discharge flow from the oxygen separator is selectively expanded through additional gas turbine stages. U.S. Pat. No. 5,562,754 (Kang et al.), "Integrated High Temperature Methods for Oxygen Generation," describes oxygen production by ion transfer membranes, wherein ion transfer separators are characterized by two independent controlled direct (e.g., combustion engines). In) or between indirect heating devices. The permeate side of the ion transport membrane is washed away by water vapor. The oxygen-containing gas stream is moderately heated in a directly heated combustor, passes through the retentate zone of the ion transport membrane and then directed to the gas turbine to produce power. The impervious flow here is immediately dumped into the outlet. In US Pat. No. 5,565,017 (Kang et al.) 'Production of Hot Oxygen by Steam and Power', the gas turbine is incorporated into an ion transport membrane for heating and steam, followed by recovery of energy from a retentate gas stream. It refers to the system. Water is applied to the holding gas flow from the ion transport device in front of the gas turbine to increase the mass flow in the turbine. This allows the ion transport device and gas turbine to be operated at optimum temperatures, respectively. In US Pat. No. 5,516,359 (Kang et al.) 'Integrated High Temperature Method for Oxygen Generation,' a first heating step (using a heat exchanger and a combustion tube) is carried out before passing the heated and compressed air through an oxygen separator using mixed conductive oxides. The compression and heating of the supply air at) are described. The holding gas flow from the ion transport device is heated in the second heating stage before expanding through the gas turbine for power generation. Hot exhaust gas from the gas turbine is used to produce steam, which is then expanded through the steam turbine to produce another power source. In this process, the operating temperatures of the ion transfer device and the gas turbine are independently maintained by controlling the heating rate in the first and second heating steps. Oxygen generation by ion-transfer membranes with non-permeate work recovery in US Pat. No. 5,753,007 (Russek et al.) Describes a combination system of oxygen recovery and useful work recovery. The hot, non-permeable gas is recovered from the cathode of the ion selective oxygen transfer membrane. The non-permeable gas is cooled to near ambient temperature inside the heat exchanger and expands to low pressure to generate shaft power, which can operate pneumatic tools, for example. No prior patents describe the simultaneous production of nitrogen, the incorporation of ion transport membranes into Rankine power cycles, and / or the like in US Pat. No. 08 / 972,410 (prasad et al., 'Production of Solid Electrolyte Ion Oxygen by Steam Purge'). No purge of the permeate surface of the ion transport membrane with combustion products or water vapor, or with respect to steam at elevated pressures and recovery of oxygen and nitrogen at elevated pressures. This prior art describes that ion transport membranes can be used to recover some of the oxygen that is not needed for combustion from the compressed air stream in the gas turbine cycle, but this replaces the oxygen removed with the oxygen removal system with capital loss. Only by compressing the additional feed air. Summary of the Invention The present invention consists of a process for generating a gas flow from which oxygen is removed from a feed gas stream containing oxygen and a high pressure gas flow including oxygen and water vapor. The feed gas stream is compressed and heated, and the heated feed gas contains oxygen at the permeate side of the ion transfer membrane and the gas flow from which oxygen is removed from the holding surface using at least one first ion transfer device including an ion transfer membrane. Separated by a gas stream. The permeate surface is purged using a high pressure purge gas flow containing water vapor to generate a high pressure gas flow containing oxygen and a purge gas. The discharged high pressure permeate gas stream containing oxygen and water vapor expands in the turbine and generates power to produce a low pressure gas stream containing oxygen and water vapor. Preferably, the expanded low pressure gas stream containing oxygen and water vapor is divided into water and oxygen gas streams by condensing water in a water- or air-cooled condenser. According to a preferred embodiment of the present invention, the heat contained in the retentate stream is recovered in the heat exchanger to preheat the inlet air. The high pressure purge gas flow is directed to the second turbine and is sufficiently superheated to avoid condensation during expansion in the second turbine. The high temperature retention flow expands sufficiently with or without additional heating in another turbine. According to another preferred embodiment of the present invention, the retention flow from the ion transfer membrane purged with water vapor is treated in a deoxo stage consisting of a reactively purged ion transfer membrane to simultaneously flow the high purity nitrogen product. Create According to another preferred embodiment of the present invention, the permeate side of the oxygen separation unit is purged by a permeate stream exiting the deoxo reaction unit and optionally a low pressure or medium pressure steam generated by heat recovery from the gas turbine discharge stream. It can be purged by to create a low to medium pressure product stream consisting of oxygen, water vapor and carbon dioxide. Low-purity oxygen containing mainly CO 2 as impurities can be recovered by condensing water vapor. Optionally, the downstream system can separate this stream into oxygen and selective byproduct CO 2 . According to another embodiment of the present invention, the nitrogen retention flow from the deoxo reactor is cooled to an appropriate temperature (1200 to 1400 ° F.), which allows the use of structural standards in turbines such as 17-4 stainless steel. This is a sufficiently low temperature, while sufficient temperature to hold sufficient energy potential to operate the air compressor while using only a portion of the holding flow, thus allowing for recovery of residues of the flow, such as nitrogen products, at elevated pressures. According to a preferred embodiment all the energy required to operate the separation system can be provided by the generation of heat by the oxygen-fuel reaction in a deoxo reactor. According to a preferred embodiment, the selective pressure and temperature swing preliminary agent is installed in an air supply line to remove water, carbon dioxide and other impurities from the stream and, as a result, to recover high purity nitrogen. In a preferred embodiment the beds of the prepurifier are regenerated by exhaust gas from the expansion turbine. In a preferred embodiment, the oxygen transfer membrane (OTM) separator and the deoxo reactor are combined with the appropriate preheating and cooling sections in a single unit, thereby placing the main components such as tube thin films and shells, etc. in a suitable temperature environment. It allows the use of standard engineering materials such as stainless steel or carbon steel and allows the tube to be easily manufactured from tube thin film joints. In a preferred embodiment all the tubes are one end free floating to avoid stress due to thermal and component dimensional changes. The present invention relates to the use of a solid electrolyte ion conduction system in a gas separation system. More specifically, the present invention purges the permeation surface of the solid electrolyte ion conductive membrane using combustion products and / or water vapor from the ion transfer membrane reactor to increase the efficiency of the process and generate oxygen, carbon dioxide and water vapor flow. It relates to a solid electrolyte ion conducting system which obtains pure oxygen product easily at the same time, produces nitrogen at elevated pressures and generates sufficient power to operate the system's air compressor. 1 is a schematic diagram of the invention for separating oxygen from air using a steam-purged solid electrolyte ion conducting device together with a steam turbine and a heat recovery device downstream of the heat recovery portion and ion transfer device. FIG. 2 shows the incorporation of oxygen separation by a steam-purged ion transfer device into a steam Rankine cycle and a gas turbine, and is a detailed view illustrating the recovery of oxygen from the steam-oxygen mixture by condensing water returned to the Rankine cycle. Figure 3 is similar to Figure 2, in which a deoxo device is integrated into the process to produce a high-purity co-product nitrogen stream, and a more efficient two-stage Rankine cycle maximizes generation of by-product power during oxygen and nitrogen production. A schematic diagram of the present invention showing the integration into a system for the purpose of doing so. 4 is a schematic diagram illustrating an integrated oxygen and nitrogen production system including an oxygen selective ion transport membrane and a turbine. 5 shows a turbine / 3 stage compression assembly used in some embodiments of the invention. FIG. 6 is a schematic representation of an embodiment of the present invention, similar to FIG. 4, further comprising turbine emissions used to regenerate the adsorption bed in the pre-purifier. 7 shows a cross sectional view of a first reactor useful for the simultaneous production of oxygen and nitrogen in accordance with an embodiment of the present invention. 