Integrated electrochemical cell power generation and electrolysis system

Abstract

The electrochemical cell system (51) and electrochemical cell process are described as applicable in either power generation mode or electrolysis mode with the system including any or all of the following: a containment vessel interior space, a multiple electrochemical cell stack stack inlet plenum (43) that can accommodate thermal expansion and contraction in an economical manner and provide a substantially equivalent environment for each stack inlet; a vessel exterior compression stack mount, which may be configured as a cathode outlet manifold (111) configured as a stack mount, if desired; a fully contained thermal expansion-contraction electrochemical cell stack mount, which may be configured with an external spring (91); and an axial flow adjustment device, such as a beveled plate (99) for better operation.

Description

[Technical field]

[0001] [Government License Rights] This invention was made with Government support under ARPA-E INTEGRATE Contract DE-AR0000956 awarded by the Department of Energy. The Government has certain rights in this invention.

[0002] CROSS-REFERENCE TO RELATED APPLICATIONS This application is a PCT international patent application claiming priority to and the benefit of U.S. Provisional Application No. 63 / 297,525, filed January 7, 2022, which patent application and any priority cases are incorporated herein by reference in their entireties.

[0003] The inventive technology described herein generally relates to the field of electrochemical cell processes and integrated solid oxide fuel cell (SOFC) stacks (or other types of fuel cells) with gas turbine (GT) systems for high-efficiency power generation, and solid oxide electrolysis cells (SOEC) (or other types of electrolyzers) for gas or hydrogen production. This specification serves as a disclosure of several embodiments developed by the present inventors relating to integrated solid oxide fuel cell (SOFC) stacks (or other types of fuel cells) and gas turbine (GT) systems intended for various purposes, including high-efficiency power generation and electrolysis. Furthermore, while some embodiments relate to integrated SOFC / GT systems, other embodiments may be used separately with standalone pressurized or unpressurized SOFC, SOEC, or other types of fuel cell systems. Furthermore, some embodiments may be used as part of an SOEC electrolysis system for gas or hydrogen production. The present technology also relates to systems and methods for integrating a solid oxide fuel cell (SOFC) stack (or other type of fuel cell) and a gas turbine (GT) system for high efficiency power generation, either used separately as a standalone SOFC (or other type of fuel cell) system or integrated into a SOFC / GT system. [Background technology]

[0004] Solid oxide fuel cells are advanced high temperature (between 500-1000°C, but not limited to) electrochemical devices that can efficiently convert fuel (mainly hydrogen) into electricity. Although relatively efficient, there is still room for system and efficiency improvement due to the high operating temperature of SOFCs, the need for constant hot air to supply oxygen to the electrochemical reaction, and the fact that not all fuel supplied to the SOFC is consumed. System efficiency can be increased by utilizing both waste heat and unconsumed fuel and incorporating a gas turbine into the system. Additionally, although SOFCs ultimately consume hydrogen in the electrochemical reaction, the high operating temperature of the system also allows fuels such as natural gas to be reformed and converted into hydrogen, which can then be consumed within the SOFC stack. Solid oxide electrolysis cells (SOECs) are closely related to SOFCs, and effectively reverse the process of converting steam and electricity into hydrogen (which can be used as fuel) and oxygen. They may also generate electrical power. Many of the embodiments disclosed herein are applicable to SOECs as well as SOFCs. In this document, SOFC is often used as a general term that should be understood to encompass both SOFCs and SOECs. Summary of the Invention

[0005] In general, the present technology includes both apparatus and methods in various embodiments for realizing efficient and robust integrated solid oxide fuel cell (SOFC) stacks (or other types of fuel cells) and gas turbine (GT) systems for high efficiency power generation, and for realizing integrated solid oxide electrolysis cell (SOEC) systems for producing gas, fuel, and possibly oxygen and hydrogen. The present invention can be applied to various types of electrochemical cells and processes. For example, technology applicable to planar solid oxide fuel cell stacks and solid oxide electrolysis stacks, as well as stacks operating at high temperatures (perhaps 600-900°C), is disclosed. These stacks may consist of a number of ceramic planar components (oxygen ion conducting ceramic electrolyte plates) with electrodes on opposing faces. These planar solid oxide cells are typically stacked and sealed with metal interconnects, current collectors, and shims to define gas flow paths such that two different gases can flow on opposing faces of the planar cells to allow electrochemical reactions to occur. In embodiments, various types of solid oxide electrochemical systems and cells can be used within the general concept of both a power generation system, such as a solid oxide fuel cell, or an electrolysis system, such as a solid oxide electrolysis cell. Each type will be described in detail below.

[0006] While building a highly efficient power generation system by integrating SOFCs with GTs is one goal, the disclosed method and system architecture goes beyond that goal and is applicable in many other contexts. The inventor team's objective was, first, to develop a system design that maximizes system efficiency while ultimately producing the system at an economically viable price point, and, second, to minimize complexity and maximize robustness. Furthermore, this technology has now been expanded to include solid oxide electrolyzers or electrolysis cells (SOECs), which may be closely related to SOFCs and effectively reverse the process of converting steam and electricity into hydrogen (which can be used as a fuel) and oxygen. Many of the embodiments disclosed herein are applicable to SOECs as well as SOFCs, and therefore SOFCs are often used herein as a generic term to encompass both SOFCs and SOECs. [Brief description of the drawings]