8 shows a cross sectional view of a second reactor useful for the simultaneous production of oxygen and nitrogen in accordance with an embodiment of the present invention. The present invention relates to an invention in which an ion-transfer oxygen separator is installed in a steam-based fluid or combined-cycle power generating structure in which the permeate surface of the ion transfer membrane is purged by high pressure steam. This steam purge enhances the transport of oxygen through the ion transport membrane and facilitates the recovery of oxygen from a feed gas stream, such as air. After the permeate gas stream containing water vapor and oxygen is expanded and cooled in a steam turbine, the water condenses from the gas stream and is saturated with water vapor but a pure oxygen gas stream can be obtained. In another part of the structure, a partially oxygen-retentate gas stream from the ion transport device is burned or heated externally with fuel and expanded in the gas turbine to produce more power. Gas turbine emissions are generally hot enough to aid in the production of steam, which can be used in the process to preheat the air supplied to power generators or separators based on steam. The new invention of producing oxygen at such a very low power ratio is attractive compared to other oxygen production methods. Gases in which oxygen is separated are usefully prepared at relatively high temperatures (above 400 ° C). On the other hand, the commercial production of oxygen currently used is typically operated at temperatures below 100 ° C. Due to this limitation, the conventional oxygen separation method has not gained a noticeable increase in efficiency due to the integration of the power generation process. Therefore, the new gas separation process using the oxygen ion conductor can achieve a high synergy effect by merging with a power generation process that can significantly reduce the cost of oxygen production. The present invention enables the combination of a steam purged ion transfer membrane for separating oxygen from air and Rankine water vapor, Brayton gas and a combined Brayton / Rankin steam power cycle. The main advantages of the process of the present invention are as follows. The present invention reduces the effective partial pressure of oxygen on the purge when it is purged by using water vapor as the purge gas at elevated pressure. This enhances the driving force through the ion transport membrane, increases the oxygen flux, and makes the diaphragm smaller. Indeed, it increases the recovery of oxygen in the air and, if necessary, allows the recovery of oxygen at elevated pressures or the expansion of purge flow and recovery of power. Alternatively, the flow can be expanded to medium pressure and oxygen is recovered at this medium pressure. Purge at elevated pressures also reduces or eliminates the pressure differential before and after the ion transport membrane and facilitates structural design and sealing. The amount of oxygen recovered is changed by varying the amount of water vapor used for purging. In fact, as mentioned earlier, most of the oxygen is recovered from the feed gas. Of course, the diaphragm area will be reduced. It is easy to apply to the gas turbine cycle. This is because the operating temperatures of ion transfer separators and gas turbines can be lowered and typical gas turbines handle a significant amount of excess air. Thus, the fraction of oxygen removed from turbine air occupies only a small fraction of the total flow. The oxygen produced by the device is diluted with water vapor, making it easy and safe to operate. Despite reduced power generation, it is possible to recover oxygen and oxygen gas streams from steam turbine emissions at moderate pressures and to obtain oxygen gas at medium pressure by condensing the water vapor. By-product nitrogen can also be produced by placing a deoxo reactor with or without an external combustion heater. Simultaneously generated power can be raised and optimized by properly coupling the high pressure stage steam turbine upstream of the ion transport device. Some embodiments of coupling ion transfer membranes to gas turbine systems, including retrofits of turbine power generation systems, are disclosed in U.S. Patent No. 08 / 490,362, filed June 14,95, and its Sep. No. 08 / 933,248 (Prasad. Et al.), Filed on May 18, incorporated herein by reference. The ion transport membrane using the above-mentioned oxygen separator in the present invention is a solid electrolyte ion conductor. Ion transporters that deliver oxygen ions are useful for separating oxygen from gas mixtures. Constant ion transporters are mixed conductors that conduct both oxygen ions and electrons. At elevated temperatures, these materials have mobil oxygen ion vacancies, which provide conductive sites for the selective transport of oxygen ions through the material. Delivery is driven by the partial pressure ratio of oxygen passing through the diaphragm. In other words, the oxygen ions flow from the high oxygen partial pressure side to the low partial pressure side. The ionization of oxygen into oxygen ions occurs at the cathode surface or the retention surface of the diaphragm, and the ions migrate through the ion transport membrane. Oxygen ions are deionized at the permeate side of the diaphragm to release oxygen molecules. In the case of materials exhibiting only ionic conductivity, the external electrode is placed on the surface of the electrolyte and current flows into the external circuit. In the case of a mixed conductive material, the electrons move inward toward the anode, flowing through the circuit and eliminating the need for external electrodes. Dual phase conductors in which oxygen-ion conductors are mixed with electrical conductors can be used for the same purpose. Table 1 shows a partial list of ion transport materials used for oxygen separation. Material composition One. (La 1-x Sr x ) (Co 1-y Fe y ) O 3-δ (0 ≦ x ≦ 1, 0 ≦ y ≦ 1, δ is obtained from stoichiometry) 2. SrMnO 3-δ SrMn 1-x Co x O 3-δ (0 ≦ x ≦ 1, 0 ≦ y ≦ 1, δ is obtained from stoichiometry) Sr 1-x Na x MnO 3-δ3. BaFe 0.5 Co 0.5 YO 3 SrCeO 3 YBa 2 Cu 3 O 7-β (0≤β≤1, β is determined from stoichiometry). 4. La 0.2 Ba 0.8 Co 0.8 Fe 0.2 O 2.6 ; Pr 0.2 Ba 0.8 Co 0.8 Fe 0.2 O 2.65. A x A '' x 'A 〃 x〃 B y B' y 'B 〃 y〃 O 3-z (x, x', x 〃, y, y ', y 〃 are all in the range of 0 to 1) Where A, A ', A 〃 = 1,2,3 and f-block lanthanides B, B', B 〃 = d-block transition metal 6. (a) Co-La-Bi type: 15 to 75 mol% cobalt oxide 13 to 45 mol% lanthanum oxide 17 to 50 mol% bismuth oxide (b) Co-Sr-Ce type: 15 to 40 mol% oxidized cobalt oxide 40 to 55 mol% of trondium 15 to 40 mol% of cerium oxide (c) Co-Sr-Bi type: cobalt oxide 10 to 40 mol% strontium oxide 5 to 50 mol% bismuth oxide 35 to 70 mol% (d) Co-La-Ce type: 10 to 40 mol% cobalt oxide 10 to 40 mol% cerium oxide 30 to 70 mol% (e) Co-La-Sr-Bi type: 15 to 70 mol% lanthanum oxide 1 40 mol% strontium oxide 1-40 mol% bismuth oxide 25-50 mol% (f) Co-La-Sr-Ce type: cobalt oxide 10-40 mol% lanthanum oxide 1-35 mol% strontium oxide 1-35 mol% cerium oxide 0-70 mol% 7. Bi 2-xy M ' x M y O 3-δ (0≤x≤1, 0≤y≤1, δ is obtained from stoichiometry) where M' = Er, Y, Tm, Yb, Tb, Lu, Nd , Sm, Dy, Sr, Hf, Th, Ta, Nb, Pb, Sn, In, Ca, Sr, La and mixtures thereof M = Mn, Fe, Co, Ni, Cu and mixtures thereof 8. BaCe 1-x Gd x O 3-X / 2 , where X is from 0 to about 1 9. A s A ' t B u B' v B 〃 w O x (where each component is disclosed in U.S. Patent No. 5,306,411 (Manzanec et al.)) A is a lanthanide or Y or A 'is an alkaline earth metal or mixture thereof. B is FeB' is Cr or Ti or a mixture thereof. B 〃 is Mn, Co, V, Ni, Cu or mixtures thereof. , u, v, w are the following numbers: s / t is from about 0.01 to 100, u is from about 0.01 to 1, v is from 0 to about 1, w is from 0 to about 1. x is a number satisfying the a, a ', B, B ', B 〃 atom in the formula; And 0.9 <(s + t) / (u + v + w) <1.1 10. La 1-x Sr x Cu One-y M y O One of the 3-δ materials, wherein M is Fe or Co; x is from 0 to about 1 y is from 0 to about 1 δ is La, The number satisfying the valences of Sr, Cu and M. 11. Ce 1-x A x O One of the materials of group 2-δ , where A represents Ru or Y or a mixture thereof x is a number from 0 to about 1 y is a number from 0 to about 1 δ is a number satisfying the valences of Ce and A in the formula. 12. Sr 1-x Bi x FeO Group 3-δ , wherein A is a lanthanide or Y or mixtures thereof x is a number from 0 to about 1 y is a number from 0 to about 1 Δ is a number satisfying the valences of Ce and A in the formula. 13 Sr x Fe y Co z O w group of substances, where x is a number from 0 to about 1 y is a number from 0 to about 1 z is a number from 0 to about 1 It is a number satisfying the valences of Sr, Fe, and Co in the chemical formula. 14. Double phase mixed conductor (electrical / ionic): (Pd) 0.5 / (YSZ) 0.5 (Pt) 0.5 / (YSZ) 0.5 (B-MgLaCrO x ) 0.5 (YSZ) 0.5 (In 90% Pt 10% ) 0.6 / (YSZ) 0.5 (In 90% Pt 10% ) 0.5 / (YSZ) 0.5 (In 95% Pr 2.5% Zr 2.5% ) 0.5 / (YSZ) 0.5 Any of the materials listed in 1 to 13 (metal phase) (eg Pd, Pt, Ag, Au, Ti, Ta, W) may be added. In particular, if the permeate side of the ion transport membrane can be purged with an oxygen free flow, it is easy to produce a nitrogen product gas stream by removing most of the oxygen gas from the feed gas using a basic ion transfer process. However, it is more difficult to efficiently recover oxygen as a product with this basic process. For example, if pure oxygen is recovered as a permeate stream at atmospheric pressure, the amount of oxygen recovered is limited by the oxygen partial pressure of the holding stream being discharged. Therefore, the supply air flow must be sufficiently above 5 atm. At this pressure, the oxygen partial pressure is equal at the anode and cathode and the recovered oxygen is zero. If a steam purge is used, a positive driving force for oxygen delivery at 5 atm or lower can be maintained. Typically, an impractical shifting process may include a vacuum pumping of the permeate side of the ion transfer surface, to maintain the driving force of the permeate process without contaminating the generated oxygen gas flow. The process according to the invention uses pressurized superheated steam from a Rankine cycle system to purge the permeate side of the ion transport membrane. Due to the proper flow of water vapor, the partial pressure of oxygen in the permeate gas stream is lowered, thereby allowing oxygen permeation even when the feed gas stream is low pressure. By cooling the permeate stream, residual oxygen can be recovered and moisture can be condensed and recycled. This cooled oxygen gas stream may contain some residual water vapor but is still pure. It may be used as a product as it is or may be further dried, for example, in a polymer diaphragm or pressure or temerature swing adsorption (PSA) postpurifier. The product oxygen gas flow will be the saturation pressure of the condensed water vapor, which can be adjusted to low and medium pressure levels depending on product and power optimization. Nitrogen can be obtained as a product or coproduct at medium or high pressure. Since producing steam requires high energy, especially in terms of heat of vaporization, it is useful to use steam for power production for plant operation and / or export using compressors. Such power cycles have the ability to use the useful low levels of heat to reduce the energy needed to increase steam production. The present invention allows for high autonomy to select the pressure level for the feed gas depending on whether the feed gas is part of the turbine cycle gas or whether simultaneous products are needed at a constant pressure level. Preferred embodiments of the present invention provide high purity nitrogen co-products. In this case, the ion transfer membrane purged with water vapor recovers most of the oxygen contained in the feed gas, and the remaining oxygen is removed by downstream deoxo in the form of a reactively purged ion transfer membrane. In this case, it is advantageous to adjust the amount of oxygen to react at deoxo to a sufficient level in order to supply heat required for the necessary resin of the gas cycle. Since the oxygen reaction takes place on the permeate side, the retention flow is not contaminated with combustion products and high purity nitrogen simultaneous products can be obtained. Nitrogen is pressurized and all or part of the flow is expanded in the turbine to produce power depending on the amount of pressurized nitrogen. From a system simplification point of view, it is advantageous to operate the air compressor by expanding enough nitrogen while making the residue a co-product of elevated pressure. If the product nitrogen can contain a small amount of oxygen, deoxo is removed and the steam purged ion transfer membrane is purged of the feed gas to an acceptable residual oxygen content. An external heating heater upstream or downstream from the diaphragm can be used to compensate for heat loss from the system. One of the advantages of a steam purge system is that it provides a high recovery and thus limits the need to compress and process a significant amount of excess air. In another embodiment of the present invention, the high pressure steam expansion step is included upstream of the inlet of the permeation surface of the ion transport membrane. In order to simplify the system, the process conditions of the above steps are selected by the following method. That is, all or most of the superheat required in this step to prevent wet turbine exhaust can be provided by the useful heat of the turbine exhaust from the second low pressure steam turbine stage located downstream from the ion transport membrane. The advantage of this structure is that it can produce a significant amount of surplus power at increased fuel consumption. It is also noteworthy that the present invention does not require piping or handling operations of pure oxygen at high temperatures that threaten safety. Thus, the need for special materials and processes that deal with hot pure oxygen can be avoided and high stability can be achieved. As mentioned above, the ion transport membrane transfers oxygen when there is a difference in oxygen partial pressure before and after the diaphragm. Compared with polymer membranes, ion-transfer membranes have a higher flux and have an infinite separation factor for oxygen with respect to nitrogen. The type of ion transport device used in the present invention is a 4-port device, although the present invention is ideally manipulated as a countercurrent flow of permeation and retention in an ion transfer separator, other flow forms, such as co-current and cross-flow, are also applicable. Similar to A basic embodiment of the present invention is shown in the schematic diagram of FIG. During operation, the feed gas stream (10, generally air), containing oxygen at elevated pressure, is heated to the ion transfer operating temperature, and then ion transfer membrane 16 having retention surface 16a and transmission surface 16b. Is introduced into the ion transfer device (14). The high pressure steam purge flow 12 purges the permeate surface 16b of the ion transport membrane 16 to produce a holding gas flow 18 and a permeation gas flow 21. The use of the purge gas flow 12 reduces the oxygen partial pressure on the permeate surface 16b of the ion transfer membrane 16, thus enabling sufficient oxygen transfer even at a low supply gas pressure on the retention surface 16a. . Since the water vapor purge flow 12 mixes and dilutes the oxygen that has passed through the ion transport membrane 16, the permeation flow 21 from the ion transport device 14 contains both water vapor and oxygen at high pressure. The permeate gas stream 21 is directed to an energy extractor section 22, where the steam turbine 24 produces power 28 and releases the gas stream 26 at low pressure. The remaining thermal energy of the gas stream 26 is preferably extracted and used, for example, to superheat water vapor or to heat the boiler feed water. The holding gas stream 18, on the other hand, is directed to a heat extractor section 20 where energy is removed from the holding gas stream 18, for example by expansion by means of a gas turbine or heat transfer to the feed stream. Figure 2 is a detailed view of an embodiment of the present invention, showing the merging of an ion transfer separator purged with water vapor and a steam turbine with a gas turbine cycle. Feed gas 201, which is typically air, is compressed into compressor 202 at a pressure of 100 to 250 psig and produces compressed air flow 203. Flow 203 is preheated in heat exchanger 204 by waste heat contained in turbine exhaust 214. The compressed and preheated airflow 205 is further heated to an ion transfer operating temperature of 800-1900 ° F. (425-1035 ° C.) by combusting a portion of the oxygen contained in the fuel stream 208 in the combustor 206. The heated stream 207 enters the retention surface 209a of the cathode or ion transfer separator 209. Here, the oxygen passes through the mixed conductor ion transport membrane 247 and is moved by ion transfer to the permeation surface 209b of the separator 209 at a driving force due to the partial pressure ratio of oxygen before and after the diaphragm 247. A significant fraction of the oxygen contained in the feed stream can be separated because typical gas turbine cycles require the use of excess air at levels compatible with the useful structures used in the turbine to limit temperature rise in the combustor. In particular, oxygen-retained holding gas 210 may optionally be further heated using fuel flow 212 in combustor 211 to an acceptable turbine inlet temperature. The gas flow 213 at the turbine inlet temperature expands in the turbine 217 to generate power, which drives the compressor 202 and a generator to produce power to be discharged. Exhaust stream 214 contains useful waste heat that is used to preheat airflow 203 in a heat exchanger. Cooled flow 216 exits the cycle. Optionally, waste heat is also usefully used in combined steam cycles. This is mentioned in the examples below. In this embodiment, at least a portion of the flow exiting the gas turbine is flow 248, which provides the heat required for flow 225 to be evaporated in heat exchanger 218, which can be used for other selections. Is located in the evaporator coil. The process according to the invention purges the permeate surface with high pressure superheated steam which is then expanded in the turbine to recover power. As shown in FIG. 2, the high pressure superheated steam 232 is preferably introduced into the permeate surface 209B of the separator 209 in a counter flow with the feed flow 207. The presence of water vapor lowers the partial pressure of oxygen on the permeate surface 209B, which increases the driving force for oxygen transfer, thus reducing the required area for the ion transport membrane 247. The discharged permeate stream 234 is a mixture of water vapor and oxygen and is expanded in the turbine 235 to recover power. The exhaust stream 236 from the turbine 235 has adequate heat and can be used to partially superheat the high pressure steam 228 in the heat exchanger 229. The resulting stream 237 still has enough heat so that it can be used to warm the feedwater stream 223 in the heat exchanger 224. Most of the moisture of the stream 238 in the external cooling condenser 239 is condensed to produce a water and saturated oxygen mixture 240, which is separated in the separator 241 to produce a water stream 247 and an oxygen stream 242. do. Optionally, the oxygen stream 242 is further cooled in the cooler 243 to produce a cold oxygen stream 244, which is optionally compressed in the compressor 245 to produce the product oxygen stream 246 at the required transport pressure. If necessary, the produced oxygen can be dried using a polymer diaphragm or an adsorption dryer. The water stream 247 exiting the separator 241 is joined with the make-up water 221 and pumped to the required pressure in the water pump 222 to create a compressed feed water stream 223 which is heated in the feed water heater 224. The warmed water stream 225 is then introduced into the evaporator heat exchanger 249 to produce saturated or slightly superheated steam 228. Water vapor 228 recovers useful heat from flow 236 in heat exchanger 229 to further overheat and enter superheat coil 231 of external heating heater 218 to the operating temperature of ion transfer separator 209. The temperature is raised. The resulting superheated steam 232 is soon introduced into separator 209. Combustion in the external heating heater 218 is maintained in a combination of the fuel stream 219 and the air stream 220 which are exhausted into the stack gas flow 231. The advantages of the system over an alternating system without a Rankine steam cycle are: a significant reduction in the required ion transport membrane area, the simultaneous production of significant additional power by the steam turbine, the potential reduction before and after the diaphragm and the voltage difference. (total pressure difference), as well as the structural design of the separator, as well as the retention of the separator 209 and sealing between the permeate flow. Example 1 A comparison of the calculation results for three gas turbine cycles with oxygen simultaneous products is described below. That is, the system of the invention (case A) shown in FIG. 2, the cycle in which the gas turbine waste heat is used to purge the permeate of the ion transport separator and the oxygen is carried at elevated pressure (case B) and the oxygen co-products or water vapor Gas turbine cycle with no generation, in which case the turbine exhaust is used to preheat the air (case C) Reaction conditions Oxygen Simultaneous Product: 1000 MNCFH Air Compressed Release Pressure: 185 Psia Insulation efficiency of single stage air compression: 85% Ion Transfer Inlet Temperature: 1650 ° F (900 ° C) Turbine Inlet Pressure: 180 Psia Turbine Discharge Pressure: 16 Psia Turbine inlet temperature: 2000 ° F (1090 ° C) Turbine Efficiency: 90% Oxygen recovery: 5.6% of compressed air flow When using steam purge: Water vapor pressure: 84 psia Generated water vapor: 172 lbs / 1000 NCFH O 2 For steam turbines: Discharge Pressure: 16 Psia Steam turbine efficiency: 90% Oxygen generation pressure: 14.7 psia (case A and C) 82 psia (case B) Comparison of Experiment ResultsCase a Case b Case c Pure power KW 75,000 55,500 * 53,750 Required heat MM BTU / Hr 606 527 442 BTU / KW Hr in heat 8,080 9,490 8,220 O 2 driving force efficiency log (Po1 / Po2) 0.45 0.45 0.115 * 82 psia with O 2 compression The comparison shown in Table 2 clearly shows that two cases with steam purge have superior advantages in terms of driving power to move O 2 through the ion transport membrane compared to the absence of purge gas. . Since this value is substantially proportional to the ion transport area, a larger area is required for turbine cycles without purge gas. It can be seen that Case A, which represents the process according to the invention, is more advantageous than Case C in terms of energy use and has significant advantages over Case B. Preferred embodiments that combine additional inventive features of the present invention are shown in FIG. This embodiment is characterized by the simultaneous production of nitrogen and additional power production with the slight increase in fuel consumption by the addition of a high pressure steam turbine. Air 301 is compressed by compressor 