[0007] [Figure 1] FIG. 1 is an exemplary embodiment of a base system overview. [Diagram 2] FIG. 2 is an exemplary embodiment of a system overview showing power supply. [Diagram 3] FIG. 3 is an exemplary embodiment of a system overview showing start-up and shutdown components. [Figure 4] FIG. 4 is an exemplary embodiment of a solid oxide fuel cell assembly and pressure vessel. [Diagram 5] FIG. 5 is another exemplary embodiment of a solid oxide fuel cell assembly and pressure vessel. [Figure 6] FIG. 6 is an exemplary embodiment of a solid oxide fuel cell flow channel. [Figure 7] FIG. 7 is an exemplary embodiment of a solid oxide fuel cell stack shelf. [Figure 8] FIG. 8 is an illustration of conventional cathode flow and stack temperature distribution. [Figure 9]FIG. 9 is a simplified illustration of cathode flow and stack temperature distribution according to one embodiment of the present technology. [Figure 10] FIG. 10 is an illustration of a graded flow distribution in accordance with one embodiment of the present technology. [Figure 11] FIG. 11 is an exemplary embodiment of an axial flow conditioner in accordance with one embodiment of the present technology. [Figure 12] FIG. 12 is an exemplary embodiment of a SOEC system overview. [Figure 13] FIG. 13 is an exemplary illustration of a stack compression mechanism. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0008] It should be understood that the embodiments include various aspects, which can be combined in different ways. The following description is provided to enumerate elements and describe some of the embodiments of the present application. It should be understood that these elements, although enumerated with the initial embodiment, can be combined in any manner and in any number to create additional embodiments. The various described examples and preferred embodiments should not be construed to limit the embodiments of the present application to only the explicitly described systems, techniques, and applications. The specific embodiment or embodiments shown are merely illustrative. This specification should be understood and intended to support each embodiment as well as broad claims, even claims from which other embodiments may be excluded. Importantly, the disclosure of merely exemplary embodiments is not intended to limit the breadth of other more comprehensive claims that may be made when such an embodiment is merely one of several ways or embodiments that may be employed in the broader claims, etc. Moreover, the specification should be understood to support and encompass the descriptions and claims of all various embodiments, systems, techniques, methods, apparatus, and applications in any number of the disclosed elements, each element alone, and in any and all various permutations and combinations of all elements in this application or any subsequent application.

[0009] In general, electrochemical cell systems can be understood at their most basic as having electrodes of a first function and electrodes of a second function. One type of electrode can be considered to have a first function and another type of electrode to have a second function. For example, from a fluid and chemical perspective, one type of electrode cell collection is referred to herein as an oxygen cell collection, which has the function of performing an operation or function involving oxygen, and another type of electrode cell collection is referred to as a fuel cell collection, which has the function of performing an operation or function involving fuel. In such a type of first and second function, either the oxygen type or the fuel type can be considered to be the first function, since the cells can operate in the reverse order. Furthermore, the oxygen can serve to promote a fuel oxidation type event, and the fuel can be any suitably compatible material, likely a hydrogen or carbon containing material, and often both, such as a hydrocarbon containing material. Similarly, from an electrical perspective, the first and second functions can be those of a cathode and an anode, again, either one can be configured as the first function electrode type and the other as the second function electrode type. As is well known, electrodes may be layered or configured in a stack that may consist of a plurality of first function electrode elements and a plurality of second function electrode elements. As is well known, such electrode stacks in such types of cell stacks have inlets and outlets for each of the two types of electrodes. Thus, the stack may include a stack first function electrode inlet, such as for the first function electrode stack, a stack first function electrode outlet, such as for the first function electrode stack, a stack second function electrode inlet, such as for the second function electrode stack, and a stack second function electrode outlet, such as for the second function electrode stack. These types of inlets can be seen in FIG. 6, where the first function electrode elements are configured as cathode elements of the oxygen stack, and thus the first function electrode inlet is shown as the area at the start of the arrow as the cathode inlet (121) and the corresponding first function electrode outlet is shown as the area at the end of the arrow as the cathode outlet that flows into the outlet plenum (221).Similarly, the second functional electrode element, perhaps configured as the anode element of the fuel stack, may have a second functional electrode inlet and a corresponding second functional electrode outlet, as can be seen in Figure 13. These inlets and outlets are manifolded as will be described below.

[0010] One embodiment of a basic system schematic of a solid oxide fuel cell (SOFC) and gas turbine (GT) system is shown in FIG. 1, using a solid oxide fuel cell (SOFC) as the initial design. The system (51) is composed of several components, including a SOFC stack (7). These can be optionally composed of individual electrochemical cells (52) fluidly connected in series to form a stack (53), which can then be electrically connected via interconnects (34) in series and / or parallel to generate a portion of the system's power. An important aspect of SOFCs is that the electrochemical reaction is substantially exothermic. Whatever portion of the energy of the fuel consumed in the stack that is not converted to electricity can be converted to heat, which is released into the stack and carried away mainly by the anode and cathode streams. The SOFC stack can be integrated into the gas turbine flowpath (35) to maximize the thermodynamic efficiency of the system and to allow the stack (53) to operate under pressurized conditions in the pressurized region (36) to improve the electrochemical efficiency. In some embodiments, there may be other optimization advantages by integrating the SOFC stack in the middle of the gas turbine flowpath. The mechanical design of the SOFC stacks may operate with a relatively low pressure difference between the interior (38) and the exterior (40), so that they may be placed in a pressure vessel (9) pressurized by the cathode inlet flow (41) or operated under ambient pressure. This pressure vessel (9), or more generally, the containment vessel (9), may be configured to removably contain at least a portion of the connected individual electrochemical cell stacks, and may also function as an inlet plenum (43), or more precisely as a containment vessel interior space multiple electrochemical cell stack, stack first function electrode inlet plenum, such as for the first function electrode stack, depicted in this embodiment as element (43).In this manner, the intake plenum (43) or containment internal space multiple electrochemical cell stack stack first functional electrode inlet plenum can serve to ensure uniform flow distribution and recover additional heat lost by hotter components within the pressure vessel (9) assembly.