302 to a suitable pressure of 100 to 300 Psia to produce compressed air stream 303. Compressed air stream 303 is generated by heat sources such as heat from various waste heat and product streams, as well as heat generated in ion transfer reactor 310 up to ion transfer operating temperature (typically 700 to 1800 ° F.) in heat exchanger 304. Heated. Heated and compressed air 305 is introduced into retention surface 306A of ion transfer separator 306. Here, the oxygen moves through the mixed conductor film 307 by ion transfer moving at the oxygen partial pressure ratio before and after the diaphragm 307. The permeate surface 306B of the separator 306 is purged by high pressure superheated steam. Dilution of the permeate gas with water vapor effectively reduces the oxygen partial pressure on the permeate side and thus enhances the propulsion for oxygen transfer. In applications that emphasize the generation of nitrogen and oxygen, the present invention allows for maximum oxygen recovery with minimal air flow. This is because it is not limited by the partial pressure of oxygen released from the holding gas as in the absence of purge gas. If nitrogen is desired as the co-product, separator 306 removes most of the contained oxygen from the feed stream. In this embodiment, the remaining oxygen acts as an oxidant in the reaction that acts to provide the heat needed to maintain the system, so the amount of remaining oxygen remaining in the retention stream 308 depends on the portion of the retention gas that is expanded in the turbine. It functions as a heat necessity. The flow 308 is cooled by the feed stream 303 in the heat exchanger 304 and cooled to the extent that it can absorb the heat of reaction generated in the ion transfer reactor so as not to exceed the allowable maximum temperature of 900 to 1850 ° F. Partially cooled flow 309 is introduced into retention surface 310A of ion transfer reactor 310. In this device, the remaining oxygen in the flow 309 moves through the diaphragm 356 and reacts with the fuel in the permeate stream 323 on the permeate surface 310B of the reactor 310. The reaction on the permeate side provides a very low oxygen partial pressure for efficient delivery of the holding gas to a very low oxygen content resulting in a high purity nitrogen stream 324. The heat of reaction is absorbed into the internal reactor heat transfer component by raising the temperature of the holding gas, but the local diaphragm temperature does not exceed the acceptance criteria. The preferred design of reactor internal components is addressed in the design of solid electrolyte ion conductor reactors in U.S. Pat.No. 5,820,655 (Gottzmann et al.), And is incorporated herein by reference. In an embodiment all of the hot, high pressure nitrogen gas 314 is recovered as a high pressure product. In yet another embodiment all or part of this is expanded in a hot gas expander to generate power and to deliver nitrogen product at low pressure. In terms of system simplification, it is advantageous to divide the flow 314 into two flows, one of which flow 315 is expanded in the hot gas expansion turbine 354 to provide sufficient power to operate the air compressor 302. Generates. In most cases this causes sufficient nitrogen 316 to be conveyed as high pressure product 321 after recovery of waste heat in heat exchanger 304. The heat exchanger 304 is shown as a single device and somewhat less simplified, but can optionally be divided into several exchangers to provide all the necessary heat exchange functions. A portion of the product stream 321 (preferably 5-15%) is controlled by the valve 318 to become a low pressure stream 319 and mixed with the fuel stream 320 to dilute to flow 317. Create The stream 317 is heated by a permeate waste stream 324 transmitted from the heat exchanger 322 and introduced as a stream 323 to the permeate side of the ion transfer reactor 310, the fuel contained therein being Reacts with oxygen passing through the diaphragm 356. Hot permeate waste stream 324 is discharged to flow 325 after waste heat recovery in heat exchanger 322. Alternatively, at least a portion of the permeate flow released from the ion transfer reactor is a stream 324B shown virtually, which merges with stream 315 prior to the expansion process through turbine 354. In this case the reactive purge flow is almost or exactly the holding pressure and the sizing valve 318 becomes the regulating valve. Also shown virtually, valve 358 may be included to adjust the pressure of flow 315 to a pressure on the order of flow 324B. The alternating arrangement causes the low pressure nitrogen to be contaminated with combustion products but increases the amount of nitrogen recovered at this pressure, because expansion of the permeate stream can be replaced by expansion of high pressure nitrogen. As shown in FIG. 2, the permeate surface 306B of the ion transfer separator 306 is purged with high pressure superheated steam 326, preferably at a pressure of at least 50 psia and more preferably at a pressure of at least 150 psia. The steam circuit is similar to FIG. 2 except that the high pressure steam turbine stage is included upstream of the separator 306. The description of the steam circuit is as follows. Feed water 341 is pumped to an elevated pressure (typically 300 to 1200 psig) by pump 342, heated by waste heat in feed water heater 333 as flow 343, and then boiler 347 Is introduced into the evaporator section. The high pressure steam 348 at nearly or exactly saturation temperature is overheated in the heat exchanger 331 and is sufficiently high to avoid condensation while the flow 349 expands to an intermediate pressure level in the steam turbine 350. Heated to. It is advantageous to select the following operating conditions for a steam turbine. That is, all or the majority of the superheated steam in the flow 349 may be provided with adequate heat to the exhaust 330 of the low pressure stage 329. The discharge 351 from the turbine 350 is almost saturated at the intermediate pressure and is overheated in part by the transfer of the residual waste heat useful in the heat exchanger 331, here shown as a single heat exchanger but with two separate units. It is then superheated in a superheating coil (353) of the boiler 347 as a flow 352 to generate a superheated steam 326 of the ion transfer operation temperature. Flow 326 is introduced into permeate surface 306B of separator 306 to carry oxygen transferred from retention surface 306A of separator 306. The steam-oxygen mixture 328 is expanded in the low pressure stage turbine 329 to produce power. Since the discharge 330 from the turbine is still at elevated temperature, significant heat in the stream 330 is recovered in the heat exchanger 331 and feedwater heater 333 to produce the stream 334, which is an external cooling condenser 335 is introduced and most of the water contained in the condenser condenses to form a mixture 336 of water and oxygen. Stream 336 is separated in separator 337 and separated into oxygen and oxygen 338 saturated with water and stream 338 is optionally further cooled, compressed and dried to yield product 338A. Water stream 339 discharged from separator 337 joins make-up water 340 and circulates in the system. Combustion in the boiler 347 is maintained by the combustion flow 358 and the air or oxygen flow 359 and produces a flue gas waste stream 360. 3 has a distinct advantage as shown in Example 2. The use of high pressure steam purge in ion transfer separators increases the recovery of oxygen, which is not limited by the oxygen partial pressure of the holding stream being discharged. As a result, the amount of excess air handled in a complex system can be minimized, thus minimizing costs. The use of an ion transfer reactor in combination with a deoxo and combustor has the effect of preventing nitrogen simultaneous products from becoming impure products. The nature of the ion-transfer reactor, where oxygen reacts on the anode surface of the ion-transfer membrane, enables efficient combustion even at low oxygen-fuel ratios and suppresses the generation of NOx (nitrogen oxides). This is because there is no or little nitrogen present and the reaction can take place at the anode of the diaphragm, which is designed to allow proper heat transfer and be maintained at temperatures below the typical flame temperatures of conventional combustors. Dividing the retention flow into a pressurized flow and an inflated flow to generate sufficient power to run the air compressor provides a simple and efficient system. This is because no additional device is needed to compress the nitrogen to obtain the required product pressure. The use of two-stage steam turbine expansion as reheating of the first stage effluent and the use of intermediate stage pressure flow as the purge gas in the separator has the advantage of avoiding the design of ion transport devices at very high pressures in energy efficient Rankine cycles. Very high pressures are typically required for efficient energy production from the steam stream at the high temperatures at which ion transport systems are operated. According to the invention, the design can be simplified by manipulating and balancing the variables of the system, i.e. all or most of the superheat supplied to the turbine at high pressure to prevent condensation during the expansion process is reduced to moderate heat in the second low pressure stage discharge. Can be provided by This combined system can simultaneously produce oxygen, high purity nitrogen and power with very economical fuel consumption as shown in the examples below. Example 2 Oxygen Product: 1000 MNCFH Nitrogen simultaneous product at 145 Psia: 1670 MM NCFH Air Compressed Discharge Pressure: 155 psia Air Compression Stage: 4 (The compressor is operated by hot gas expander, not by gas turbine.) Air Compression Efficiency: 85% Hot gas turbine inlet pressure: 150 psia Hot gas turbine inlet temperature: 1750 ° F (955 ° C) Hot gas turbine discharge pressure: 16 psia Hot gas turbine efficiency: 90% Ion Transfer Separator Inlet Temperature: 1650 ° F (900 ° C) Ion Transfer Oxygen Removal Exhaust Temperature: 1750 Deoxygenated Fuel Dilution: 79 MNCFH N 2 High Pressure Steam Turbine Inlet Pressure: 1000 psia Hot Turbine Inlet Temperature: 805 ° F (430 ° C) Low pressure turbine inlet pressure: 150 psia Low pressure turbine inlet temperature: 1650 ℉ Low pressure turbine discharge pressure: 16 psia Steam turbine efficiency: 90% Water vapor condensation pressure: 14.7 psia Water vapor generation: 303 M lbs / hr Experiment result: Oxygen recovery: 83% of oxygen in feed air Simultaneous generation of N 2 at 145 psia: 1670 M NCFH Pure power generation: 58,560 KW Required heat: 490 MM BTU / Hr Heat flux: 8370 BTU / KW Hr Heat flux due to N 2 compression: 7850 BTU / KW Hr Heat flux by power separation (7kw / mncfh): 7060 btu / kw hr Average efficiency of oxygen transfer drive force: 0.308 Example 2 shows a very satisfactory value for the embodiment of the invention shown in FIG. The use of a steam purge on the permeate side of the ion transfer separator increases the recovery of oxygen and thus reduces the amount of excess air required for the system. Compared with Example 1, the amount of air is less, 3.1: 1. The use of an ion transfer reactor, which functions simultaneously with the removal of oxygen and generates the heat necessary for air purification, makes it possible to recover 90% of the nitrogen contained in the feed air in high purity even in very simple cycles. 41% of the product nitrogen can be recovered at high pressure. Using a two stage steam turbine cycle enables very efficient energy utilization. The rates consume higher peak temperatures but are far superior to the best results of Example 1. Although the invention is not limited, it is important that the cycles described herein are Rankine and Brayton-Joule cycles. Therefore, the embodiments referred to herein apply to other cycles well known to those skilled in the art, such as multiple reheating and regeneration cycles, dual pressure cycles, co-production cycles without departing from the spirit of the present invention. Will be modified to some extent. It is also well known to those skilled in the art that the Brayton and Rankine portions of the above-mentioned embodiments can be further combined in practical applications, in particular in the optimal use of waste heat. In addition, the inlet conditions of the various components can be changed according to the material within a range without departing from the spirit of the present invention. For example, the purge stream exiting the ion transport membrane is cooled prior to introduction into the steam turbine, or the separator or deoxygenation retention flow is cooled before entering the hot gas expander. Since the process of the present invention can be run in part by low levels of heat, it can be combined with other processes that generate heat, including processes that use oxygen products to generate heat. When operated with a high pressure supply, the present invention can be combined with gas turbines or other devices to generate power from high pressure products or waste streams as shown in the examples. Typical ranges of operating parameters of the ion transfer device are as follows. Temperature: In an ion transfer device, the temperature is usually in the range of 700 ° F to 2000 ° F (370 ° C to 1100 ° C), preferably in the range of 1000 ° F to 1850 ° F (535 ° C to 1010 ° C). Steam turbines typically range from 400 to 1700 ° F. Gas turbines typically operate in the range of 1300-2600 ° F. Pressure: The pressure at the purge surface is typically 1 atm to 40 atm, preferably in the range of 1 atm to 12 atm. The feed side pressure ranges from 1 atm to 40 atm when pressurized nitrogen is required as a product or when ion transfer exhaust gas enters the gas turbine for power generation. The pressures on the feed and permeate sides should be made substantially the same to reduce the need for sealing between the diaphragm faces. The gas turbine inlet pressure will typically range from 5 atm to 40 atm and the discharge pressure will range from 1 atm to 1.5 atm. The steam generator generates steam at a pressure between 3 atm and 80 atm in a Rankine cycle. Oxygen ion conductivity of ion transfer membrane: Typically in the range 0.01 to 100 S / cm (1S = 1 / Ohm) Thickness of Ion Transfer Membrane: The ion transport membrane can be used in the form of a thick membrane or a thin film supported by a porous substrate. The thickness t of the ion transport membrane / layer is less than 5000 µm, preferably less than 1000 µm, most preferably less than 100 µm. shape : The components of the ion transport membrane are usually tubular or planar. If high purity (99.9% or more) of nitrogen to generate a separation step using an ion transfer device will have to be postpurification (Example 2). Oxygen and low purity nitrogen, for example, are produced in the ion transfer stage and late stage purifiers can be used to remove all or most of the remaining oxygen from the low purity nitrogen holding stream from the ion transport stage. The post purifier may be a typical deoxygenation system (eg deoxygenation based on H2), or another ion transfer device, preferably as in Example 2. If the second ion transfer stage is used for later purification, a reactive purge gas such as methane can be used to purge the permeate side of the ion transfer membrane. This reactive purge gas significantly reduces the oxygen partial pressure on the purge side of the ion transfer membrane to enhance oxygen transfer and require much less area of the ion conductive membrane than with non-reactive purge gases. The reactive purge gas provides all or part of the heat introduction necessary to maintain a high operating temperature in the ion transfer stage. Although not preferred, it is also possible to use a product purge system in the second ion transfer stage, whereby a portion of the high purity nitrogen bearing gas stream is circulated to flush the anode side of the ion transfer unit. The ion transfer membrane area required in a product purge system requires a much larger area than that of a reactive purge system. The amount of oxygen separated in the ion transfer device can be easily controlled by changing the feed gas flow pressure, feed air flow rate and / or ion transfer operating temperature if necessary. Pressure-driven ion transport devices are preferred in terms of device simplicity, but the invention described herein is applicable to both systems that use electrically driven or pressure-driven ion transport membranes. In accordance with the embodiment of the present invention shown in FIG. 4, the flow 452 is cooled in the turbine 400 to a temperature of between 1100 and 1400 ° F. and then the power generated by the expansion is dependent upon the power required for the air compressor 402. Almost identical. The result is an independent device that produces oxygen and nitrogen simultaneously. The energy for operating the air compressor 402 can be obtained from the heat generated in the oxygen removal reaction, and can be recovered from the air at a relatively high air compression ratio. Thermal energy runs the system, higher oxygen recovery and lower energy costs than electrical energy. The oxygen containing gas 404 is compressed by the compressor 402. Preferably the compressor 402 is a two to four stage device, in which each turbine and compression stage movable shaft, such as three or four poster centrifuges, draws air in the range of about 100 psia to 250 psia. It has a conventional gear transmission that compresses. Gas flow 404 ′ containing compressed oxygen is divided into a first compressed portion 406 and a second compressed portion 408. The balance of the two portions 406, 408 is due to the adjustment of the first valve 410 and the second valve 412. The first and second valves 410 and 412 are efficient in any device construction to precisely regulate the flow rate of each compressed portion. The valve may be manually set and maintained at a constant flow rate during operation of the device, or alternatively to control the temperature of the flow 418 and the flow 450 and to maintain the temperature at the required level during operation of the device, Integrate into the feed back loop to regulate the valve by means such as Balancing the first compressed portion 406 and the second compressed portion 408 provides a sufficient volume of relatively cold gas for the first heat exchanger 414, that is, the first compressed portion 406. And the integrated heat capacity of the fuel stream 416 is sufficient to cool the oxygen product stream 418. Typically the oxygen product stream 418 is cooled to a temperature of about 150 to 350 degrees Fahrenheit. A late cooler 420 may optionally be included upstream of the first heat exchanger 414 to increase the heat capacity of the first compressed portion 406. Here, ″ upstream ″ refers to the direction that flows back into the gas flow as it is commonly used in the art. The gas flow direction is indicated by the arrow head in the figure. "Downstream" is also intended to indicate a conventional meaning in the art, which means the direction of gas flow airflow. The first compressed portion 406 in the first heat exchanger 414 is heated within a range of about 50 to 200 ° F., which is the operating temperature of the oxygen transfer membrane 422. Depending on the material used for the diaphragm component 424, the operating temperature is typically in the range of about 1450 to 2000 ° F. The diaphragm component 424 has an anode side 428 opposite the cathode side 426. The first compressed portion preheated at the cathode side 426 is preheated while traveling through one or more second heat exchanger 430, third heat exchanger 432 and internal heat exchanger 434. And recombine with the second compressed portion 408. The diaphragm component 424 is divided into two parts, the separation part 436 and the reaction part 438. The two parts may be part of the same diaphragm component as shown in FIG. 4 or alternatively may be composed of two separate diaphragm components as described in FIG. 8 below. Alternatively two diaphragm components can be included in two separate assemblies. 4, the recombined first compressed portion 406 and the second compressed portion 408 abut the cathode 426 of the diaphragm component 424 along the separator 436. A portion of the oxygen contained in the oxygen containing gas (typically greater than 70% by volume) travels through the diaphragm component 424 and is recovered as the oxygen production stream 418. Residual oxygen contained in the integration of the first compressed portion 406 and the second compressed portion 408 moves through the diaphragm component 424 in the reaction portion 438 and generates heat by an oxidation reaction with the fuel 440. Forms mainly CO 2 and H 2 O. The oxygen moved and reacted in the reaction section is adjusted to generate sufficient heat for the following cases. That is, (1) to raise the feed gas to the oxygen transfer membrane temperature, (2) to power in the compression stage, (3) to compensate for the energy loss of the device, and (4) to recover the heat that has not been recovered from the discharge stream. To compensate for heat loss to the surroundings. Typically about 70 to 90% by volume of oxygen contained in the combined first compressed portion 406 and the second compressed portion 408 moves in the separator 436 and substantially all of the remaining oxygen is reacted. It moves within 438. The combustion products produced in the deoxo section 438 are used to sweep the permeate side of the separator 436, thereby lowering the effective partial pressure of oxygen at the separator and increasing oxygen recovery or separating the oxygen transfer diaphragm area. Decreases. The oxygen product stream 418 mainly contains oxygen and the combustion products from the reaction section 438 mainly contain water and carbon dioxide. The oxygen product stream is cooled while transferring heat to the first compressed portion 406 and the fuel