[0011] As can be appreciated, the use of the more general terms first function and second function for the electrodes encompasses a variety of different configurations. For example, the oxygen electrode elements can be arranged in a stack. The stack of oxygen electrode elements can be considered as a stack of first function electrode elements, which can provide the cathode elements. The fuel electrode elements can also be arranged in a stack, which can be considered as a stack of second function electrode elements, which can provide the anode elements. This type of configuration can represent a SOFC system. If the functions are reversed electrically, the stack of oxygen electrode elements can be considered as a stack of first function electrode elements, which can provide the anode elements, and the stack of fuel electrode elements can be considered as a stack of second function electrode elements, which can provide the cathode elements. Such a configuration can represent a SOEC system. If the functions are reversed chemically, the stack of fuel electrode elements can be considered as a stack of first function electrode elements, which can provide the cathode elements, and the stack of oxygen electrode elements can be considered as a stack of second function electrode elements, which can provide the anode elements. Such a configuration can represent a SOEC system. Once again, by electrically reversing the previously described functions, the stack of fuel electrode elements can be considered as a stack of first functional electrode elements and can provide the anode elements, and the stack of oxygen electrode elements can be considered as a stack of second functional electrode elements and can provide the cathode elements. This type of configuration can represent a SOFC system.

[0012] An electrochemical cell stack may include a plurality of connected individual electrochemical cell stacks that may be fluidically, electrically, or most likely both connected, where, for example, the plurality of connected individual electrochemical cell stacks may be configured as a stack selected from: series electrically connected electrochemical cell stacks; series fluidically connected electrochemical cell stacks; parallel electrically connected electrochemical cell stacks; parallel fluidically connected electrochemical cell stacks; and any permutation and combination of the above, even in a particular system. Thus, in establishing a system for operation, configurations may be selected, purchased, operated, or individually constructed such that the system may be considered to provide a series electrochemical cell stack; provide a series fluidic chemical cell stack; provide a parallel electrochemical cell stack; provide a parallel fluidic chemical cell stack; and any permutation and combination of the above.

[0013] Additionally, turbomachines (1, 2, 3) may be additional components in some systems. A compressor (2) and / or turbine (3) may provide the potentially necessary compressed air (44) from an inlet (15, 16) to support both the gas turbine cycle and the SOFC. The turbine (3) may take the pressurized and heated exhaust stream (45) and generate mechanical power that is used in part to power the turbomachine compressor (2), with the remaining turbine power potentially being converted to electrical power via a generator (1). This motor / generator (1) may operate both as a generator to generate electricity while the system is running, and as a motor to power the compressor (2) during startup and possibly shutdown.

[0014] For physical reasons, the turbine (3) may not be able to extract all of the available heat from the combustor exhaust stream (45). To improve efficiency, a turbine recuperator (4) may be added to move much of the remaining heat from the turbine exhaust (46) to the compressor exhaust (47) for recirculation within the system (51) or exhaust (17). The SOFC stack (53) may require relatively high operating temperatures to drive the electrochemical reactions, and as a result, the incoming cathode stream (41), such as from the compressor (2), may need to be sufficiently preheated to prevent undesired cooling of the stack (53). Thus, some electrochemical cell systems may include utilizing a turbine recuperator (4) for part of the process. The turbine recuperator (4) may provide some or most of this preheat, depending on how the system (51) is operated. When the turbine inlet temperature is relatively high and the turbine pressure ratio is relatively low (resulting in a high turbine exit temperature), the turbine recuperator (4) may provide most of the preheat to the cathode inlet flow (41). However, when the turbine inlet temperature is low or the pressure ratio is high, the system may further include a cathode recuperator (5) integrated into the system or utilized by the system (51) to transfer additional heat from the cathode exit flow (48) to the inlet flow (41).

[0015] In some embodiments, the system (51) may be fed by a variety of gaseous fuels (49), possibly including natural gas. In embodiments utilizing natural gas, the fuel (49) may first pass through a desulfurizer (14) to remove sulfur that may contaminate the catalyst in the SOFC, or may include utilizing a desulfurizer or may be desulfurized to accomplish the same. Additionally, the fuel may be metered by a main natural gas valve (13) and then enter the system (51) as the primary fuel source. In some embodiments, it may be beneficial for the fuel to be properly conditioned by some type of conditioner (50) before entering the SOFC stack (53) to ensure that the stack (53) operates effectively and robustly as intended. In some embodiments, important considerations for the stack (53) with respect to fuel supply include having the SOFC electrochemical reaction primarily consume hydrogen directly, and having the stack comprise a catalyst (54) that may convert methane and water, etc., into carbon monoxide and hydrogen in strongly endothermic (heat absorbing) reactions, which, if occurring in high concentrations, may cause supercooling and be damaged by thermally induced stresses. Additionally, hydrocarbons in higher concentrations than methane may have an increased tendency to cause detrimental carbon deposition (coking).

[0016] In some embodiments, a reformer (10) may be included in the system or may be involved as a step in the operation of the system (51) to condition the fuel (49) before it enters the SOFC stack (53) to help address stack fuel supply issues. The reformer (10) may also be included as a catalytic reactor (55) that may support several reactions, such as converting higher hydrocarbons and water to carbon monoxide and hydrogen, possibly using endothermic reactions, converting methane and water to carbon monoxide and hydrogen, possibly using an endothermic methane steam reforming reaction, and converting carbon monoxide and water to carbon dioxide and hydrogen, possibly using an exothermic water gas shift reaction. The water and heat required to drive these reactions may be provided by recycling (56) a portion of the anode effluent (57), which may include heat from the system and water from the SOFC electrochemical reaction, and mixing the recycled liquid with fresh natural gas (58) entering the reformer (10). The reformer (10) may be an adiabatic (or near adiabatic, minimizing heat or mass transfer in the system) device in which the type and temperature of the inlet gas (60), coupled with the equilibrium chemistry between the various reactions, determine the composition and temperature of the reformer outlet (61).