stream 416 coming from the first heat exchanger 414. The condenser 442 condenses most of the water from the oxygen product stream 418 and produces a gas water mixture as the condenser exhaust 444, which is saturated with liquid water and water in the separator 446. Gas flow 448, which is comprised of about 80-90% by volume of oxygen and about 10-20% by volume of carbon dioxide. Oxygen effluent 448 is further downstream to remove the selectively contained water vapor and to separate and recover carbon dioxide. The heat of reaction generated in the reaction unit 438 is mainly absorbed by raising the temperature of the second compressed portion in the internal heat exchanger 434. Further heat moves to the cathode side retention flow 450 and the oxygen product stream 418. Preferably the heat exchange rate is high enough to maintain the temperature of the diaphragm component 424 in the range of 1450 to 2000 ° F. Solutions to the temperature control problem of diaphragm components in oxygen transfer membrane reactors are shown in US Pat. Nos. 5,820,654 and 5,820,655. Cathode side retentate 450 is the oxygen-depleted gas, mainly nitrogen. This is sufficiently cooled in the third heat exchanger 432, allowing 17-4 Ph of stainless steel or similar standard material to be used in the turbine 400, while expanding a portion (60-80%) of the flow 450. Is sufficient temperature to operate the air compressor 402. The anode surface retention flow is preferably cooled to a temperature of 1100 ° F. to 1400 ° F. most preferably to a temperature of about 1300 ° F. Cathode side retentate 450 is divided into a first oxygen removal portion 452 and a second oxygen removal portion 454. Dividing the flow 450 into the flow 452 and the flow 454 is controlled by the control valve 456 to match the generated turbine power and the consumed compressor power. The third valve 456 may be manually pre-adjusted or may include a feed back loop and continuously adjust according to the emissions imposed on the turbine 400. Oxygen-depleted first portion 452 is cooled in second heat exchanger 430 and heat moves to second compressed portion 408. The cooler 458 is further cooled by an after cooler 458, which produces a compressed nitrogen stream 460. Nitrogen is typically about 5 to 30 psi lower pressure of the compressor 402 discharge pressure. The deoxygenated second portion 454 is expanded in the turbine 400 to produce as much work as is needed to operate the air compressor 402. Turbine discharge 462 has significant heat which is recovered in fourth heat exchanger 464. The cooled turbine discharge is recovered to the low pressure nitrogen gas stream 466. Typically low pressure nitrogen gas stream 466 is released at atmospheric pressure. Optionally, heat recovered from turbine exhaust stream 462 is used to generate steam 470 in boiler 464. The water vapor, typically at a low to medium pressure (15 to 65 psia), is an additional sweep gas that mixes with the fuel 440 and purges the permeate surfaces of the reaction section 438 and separator 436. Used. Water recovered from separator 446 is pumped to fourth heat exchanger 464 by pump 468 and converted to water vapor 470. The amount of steam 470 generated generally depends on the heat in the exhaust stream 462. Optionally additional steam can be produced in the second boiler, which is heated by the reaction of fuel and oxygen from an atmospheric air supply. Further, adding water vapor to the anode side 428 of the oxygen transfer film 422 reduces the oxygen partial pressure on the cathode side, thereby increasing the oxygen transfer driving force from the anode side 426 to the cathode side 428. Let's do it. In practical applications purge steam, consisting of a mixture of combustion product gas and water vapor at the anode side (428), yields an average ratio of oxygen partial pressures between the cathode and anode surfaces at separator 436. When maintained at, it enables recovery of about 84% of oxygen at a negative pressure of 115 psia from mixing the first compressed portion 406 and the second compressed portion 408. Standard turbine / compressor units are shown in Table 5. Turbine 400 operates a conventional transmission gear 472 by expanding the second portion 454 from which oxygen has been removed. Conventional transmission gears operate in three compression stages, C1, C2 and C3, which continuously compress the oxygen containing gas 404 to produce a compressed oxygen containing gas 404 '. An optional motor 474 is connected to a conventional transmission gear 472 to provide power in the system start mode and also provide additional power if necessary. Although not shown in the figure, an intermediate cooler may be included between each stage to increase efficiency. 6 is a configuration diagram showing in more detail the invention shown in FIG. 6, the compressed oxygen-containing gas 404 'is a multibed pressure swing adsorption consisting of an adsorption bed formed from a layer of activated alumina and zeolite molecular sieve pellets or beads. prepurifier 476 to remove air contaminants in water, carbon dioxide, heavy hydrocarbons and other gases. If prepurifier 476 is included in the flow, an aftercooler is included between compressor 404 and prepurifier 476 to increase the capacity of adsorbent in prepurifier 476. The compressed oxygen-containing gas 404 'is sufficiently cooled to allow the post cooler 420 to be omitted. When the adsorption prepurifier 476 is used, some or all of the turbine discharge 462 is sent 478 to the adsorbent prepurifier for regeneration of the adsorbent beads of the adsorbent prepurifier. The volume of turbine discharge 462 that may be transferred 478 to the adsorbent prepurifier 476 is equal to 60% of the volume of gas 404 containing incoming oxygen. This coincides with the correct ratio of (volume of turbine emissions) / (volume of air) = 4.3 and is suitable for manipulating the adsorption bed of a single pressure swing cycle. 7 illustrates a cross-sectional view of a reactor 500 useful for producing oxygen and nitrogen in accordance with embodiments of the present invention. Many features of the reactor 500 are described in US Pat. Nos. 5,820,654 and 5,820,655 and are incorporated by reference. Inlet 504 receives and transports a first compressed portion 406 of oxygen-containing gas, typically air. Inlet 502 receives and transports a second compressed portion 408 of the oxygenous gas. Fuel 440 and optionally water vapor are introduced into feed tube 506. The reactor consists of a preheating unit 529, a reaction unit 438, a separation unit 436 and a cooling unit 535. Encircling at least a portion of the feed tube 506 is the tubular diaphragm component 424. Preferably, the diaphragm component 424 is composed of a porous substrate or a metallic substrate capable of supporting a thin coating. Coating of reaction section 438 and separator 436 may be any material effective for selective transfer of oxygen. Most preferred for the reaction section is a perovskite coating containing chromium, for example one of the materials listed in line 9 of Table 1. In addition, in the case of the separation unit, a coating made of a mixed conductor having a high conductivity such as item 1 in Table 1 above is preferable. An impermeable coating 508, such as nickel, preferably coats a portion of the diaphragm component 424 adjacent to the open end of the cooling section 535, so that oxygen transfer can occur through the separation section 436 and the reaction section ( 438) only. A transition porous layer is required between the porous support and the coating to overcome the chemical and mechanical compatibility issues between the coating and the substrate. The outer diameter of the feed pipe 506 and the inner diameter of the diaphragm component 424 are defined by the first annular 510. A gas impermeable shroud tube surrounds a portion of the diaphragm component 424. The outer diameter of the diaphragm component 424 and the inner diameter of the cover tube 512 are defined as the second annular 514. Dummy tube 516 expands within the confinement tube 512 with the portion removed from membrane component 424. The outer diameter of the dummy tube 516 and the inner diameter of the cover tube 512 are defined as a third annular 518. The annulus of each of the first 510, the second 514, and the third 518 is sized to improve heat transfer convection. In general, each annulus has a width less than about 1/8 inch. The plurality of baffles improves heat transfer to the shell side. In Figure 7, the partitions are evenly spaced, but typically the spacing of the partitions is closer to the inlet 502 than the inlet 504. This is because the volume of the second compressed portion 408 is larger and slightly warmer than the first compressed portion 406. The portion of the reaction wall 438 has a larger cooler end, a smaller hot end, and a smaller portion of the temperature difference between the diaphragm and the shell side gas, keeping the total heat transfer coefficient low. The small part keeps the total heat transfer coefficient high. An insulating sleeve 537 having a thickness of about 1/32 to 1/8 inch near the inlet of the reaction section is added to the outside of the lid tube to prevent the diaphragm temperature from falling below the operating temperature. The reactor 500 has a metallic shell 522 and an insulating layer 524 formed on the inner surface of the metallic shell. When the reactor is operated, the second compressed portion 408 is introduced through the inlet 502 around the interior of the metallic shell 522. While traveling upstream of the preheat diaphragm 520, the second compressed partial gas stream recovers heat from the heated nitrogen holding flow 465 contained in the third annulus. While flowing through the shell surface of the reaction section 438, a second portion compressed gas stream absorbs most of the heat generated by the reaction of the annular 428 oxygen-fuel and at its temperature throughout the process. Rises near the diaphragm operating temperature. Prior to introduction into the second annular 514, the first compressed portion recombines with the second compressed portion. The first compressed portion 406 is introduced into the nozzle 504 and heated in the cooling unit 532 to rise near the diaphragm adjustment temperature. The recombined hot oxygen-containing stream 528 is introduced into the annulus 514, with the majority of the oxygen-containing gas at the cathode side 426 of the diaphragm component 424 by ion transfer in the separator 531. It moves to the anode side 428. After going up the separation part, it is introduced into the reaction part 438, where most of the remaining oxygen contained in the flow moves to the anode to exothermic reaction in the fuel 440 and the reaction part 438. Since the permeate flow is a holding flow and countercurrent, the residual combustion product is efficient as a purge gas for the anode side of the diaphragm component 424 in the separator 436, thus enhancing the transport of oxygen. The exiting oxygen product stream 418 consists primarily of oxygen, water and carbon dioxide, cooled by an incoming first compressed portion 406 and exits reactor 500 through outlet 530. . Nitrogen-rich cathode side retentate 450 exits outlet 534 as nitrogen product 532. Heat transfer in reactor 500 is combined with insulating layer 524 to ensure that all structural components, such as tube sheets and shells, must conform to the use of universally engineered materials such as stainless steel and carbon steel at moderate temperatures. And also facilitates the manufacture of tubes in tube thin film joints. Each tube has an uncontrolled, free-floating end that avoids stress due to expansion and contraction of thermal and component differences. 