[0017] A recycle blower (11) or ejector can use the recycle stream (62). The amount of anode effluent recycle (57) can be set to control the conditions at the reformer outlet (61). This flow rate can be set to ensure that all higher hydrocarbons are cracked, that enough hydrogen is recirculated in the recycle stream (62) to prevent local fuel starvation in the stack (53), and that a suitable amount of methane remains in stream (48) to help cool the SOFC so that more power can be produced, but not so much that the stack (53) becomes overcooled and is damaged. In an adiabatic design, the outlet of the reformer (10) can be much colder than the inlet (63) due to endothermic reactions, and can be heated to the operating temperature of the SOFC to prevent damage to the stack (53). This can be achieved by using an anode heat exchanger (6) that can heat the anode inlet (64, 421) with the cathode outlet stream (48). In such an embodiment, the process can include utilizing the anode heat exchanger (6) as part of the process.

[0018] A portion of the fuel (49) supplied to the SOFC may remain unconsumed as it exits the stack (53). Any fuel not recirculated by the recirculation blower (11) may enter the combustor (12) and thus provide a utilization step for the combustor (12) where it may be mixed with air, such as from the cathode exhaust in the cathode outlet stream (48), and combusted. This combustion process consumes the remaining fuel (65) while at the same time further heating the already hot cathode exhaust in the cathode outlet stream (48), which may be entered into the turbine (3) to extract a degree of remaining power.

[0019] FIG. 2 is a schematic diagram of an exemplary embodiment of another SOFC-based system (51) showing power export. FIG. 2 adds components that may be useful for controlling the SOFC and motor / generator (1) and outputting power therefrom. Control of the flow of power to and from the motor / generator (1), and thus the speed of the turbomachine, may be achieved through power electronics (18) including a drive, possibly a variable frequency drive (66). Similarly, the load on the SOFC, and thus the power generated by the stack (53), and the fuel consumed in the stack (53), may be achieved through separate power electronics (18). In some embodiments, the system (51) may export power as either DC or AC, and in either islanded or grid-synchronous modes. In embodiments exporting AC power, it may be necessary to step up the voltage, such as from the motor / generator (1), or the generator and SOFC, to a higher level, such as 750V, by the power electronics (18), particularly to voltages common in industrial environments, such as 480V three-phase. For AC systems, an inverter (20) can be used to generate the required frequency / voltage from the DC bus. To stabilize the DC bus (19), a battery (21) can be connected to the bus via its own battery power electronics (67). For grid (22) connected systems, the system (51) can be operated in such a way that the supervisory control system (68) commands it to generate and export a constant amount of power (with or without operator input (69)). However, for islanded systems, the system (51) may need to respond reactively to external electrical loads placed on the system (51). In this case, to prevent the SOFC / GT system from experiencing sudden transients, the supervisory control system (68) can slowly adjust the power output from the system (51) to both supply the external loads, such as the grid (22), and recharge the battery (21) as needed, while the battery (21) can be used to supply short-term electrical demands.

[0020] FIG. 3 is an exemplary embodiment of a schematic diagram of a SOFC-based system (51) including start-up components (70) and shutdown components (71) that may be connected as would be well understood by one of ordinary skill in the art. In some embodiments, additional components are beneficial for the start-up and shutdown of the system (51) and may be included as additional safety features, as shown in FIG. 3. Once the system (51) is fully operational, it may become thermally self-sustaining. However, to reach a point where the SOFCs begin to generate electricity (and generate excess heat), the stack (53) must first be sufficiently heated. This heating may be primarily accomplished via a resistive pressure vessel start-up preheater (27) attached directly to the pressure vessel (9). The pressure vessel (9) itself may be the largest thermal heat sink in the system (51) and may be preheated, such as by the pressure vessel start-up preheater (27), to prevent heat from being drawn from the stack (53). When the pressure vessel shell (8) heats up, all components within the vessel (including the stack (53) and piping) are also heated. In this manner, the system (51) can be smoothly heated without burning other equipment. In some embodiments, additional heat can also be obtained from a cathode-started preheater (26) if desired.

[0021] In some embodiments, to allow the GT system (51) to start up partially independent of the SOFC, the reformer (10) may be vented to the proper inlet conditions before fuel supply, and thus may include an auxiliary natural gas valve (28) to supply the fuel (49) directly to the combustor (12). During start-up and shutdown, once the SOFC stack (53) and reformer (10) exceed a certain temperature, it may be necessary to protect the catalyst (54) from oxygen to prevent degradation. This can be achieved by a purge system (72) that primarily supplies nitrogen to atmospheric or other oxygen-displacing gas (30). Secondarily, a small amount of hydrogen can be added to the flow as a first reaction supplement (73) to create a reducing environment to consume any oxygen that may escape into the system (particularly through the SOFC assembly). This purge stream (74) may be supplied to the system (51) during start-up and shutdown by a valve that introduces a flow of reducing gas (29). Such reducing gases can have a variety of compositions, including, by way of example only, 5% H2 (or other percentages) in N2. In order for the reformer (10) to begin converting higher hydrocarbons to lower molecular weight species and possibly produce the hydrogen needed to initialize the SOFC, some water (33) may first need to be mixed with the fuel (49) via the second reaction complement (75) (with or without the first reaction complement (73)) before entering the reformer. This may be accomplished via the start-up steam generator (32) and metered by the H2O valve (31).

[0022] To support the safety of the system, several additional valves may be incorporated into the system. First, there is a bleed air valve (23). This valve (23) can serve two important functions, but is not limited to these. First, if the compressor (2) approaches a destructive stall / surge event, the valve (23) may be opened to increase the flow from the compressor (2) and move the compressor condition away from that stall / surge condition or line. Second, if the system (51) is operating and the motor / generator (1) load is lost, which could otherwise cause the turbomachinery (1, 2, 3) to overspeed, the bleed air bypass valve (23) may be opened to add additional load to the compressor to make up for the loss of the generator load. A hot air bypass valve (25) may be added to allow flow from the compressor (2) via the compressor exhaust to largely bypass the SOFC during startup and shutdown. This hot air bypass valve (25) is then slowly closed, allowing an increasing proportion of flow from the hot air bypass compressor as the compressor discharge (47), until the valve (25) is fully closed and all flow is diverted through the SOFC, past the compressor, and into the SOFC path. In some embodiments, a cold air bypass valve (24) can be added to the system to bypass flow around the turbine recuperator (4) to help further control temperatures in the system.