8 is a cross-sectional view illustrating an alternative reactor 550. Reactor 550 has two separate diaphragm components, that is, separation 436 and reaction 438. The shape of the reactor allows cocurrent flow of the holding and permeate surfaces in the reaction section 438, but reserves the countercurrent flow between the holding and permeate surfaces in the separator to make full use of the permeate purge. The cocurrent flow of the reaction section is advantageous in that it generates lower component stresses in the diaphragm component. Reactor 550 has a hollow metal shell that is a sealed enclosure. The first tube thin film 536 and the second tube thin film 538 are arranged spaced apart at regular intervals in a sealed enclosure. The first reaction tube including the reaction portion 438 has an inner (anode) surface 428 'and an outer (anode) surface 426'. An open first end 540 of the first reaction tube is fixed to the first tube thin film 536, and a second closed end 542 extends at a constant distance. Typically only a portion of the first reaction tube is efficient for the oxygen selective ion transport membrane. The tube ends are covered with an impervious barrier layer because the first function of this section is to transfer heat. The second reaction tube including the separator 436 has an inner (anode) surface 428 and an outer (anode) surface 426. The first open end 544 of the second reaction tube is fixed to the second tube thin film 538, and the second closed end 546 extends at a constant distance. As with the first reaction tube, typically only a portion of the second reaction tube is efficient for the oxygen selective ion transport membrane. A shroud tube 512 surrounds a portion of the first and second reaction tubes, including at least part of both the oxygen selective ion transport membrane. The combination of the inner surface of the tube and the outer surface of the oxygen selective ion transport membrane is defined as an annulus 514 to cover. The plurality of oxygen-containing gas inlets 502 and 504 carries the oxygen-containing feed gas into the annular 514. The third tube thin film 550 is arranged between the first tube thin film 536 and the second tube thin film 538. In order to cover, the tube extends through the separator and the reaction and thus places two sections in succession on the holding surface. Flowing in an annular between the outer diameter of the inner feed tube and the inner diameter of the diaphragm tube is defined as the anode and can be in any direction. Thus, this configuration allows for free choice of retention of the reaction section and flow of the permeate side, allowing either cocurrent or countercurrent. As in the reactor 500, the reactor 550 includes a preheating part and a cooling part as well as a reaction part and a separation part. The gas stream 408 is partially warmed by the exiting nitrogen product first through the baffled preheated section and then absorbs and retains the heat of reaction while flowing through the baffled shell side of the reaction section. Joins the stream 406 warmed up by the exiting gas stream 418 prior to introduction into the flow annulus 514. The fuel gas inlet 548 transports the fuel gas 440 through the feed tube 506 to the inner surface 428 ′ of the reaction portion 438. The feed gas is introduced into the reaction section located near the closed end 542 and flows in co-current with the oxygen containing gas in the annulus 510. The outlet is used to remove the oxygen product gas 418 and the nitrogen product gas 460 as well as the combustion product 533. Combustion product 533 may be used to purge separator 436 by introduction through purge tube 552. The purge tube 552 extends to the separator so that combustion products are introduced close to the closure 546 and the flow flows countercurrently to the oxygen containing gas in the annulus 510. In operating the reactor 550, a first compressed portion 406 of the oxygen containing gas, in particular air, is introduced into the reactor shell and discharged while it is discharged while flowing across the partition 520. Warmed by The second compressed portion 408 is heated by the nitrogen product discharged from the preheater and then absorbs the heat of reaction in the reaction zone and heats up to join the first compressed portion 406. . As the hot joined stream 528 traverses the cathode side 426 of the separator 436, some of the oxygen is moved to the anode side 428 and recovered to the oxygen product stream 418. do. A purge gas 533 is introduced through the purge tube 534 to reduce the oxygen partial pressure at the anode side 428 and thus increase oxygen transport through the separator 436 of the diaphragm component. One suitable purge gas is the combustion product from reaction section 438. Cathode side retentate 450 flows along the cathode side 426 ′ of the diaphragm component of the reaction section 438 and the remaining oxygen flows to the anode side to react with the fuel 440. 428 '). Nitrogen product gas 460 is recovered from the reactor shell, and combustion products 533 are discharged or sent to purge inlet 534. 5 and 6 show only one diaphragm tube device for clarity. It will be apparent to those skilled in the art that this is a sample of multiple devices. In this embodiment, a higher air supply pressure than shown in the examples increases the work potential of the nitrogen holding flow while allowing for reduction in turbine flow and increases the nitrogen recovery at higher pressures. . The heat used to increase the purge flow will be reduced. However, since the pressure of the cathode is higher, the efficiency and separation area of oxygen recovery will be smaller. Increasing the turbine inlet temperature will increase the work potential of the turbine, especially at higher cathode side pressures, which requires the use of heat-resistant materials to manufacture the turbine. Although embodiments of the present invention include an external steam purge, the present invention is equally useful in systems without an external steam purge. Without an external steam purge, lower oxygen recovery and / or more separation area would be required. Example 3 The following example uses the flow of FIG. 4 and the reactor design of FIG. 5 and the values are as follows. Air flow: 1130 MNCFH 85% three-stage air compression insulation efficiency at 115 psia Air flow to reactor separator and coolant: 225 MNCFH at 120 ℉ 905 MNCFH at 400 ℉ Maximum Oxygen Transfer Membrane (OTM) Operating Temperature: 1760 ℉ Average OTM Separation Driving Force: log (PO cathode / PO anode ) = 0.3 Nitrogen flow out separator, reactor, cooler: 1300 ℉ Turbine Flow: Nitrogen 680 NCFH (1300 ℉) Turbine Efficiency: 85% Increased Fuzzy Vapor: 4.21 lbs / hr Fuel: Natural gas with a lower heating value of 900 BTU / NCFH Fuel Ingredient: 18900 NCFH Product flow: 200 MNCFH O 2 (with 91.4% O 2 , 8.6% CO 2 ) 15 psia 212 MNCFH N 2 (O 2 〈10 ppm) 100 psia Oxygen recovery: 84.3% of full theoretical amount KW-nitrogen product compression required for air compression: 10.03 / MNCFH O 2 Air Compression Costs-Separation 2 $ / MNCFH Natural Gas: 0.156 $ / 1000 NCFH O 2 In the above example, energy recovery from the hot stream is limited to large cold end temperature gradients and low heat exchange costs. The increase in heat recovery lowers gas consumption by 10%. Nevertheless, the energy and nitrogen costs of the separation are comparable to cryogenic and non-cryogenic processes, which typically consume about 8 KW / 1000 NCFH O 2 for separation at 0.035 $ / KW HR or 0.280 $ / 1000 MNCFH O 2 . low. Embodiments of the present invention are shown in one or more drawings for convenience, and each form may be combined with other forms according to the present invention. In addition, various modifications of the invention described herein may be clearly recognized by those skilled in the art from the foregoing description, and such modifications are construed as being included in the claims of the present invention. Technical problem to be invented It is an object of the present invention to efficiently recover oxygen from an air supply flow that is part of a power cycle process. Another object of the present invention is the use of an ion transfer device purged with water vapor allows for the creation of crude-nitrogen flow as a retentate from which residual oxygen is removed in a reactively purged ion transfer separator to simultaneously purify high purity nitrogen. To make it possible to produce a product flow. It is another object of the present invention to provide a steam purge stream at moderately elevated pressures after expansion in a steam turbine and to condense the water, thereby enabling the recovery of oxygen at elevated intermediate pressures using the process without the need for an oxygen compressor. To do that. Another object of the present invention is to maximize power production in the Rankine cycle and to improve energy utilization by including one or more high pressure steam expansion stages upstream of the ion transfer separator purge inlet. Another object of the present invention is to simplify the system by expanding the holding flow in the turbine to generate sufficient power to operate the supply air compressor while producing nitrogen, which is a simultaneous product at elevated pressure. Another object of the present invention is to enable efficient recovery of product oxygen and high pressure nitrogen by a thermally driven free standing air separation plant. Another object of the present invention is that the turbine feed is low enough to allow the use of less expensive engineering materials such as stainless steel prior to the expansion process but high enough to hold suitable work with the potential to run the air compressor. By cooling to a degree of temperature, it is possible to use only low cost turbines to recover only part of the retention flow with nitrogen. Another object of the present invention is to enable the use of small, low cost turbomachinery by integrating a turbine and a multistage air compressor in a single assembly. It is a further object of the present invention to enable the production of high purity nitrogen using pressure and, optionally, a temperature swing adsorptive clarifier, which is regenerated by removing carbon dioxide, water and other impurities from the feed air by the turbine exhaust.