[0023] It should be noted that the components and configurations described above are not an exhaustive list of all components necessary or possible for operation or system configuration. In certain embodiments, the present technology may include selective variations of the system architecture detailed below, including, but not limited to: ● The recirculation blower (11) can be replaced with an ejector (78). The ejector (78) can be a device that entrains the flow from the suction port by accelerating and then decelerating the flow from the motive stream. In this case, the motive stream and the power driving the ejector (78) can come from the incoming fuel or perhaps natural gas stream (77), while the suction port is connected to the anode outlet (29, 521) or anode manifold outlet (79). This method can be cheaper and more robust than the recirculation blower (11), but it removes one control variable and can be less efficient. The number of SOFC stacks (53) and their electrical configuration and type are completely variable based on the desired system efficiency and cost. Similarly, the power output of the turbomachinery (1, 2, 3) relative to the SOFC is also variable. The reformer (10) may be isothermal (e.g., the internal gas temperature is kept constant by heat transfer from the outside) rather than adiabatic. This may reduce the amount of external reforming and reduce the amount of methane cooling the stack (53). However, under certain conditions this may be desirable and may also eliminate the need for the anode heat exchanger (6). If there is enough heat present at the turbine exit or exhaust (46) via the GT flowpath (35) or if enough heat is passively transferred from components within the pressure vessel (9) to the cathode inlet flow or stream (41), the cathode recuperator may be eliminated. Removing this component may be desirable as it can add additional pressure drop to the system (51) (e.g., power loss), and additional external heat losses (due to increased surface area), as well as additional system costs. It is also possible to remove the cathode preheater (26) and use only the pressure vessel preheater (27). This may improve the response time in adding additional heat to the gas stream, but it removes a component (additional cost) and may reduce the pressure drop through the system (51). Depending on the control strategy employed during start-up, shutdown and load transients, the hot and cold air bypass valves (25, 24) may be removed. ● The system (51) may be powered by the alternative fuel (49) and the alternative fuel stream or incoming fuel stream (77). If a hydrogen fuel stream is available, the reformer (10) may be eliminated and hydrogen may be used directly. Other hydrocarbon fuels may be used by modifying the reformer (10) recipe. - The fuel stream or streams (77) may be preheated via the system exhaust (17) or exhaust gas stream, or via a heat exchanger with other flow paths in the system. • The system may be operated under pressurized rather than pressurized conditions. As will be readily understood by one of ordinary skill in the art, as part of an SOEC system, the system may be operated in reverse to convert steam (or steam and carbon dioxide) and electricity into oxygen and hydrogen (or hydrogen and carbon monoxide).

[0024] In some embodiments, due to the mechanical design of the SOFC (and SOEC) stack (53), the system (51) may generally have approximately the same internal and external pressures to minimize mechanical stresses and stack leakage that may be induced by pressure differences. Because the stack (53) in a SOFC / GT system operates under pressure, it may be necessary to house the stack within a pressure vessel (9). Given that the stack (53) is hot and may be located within a pressure vessel (9), careful design is beneficial in creating the system (51). Considerations in this regard include: To ensure consistent operation, the cathode and anode flow distribution among the various stacks (53) may need to be uniform, which can be difficult to achieve due to the complexity of manifolding all the stacks (53) in a limited area while minimizing pressure drop, which directly impacts system efficiency. For maximum efficiency, it is essential that the pressure vessel (9) is well insulated against heat loss from the outside, and this has certain sub-considerations: The pressure vessel (9) may be pressurized by the gas turbine (3), which means that the flow path (80) between the two elements may be pressurized. Previous studies have shown that insulation within the pressure vessel (9) may become dislodged and enter the turbine (3) or other components, causing damage. When the system (51) is shut down, the pressure in the pressure vessel (9) will drop. If this happens suddenly, the insulation in the pressure vessel may experience an explosive decompression as air trapped in and behind the insulation expands, which may damage the insulation. The mechanical structures inside the pressure vessel (9) are very complex and can be difficult to insulate. ●Leaking hydrogen or other fuels into the pressure vessel (9) could be extremely dangerous, especially if they build up to explosive levels in parts of the pressure vessel (9) that do not have much air flow, or if they become trapped and concentrated in some of the internal insulation. ● When the system (51) is heated to operating temperature, significant thermal growth often occurs, causing all the stacks (53) to move away from each other. This can pose challenges to the manifolds and support structures within the pressure vessel (9). It can be beneficial to carefully design the system (51) so that thermal growth of components within the pressure vessel (9) does not cause thermally induced stresses that could damage the hardware. During shutdown, the internal pressurized gas expands back into the atmosphere, potentially causing compressed cathode air to backflow through the compressor (20), which could reverse the flow through the cathode portion of the stack (53) and cause combustion products to enter the stack (53), potentially damaging the SOFC. The stack may require compression forces to prevent the individual cell layers from separating. The compression mechanism (81) may need to withstand the thermal expansion of the stack up to operating temperatures and, even more challenging, may need to withstand the high temperatures within the stack (53) or pressure vessel (9) without adversely affecting the compression forces.

[0025] FIG. 4 is an exemplary embodiment of a solid oxide fuel cell assembly (82) and a pressure vessel (9, 100). In such a system, as in the embodiment of the pressure vessel shown in FIG. 4, some of the above considerations may be taken into account. As embodied herein, it may be beneficial to utilize the pressure vessel (100), which may be the "containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum" itself, as the cathode inlet plenum (200). This may provide several advantages, including ensuring uniform flow distribution among the various stacks (53), ensuring non-uniform flow distribution within each stack among the various cells (52), etc. It may also eliminate the need for large cathode manifolds to distribute flow to and from the various stacks (53). In this design, all components within the pressure vessel (100) may be surrounded by the cathode inlet flow (41) before this flow enters the stack (53). This allows the cathode inlet flow (41) to recover some heat from the surrounding components that may otherwise be lost. This also serves to add additional heat to the incoming cathode air in the cathode inlet stream (41), eliminating the otherwise costly cathode recuperator (5).

[0026] As particularly shown in FIG. 13, the configuration can be selected, purchased, operated or constructed such that the system can be considered to establish a "containment vessel internal space multiple electrochemical cell stack stack first functional electrode inlet plenum" and further provide a plenum that accomplishes the step of completely surrounding and containing each of the multiple stack first functional electrode inlets.

[0027] In further embodiments, the system may be configured to completely surround and include multiple stack second functional electrode outlets, either separately or together. Additionally, the system may include various manifolds. There may be a first functional electrode outlet manifold likely to be connected to each of the stack first functional electrode outlets; a second functional electrode inlet manifold likely to be connected to each of the stack second functional electrode inlets; and a second functional electrode outlet manifold likely to be connected to each of the stack second functional electrode outlets. Similarly, the system may be selected, purchased, or constructed in a manner that would be considered to establish a first functional electrode outlet manifold, connect the first functional electrode outlet manifold to each of the stack first functional electrode outlets, establish a second functional electrode inlet manifold, connect the second functional electrode inlet manifold to each of the stack second functional electrode inlets, establish a second functional electrode outlet manifold, and connect the second functional electrode outlet manifold to each of the stack second functional electrode outlets. When such manifolds are included, the system may be configured to accomplish the steps of surrounding at least a portion of the second functional electrode inlet manifold and surrounding at least a portion of the second functional electrode outlet manifold. Other embodiments may also include a "containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum" configured to surround each of the second functional electrode inlet manifold and the second functional outlet manifold. Further embodiments may be configured to establish substantially equivalent environmental intake conditions for each of the plurality of first functional electrode elements or may include establishing substantially equivalent environmental intake conditions for each of the first functional electrode elements.

[0028] In some embodiments where the cathode inlet stream (41) surrounds all components, the internal temperature will be in the range of 750-850°C, with lower temperatures outside the stack (53) and higher temperatures at the outlet (83) of the stack (53) (due to heat released within the SOFC). This approach is referred to herein as the "high temperature pressure vessel" concept. In this embodiment, all or most of the insulation (300) can be located outside the pressure vessel. This can have several advantages including greatly simplifying the design of the insulation (300) (e.g., it can be placed around a relatively smooth cylinder rather than surrounding complex components within the pressure vessel (100)). Locating the insulation outside the pressure vessel (100) eliminates the possibility of the insulation (300) experiencing an explosive decompression or otherwise entering the air stream and damaging components within the system (51). Similarly, by not locating the insulation (300) within the pressure vessel, hydrogen and other fuels are not trapped within the insulation (300) and causing potential hazards. Furthermore, any hydrogen leaking from the anode manifold into the pressure vessel (100) may immediately combust, well above the hydrogen's autoignition temperature of 585° C., due to the presence of oxygen in the cathode intake plenum containing the cathode inlet stream (41). (While this sounds dangerous, it may be preferable to a large amount of fuel collecting in the pressure vessel (100) and exploding.)

[0029] In another embodiment, another advantage of the high temperature pressure vessel concept is that most of the capacitance (volume) of the system can be held in the cathode inlet plenum containing the cathode inlet flow (41). During rapid depressurization, flow can exit through both the compressor (2) and turbine (3) of the GT. However, since the cathode inlet plenum containing the cathode inlet flow (41) can be the largest reservoir of compressed air, this air can flow through the stack (53) to the turbine (3) and back to the compressor (2). Therefore, backflow through the stack (53) should not occur.

[0030] FIG. 5 is another exemplary embodiment of a solid oxide fuel cell assembly (82) and pressure vessel (9). In some embodiments, as the system heats up to operating temperatures, all components within the heated area, and possibly within the pressure vessel (9), may expand away from one another. To address this, embodiments may include electrochemical cell stack mounts that are fully accommodative for thermal expansion and contraction. Through such mounts, the system may be able to thermally expand and contract, substantially fully or fully, the multiple connected individual electrochemical cell stacks within the containment vessel interior space multi-electrochemical cell stack stack first functional electrode inlet plenum as the temperature changes from ambient to maximum operating temperature. As also shown in FIG. 5, in addition to accommodating thermal expansion and contraction of the stack, embodiments may have elements that accommodate manifold expansion and contraction as well. As shown in FIG. 5, the pressure vessel (9) and even the stack first functional electrode inlet plenum (43) may be sized to accommodate any or all of the various manifolds (as shown), as well as each of their thermal expansions and contractions. In such an embodiment, the manifold can be entirely, substantially, or partially within the containment vessel interior space of the multi-electrochemical cell stack stack first functional electrode inlet plenum. Additionally, the manifold can be designed as a substantially fully thermal expansion-contraction manifold, such as with accordion-type expansion tubes, expansion joints, or other known elements. Additionally, the pressure vessel (9) or stack first functional electrode inlet plenum (43) can have a fully dimensionally thermal expansion-contraction interior space.Also, as can be seen in FIG. 13, where only a portion of the manifold(s) is within the plenum (such as the anode inlet manifold (89) and the anode outlet manifold (90)), the system may be operated to accomplish any or all of the following steps: making at least a portion of the second functional electrode inlet manifold within the containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum substantially completely accommodate thermal expansion and contraction; making at least a portion of the second functional electrode outlet manifold within the containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum substantially completely accommodate thermal expansion and contraction; or the like with respect to any of the manifolds.