权利要求:
Claims (20) [1" claim-type="Currently amended] (a) compressing the feed gas stream; (b) heat the feed gas stream; (c) separating the heated feed gas flow into an oxygen-depleted gas stream on the retention surface and an oxygen gas flow on the permeate surface using at least one first ion transfer device having an ion transport membrane having a retention surface and a permeate surface. Purging the permeate side of the ion transport membrane using a high pressure purge gas stream containing water vapor to generate a high pressure gas stream containing oxygen and water vapor; And (d) send a high pressure gas stream containing oxygen and water vapor to the first turbine to recover power and produce an expanded low pressure gas stream containing oxygen and water vapor, the low pressure gas stream containing oxygen and water vapor being oxygen Separated into gas stream and water stream or steam stream; A method for generating a high pressure gas flow comprising oxygen and water vapor and a gas stream from which oxygen is removed from a feed gas stream containing oxygen, characterized in that it comprises a step. [2" claim-type="Currently amended] The method of claim 1 wherein the high pressure purge gas stream containing water vapor passes through the second turbine before passing through the permeate side of the ion transport membrane. [3" claim-type="Currently amended] 3. The method of claim 2, further comprising heating the high pressure purge gas flow sufficiently to avoid condensation during expansion in the second turbine. [4" claim-type="Currently amended] The apparatus of claim 1, further comprising purifying nitrogen to direct a gas flow from which oxygen is removed from the ion transfer membrane to a reactively purged ion transfer device to produce a simultaneous product. Reaction in which provides the heat necessary for operation of the first device. [5" claim-type="Currently amended] (a) compressing the feed gas stream; (b) heat the feed gas stream; (c) separating the heated feed gas flow into an oxygen-depleted gas stream on the retention surface and an oxygen gas flow on the permeate surface using at least one first ion transfer device having an ion transport membrane having a retention surface and a permeate surface. Purging the permeate side of the ion transport membrane using a high pressure purge gas stream containing water vapor to generate a high pressure gas stream containing oxygen and water vapor; (d) sending a high pressure gas stream containing oxygen and water vapor to the first turbine to recover power and to produce an expanded low pressure gas stream containing oxygen and water vapor; (e) separating the low pressure gas stream containing oxygen and water vapor into an oxygen gas stream and a water stream or a steam stream; And (f) passing the high pressure purge gas stream containing water vapor through a second turbine before purging the permeate side of the ion transport membrane; A method for generating a high pressure gas flow comprising oxygen and water vapor and a gas stream from which oxygen is removed from a feed gas stream containing oxygen, characterized in that it comprises a step. [6" claim-type="Currently amended] The low pressure gas flow of claim 5, wherein the high pressure purge gas flow further comprises heating sufficiently to avoid condensation during expansion in the second turbine, wherein the heating step expands the expanded low pressure gas flow before expanding by the second turbine. Significant heat transfer from the high pressure purge gas stream to the feed gas is air, and further comprising the step of concurrently producing nitrogen from the degassed gas stream. [7" claim-type="Currently amended] (a) compressing the feed gas stream in a compressor; (b) placing the feed gas at an initial temperature such that the retention flow containing nitrogen-rich product gas is useful for increasing the pressure-driven migration of oxygen from the anode side to the cathode side of the oxygen selective ion transport membrane remaining on the anode side. Contacting the compressed feed gas stream with a cathode side of an oxygen selective ion transport membrane; (c) dividing the retention flow into a first oxygen removal portion at a first flow rate and a second oxygen removal portion at a second flow rate; (d) recovering the high pressure nitrogen-rich product gas from the first oxygen removal portion; (e) expanding the second oxygen removal portion in the turbine, thereby creating a combination of work and low pressure nitrogen rich product gas with the turbine exhaust, wherein the first flow rate in the separation step is determined by the turbine Make it possible to provide sufficient work to operate; And (f) recovering the oxygen generating gas from the permeate flow at the anode side of the oxygen selective ion transport membrane, wherein the feed gas sequentially contacts the first separation section and the reaction section of the oxygen selective ion transport membrane. In addition, most of the oxygen contained in the feed gas moves through the separation unit and substantially residual oxygen moves through the reaction unit; A process for producing oxygen and nitrogen at a low energy cost from a feed gas containing a mixture of oxygen and nitrogen, characterized in that it comprises a step. [8" claim-type="Currently amended] The method of claim 7, wherein the fuel is combusted with oxygen delivered from the reaction unit to generate a mixture of carbon dioxide and water vapor and heat energy, wherein the heat energy raises the supply gas to the operating temperature of the oxygen transfer membrane, and (ii) Pure heat energy and substantial energy needed to perform the compression step, (i) to overcome energy losses in the device, and (i) to compensate for external heat loss and unrecovered heat from the discharged gas stream. Method for producing oxygen and nitrogen at low energy costs, characterized in that the same. [9" claim-type="Currently amended] 9. The separator according to claim 8, wherein the cathode face of the separator and the reaction part are arranged in series and sweep the cathode face of the separator in the direction of feed flow and countercurrent with combustion products from the reaction part, thereby producing carbon dioxide, water vapor and A process for producing oxygen and nitrogen at low energy costs, characterized by producing a separator cathode gas stream consisting predominantly of oxygen. [10" claim-type="Currently amended] 10. The method of claim 9, wherein the feed gas comprises a first compressed portion and a second compressed portion that absorbs reaction heat at the separator side gas phase where the fuel cools and the reactant cathode side. Part into two compressed sections, thereby keeping the oxygen-selective ion transport membrane below 2000 ° F. and further extending the holding gas stream exiting the cathode side of the reactor section before expanding in the turbine. A process for producing oxygen and nitrogen at low energy costs, characterized by cooling to an intermediate temperature between 1100 and 1400 ° F. [11" claim-type="Currently amended] 11. The turbine of claim 10 wherein the turbine operates an air compressor of three or more stages, wherein the turbine and the air compressor have a shaft equipped with a shaft of three air compression stages and a conventional gear transmission. A method for producing oxygen and nitrogen at low energy costs, characterized by forming four poster arrangements. [12" claim-type="Currently amended] 10. The method of claim 9, wherein the separator and the reactor are combined in one unit. [13" claim-type="Currently amended] 8. The method of claim 7, wherein the gas flow on the cathode surface in the reaction portion is co-current with the gas flow on the anode surface. [14" claim-type="Currently amended] 9. The method of claim 8, wherein the thermal energy recovered from the discharge stream of the turbine is used to produce water vapor, and the water vapor is used to purge at least one of the separator and the cathode surfaces of the reaction part. How to produce nitrogen at low energy costs. [15" claim-type="Currently amended] 15. The method of claim 14 wherein the fuel is mixed with the water vapor and used to purge the cathode side of the reaction section. [16" claim-type="Currently amended] 15. The method of claim 14, wherein at least a portion of the turbine exhaust is used to regenerate a bed of an adsorption prepurifier that removes water, carbon dioxide, heavy hydrocarbons, and other gaseous air impurities from a feed gas downstream from the air compressor. To produce oxygen and nitrogen at low energy costs. [17" claim-type="Currently amended] (a) a sealed hollow enclosure; (b) a first tube membrane positioned in the enclosed enclosure; (c) a second tube membrane positioned at a predetermined distance from the first tube membrane in the hermetic enclosure; (d) an inner surface, an outer surface, a first open end fixed to the first tube membrane, and a second closed end extending at the gaps, wherein the first end part is partially Located between the first end and the second end, the first oxygen selective ion transfer membrane having the inner surface constituting the first cathode surface and the outer surface constituting the first anode surface A first reaction tube; (e) an inner surface, an outer surface, a first open end fixed to the second tube thin film, and a second closed end extending at the gaps, wherein the first end part is partially a second oxygen selective ion located between the first end and the second end, the second oxygen selective ion having an inner surface constituting a second cathode surface and an outer surface constituting a second cathode side A second reaction tube serving as a transfer membrane; (f) a shroud tube circumscribing at least a portion of both the first oxygen selective ion transport membrane and the second oxygen selective ion transport membrane; Wherein the inner surface of the cover tube and the outer surfaces of both the first oxygen selective ion transport membrane and the second oxygen selective ion transport membrane are defined as annulus. (g) a plurality of oxygen containing gas inlets for conveying an oxygen containing gas in the annular shape; (h) a fuel gas inlet for conveying fuel gas to an inner surface of said first oxygen selective ion transport membrane; (i) a plurality of outlets for removing product gas and reaction byproduct gas from the enclosure; Reactor consisting of. [18" claim-type="Currently amended] 18. The method of claim 17, wherein a third tube thin film is positioned between the first tube film and the second tube thin film, and the plurality of gas inlets containing oxygen are between the second tube thin film and the third tube thin film. Wherein a fuel tube extends into the first oxygen selective ion transport membrane, the fuel is introduced through the fuel tube proximate to the closed end and then flows cocurrently with the oxygenous gas in the annulus, The oxygen in the oxygen-containing gas in the annulus moves from the first cathode side to the first anode side and is burned by the fuel to form a combustion product. [19" claim-type="Currently amended] 19. The system of claim 18, wherein the purge tube extends to the second oxygen selective ion transport membrane and the combustion product is introduced through the purge tube proximate to the closed end, the oxygen in the annulus. A reactor characterized by flowing in a countercurrent with the containing gas. [20" claim-type="Currently amended] 8. The ion conductivity membrane of claim 7, wherein the ion transport membrane tube constitutes a heat transfer tube and is made of a material having high stability even at low oxygen partial pressures in the reaction area. Wherein said porous substrate in said ion transfer membrane and heat transfer area supports an impermeable hermetic coating.
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同族专利:
公开号 | 公开日 AU743693B2|2002-01-31| CN1279627A|2001-01-10| JP2001523546A|2001-11-27| WO1999025459A1|1999-05-27| EP1062023A1|2000-12-27| BR9814667A|2000-10-03| US5954859A|1999-09-21| AU1406799A|1999-06-07| CA2310377A1|1999-05-27| ID24912A|2000-08-31| MXPA00004841A|2004-03-10| US6139604A|2000-10-31|
引用文献:
公开号 | 申请日 | 公开日 | 申请人 | 专利标题
法律状态:
1997-11-18|Priority to US8/972,020 1997-11-18|Priority to US08/972,020 1998-11-13|Application filed by 조안 엠. 젤사 ; 로버트 지. 호헨스타인 ; 도로시 엠. 보어, 프랙스에어 테크놀로지, 인코포레이티드 1998-11-13|Priority to PCT/US1998/024248 2001-04-16|Publication of KR20010032208A
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申请号 | 申请日 | 专利标题 US8/972,020|1997-11-18| US08/972,020|US5954859A|1997-11-18|1997-11-18|Solid electrolyte ionic conductor oxygen production with power generation| PCT/US1998/024248|WO1999025459A1|1997-11-18|1998-11-13|Thermally powered oxygen/nitrogen plant incorporating an oxygen selective ion transport membrane| 相关专利
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