[0031] As mentioned above, embodiments can include electrochemical cell stack mounts that are fully accommodating for thermal expansion-contraction. This can accommodate expansion and contraction of the stack itself. As shown in Figures 4, 5 and 6, embodiments can include mounting all stacks (53) on a manifold, perhaps a cathode outlet manifold (111), which can then act as the primary support structure (as shown in Figure 5) with or without a shelf on the manifold. More generally, embodiments of the invention can be configured to include any or all of a substantially singular CTE mount, a manifold stack mount, and / or a stack shelf on which each of a number of connected individual electrochemical cell stacks can be mounted. One example of this can be the cathode outlet manifold (111) used as a mount as shown, where the manifold stack mount can be a first functional electrode outlet manifold stack mount, a second functional electrode inlet manifold stack mount, or a second functional electrode outlet manifold stack mount. Mounting the multiple connected individual electrochemical cell stacks with substantially differential thermal expansion coefficient mounts, such as using differential materials, may allow for more uniform expansion-contraction.Furthermore, in operating the system, utilizing a manifold stack mount may be accomplished, including utilizing a first functional electrode outlet manifold stack mount, utilizing a second functional electrode inlet manifold stack mount, or utilizing a second functional electrode outlet manifold stack mount.A configuration having an electrochemical cell support manifold in general, and possibly: having an electrochemical cell support outlet manifold or achieving the steps of supporting an electrochemical cell stack with a first functional electrode outlet manifold; having a first functional electrode outlet manifold stack mount; establishing a first functional electrode outlet manifold stack mount; having a second functional electrode outlet manifold that accommodates substantially entirely thermal expansion and contraction; or having a second functional electrode outlet manifold that accommodates substantially entirely thermal expansion and contraction within the containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum; may have several advantages. First, as an example, the cathode outlet manifold (111) is not constrained from expanding along the length of the pressure vessel (9), and therefore is free to expand without inducing internal mechanical stresses. This may eliminate the need for expensive expansion joints on the cathode side in this design. Second, the incorporation of both the cathode outlet manifold (111) and the stack support structure into a single component, such as the pressure vessel (9), may reduce the complexity, size, and cost of the system. Additionally, the cathode outlet manifold (111) can support the stack assembly (82) when the structure is cooled, and the pressure vessel body can be stored on roller elements (222) via rolling the components within the containment vessel, on slide elements (as shown in FIG. 4) via sliding the components in the containment vessel, or on some other type of interface to allow easy access.

[0032] Also visible in FIG. 5 is one potential support and mounting structure (333) approach for the stacks (53). Two (or more / fewer) stacks (53) may be loosely attached to shelves (334) (allowing for thermal growth), with a total of three shelves (although more or less) shown in FIG. 5. In some embodiments, this may include a stack shelf on which each of the multiple connected individual electrochemical cell stacks is attached, or may include utilizing a stack shelf on which each of the multiple connected individual electrochemical cell stacks is attached. In some embodiments, these shelves (334) may then be attached to a cathode outlet header (335) of the cathode outlet (or other) manifold (111). A cross-sectional view of the shelves (334) and mounting structure (533) is shown in FIG. 6. This shows how the cathode inlet and outlet flow (121) enters the front of the stack (53) and then flows into an outlet plenum (221) where the flows from the two stacks can be combined before exiting into the cathode outlet manifold (321).

[0033] Due to the design of the SOFC stack (53) (anode, electrolyte, cathode, current collectors, flow channels, and sealing layers fused together), a compressive load may be required to prevent separation of the various elements due to thermal expansion or applied pressure. This is shown as a gravity load in Figures 4, 5, 6, and 11, and as a spring compression load in Figures 7 and 13. A compressive force of hundreds of pounds (hundreds of kilograms) may be required to prevent damage to the stack. This force may be maintained (to some extent) from the time the stack (53) is initially fused during assembly, through transportation and installation, throughout the operating temperature (51) in the SOFC / GT system, and upon return to ambient temperature. This challenge is exacerbated by the high temperature environment that the compression mechanism (81) (shown in Figures 4 and 7) is required to survive. It should be noted that the same compression mechanism (81) may not need to be applied both during transportation and installation / operation. An embodiment may include compressing the compression stack mount or individual connected electrochemical cell stacks. Focusing on the methodology employed during installation and operation, an embodiment such as that shown in FIG. 13 can include a compression tie rod (94), a compression element, and / or a spring element (91), and in some cases can include steps utilizing a compression tie rod, steps utilizing a compression element, and / or steps utilizing a spring element (91).

[0034] In certain embodiments, it may be desirable to provide a compression element, possibly a spring element (91), external to the vessel or plenum (92). Thus, embodiments may include at least part vessel external compressive stack mounts, as well as at least part vessel external compressive stacks of the connected individual electrochemical cell stacks. In some embodiments, such as shown in FIG. 13, this may include at least part vessel external spring elements (91) or may include at least part vessel external spring elements. Further embodiments may include a thermal barrier (93) configured to substantially thermally isolate at least a portion of the vessel external compressive stack mounts, or may include substantially thermally isolating the at least part vessel external compressive stacks of the connected individual electrochemical cell stacks from the containment vessel internal space multi-electrochemical cell stack stack first functional electrode inlet plenum. Embodiments may also include non-hot compressive stack mounts, or may include non-hot compressive stacks of the connected individual electrochemical cell stacks.

[0035] FIG. 7 is an exemplary embodiment of a solid oxide fuel cell stack shelf (334). Two methods are proposed and shown in FIG. 7: springs (201) and weights (101). The weights (101) can be simply a mass placed on top of the stack to provide the necessary compressive force by gravity loading. The advantages of this method are that it is simple, reliable, and insensitive to temperature changes, continuing to apply the same load as the stack thermally expands and contracts. Potential disadvantages are that it is heavy (requiring additional support structure) and may not be suitable for mobile applications, as inertial loading can cause the weights (101) to momentarily lift off the top of the stack (53), removing significant compressive load.

[0036] As mentioned above, the compression mechanism (81) can be configured as gravity-based compression, spring-based compression, or a combination thereof, among other possibilities. As shown in FIG. 7, a series of compression springs (201) can be utilized to provide some or all of the required compression force. The advantage of this approach is that the springs are much lighter than the plumb bob (101) since they utilize internal strain to store the compression force. Similarly, they are lighter and do not rely on gravity for the compression load, making them less susceptible to inertial loads and suitable for mobile applications. One possible difficulty in implementing the springs (201) can be the high operating temperatures experienced within SOFC / GT systems. The strength of suitable spring materials is greatly reduced at these temperatures, and material creep can cause loss of compression force over time if the springs (201) are not properly designed (although springs have already been designed to operate under these conditions for this application). The left stack in FIG. 7 shows a hybrid design to reduce the requirements for the spring (201) where part of the compressive load is applied by the spring weight (301) and the remaining load is applied by the spring (201).

[0037] In some embodiments, multiple variations of the pressure vessel (9) and stack mounting design described above may be possible. Embodiments may include, but are not limited to, variations such as: One potential concern with the high temperature vessel concept is the cost of materials. The cost of the pressure vessel could be reduced by changing to a lower temperature alloy (less expensive) and installing a refractory liner (85) and / or a thermal barrier (93) as shown in Figure 13. This liner acts as a high temperature insulating layer that keeps the shell (8) of the pressure vessel (9) cool, potentially allowing for a more cost-effective design. In addition to utilizing weights (101) and springs (201) to provide stack compression, the force can also be applied by other mechanisms, such as pneumatic actuation. In a pneumatic design, a pneumatic actuator (84) may be installed at each stack (53) and connected to an air pressure source (85) external to the pressure vessel (9) as shown in FIG. 2. In this manner, the compression load can be dynamically controlled (by varying the air pressure) and verified (by monitoring the air pressure), and can be easily compensated for temperature changes and thermal expansion.

[0038] Other aspects for mounting the stack include: In the illustrated embodiment, only six stacks (53) on three shelves are shown. In other embodiments, this approach can be adapted to more or fewer stacks (53) as needed to meet desired system power levels, efficiencies, and / or hydrogen (or other gas) production rates. • The vessel design can be used as part of a SOFC or SOEC system. ● The cathode inlet (121) and outlet (321) may be reversed (for example, the inlet plenum (shown as element (121) in Figure 6) and the outlet manifold (shown as element (321) in Figure 6) may be reversed so that flow enters through the manifold and exits the plenum). The cathode (41,48) and anode (64,79) flows may be swapped such that the cathode flow is contained within the anode line (shown in FIG. 6 as elements (421,521)) and the anode flow is contained within the cathode line (shown in FIG. 6 as elements (121,321)).

[0039] FIG. 8 is an exemplary diagram of conventional cathode flow and stack temperature distribution. In planar SOFCs (and SOECs), the stack (53) can suffer from large thermal gradients along the width and height (perpendicular to the direction of flow) of the stack (53). These thermal gradients can result from large heat losses transferred through the stack faces to the surrounding environment, as a result of the ends (86) of the stack being much cooler than the core (87) (as shown in FIG. 8). This can be disadvantageous for several reasons, including reduced efficiency as the ends (86) of the stack operate at a lower (less efficient) temperature compared to the core (87), the need to provide additional flow to the cathode to prevent overheating of the core (87), thermally induced stresses within the stack (53), etc.

[0040] In the case of SOFC, the cathode flow may act as an oxidant for the electrochemical reaction and as a heat transfer medium to carry heat generated by the electrochemical reaction away from the stack (53). The intent of the described embodiment is to create a non-uniform flow distribution across the cathode face to match the cathode flow rate in each region of the stack with the heat that may be carried away by the cathode flow. In this way, the temperature across the width and height of the stack may be much more uniform compared to conventional approaches (e.g., constant distribution of the cathode flow across this face). By maintaining a more uniform temperature, the efficiency of the system (51) may be improved by increasing the temperature of the stack (53) along the ends (86) closer to the optimal maximum temperature of the core (87), reducing the required cathode flow rate (thereby reducing parasitic losses) and reducing thermally induced mechanical stresses in the stack (53).

[0041] FIG. 9 is a simplified exemplary diagram of cathode air flow and temperature axial distribution before and after entering the stack according to one embodiment of the present technology. The non-uniform cathode flow distribution described in this embodiment can be compensated for by placing a device such as at least one electrochemical cell stack axial flow conditioner or by achieving a step of establishing a differential axial flow in at least one electrochemical cell stack. The electrochemical cell stack axial flow conditioner may be placed in the cathode flow stream, shown conceptually in FIG. 9 as a graded distribution plate (99) and more literally in FIG. 11 as a graded distribution plate (444). This may be more generally at least one electrochemical cell axial flow conditioner plate, or may be achieved by an operation having a step of utilizing at least one electrochemical cell axial flow conditioner plate or at least one graded distribution plate, which can increase the pressure drop around the stack edge (86) compared to the core (87). Plates or other electrochemical cell stack axial flow conditioning devices may be fixed, variable, or replaceable, so that embodiments may have at least one fixed graded distribution plate, or may achieve during operation the step of utilizing at least one fixed graded distribution plate. Increasing the pressure drop over the end regions of the stack (53) results in less cathode flow through these regions, resulting in more flow in the core regions with lower pressure drop (under the same flow conditions) to achieve more uniform flow throughout the stack (53).

[0042] A gradient distribution plate (99) can be created using multiple methods. One possible approach, depicted in FIG. 9, features a plate with a series of holes that are larger in the center (potentially resulting in more flow / heat transfer through the stack's core (87)) and gradually get smaller (leading to less cathode flow / heat transfer in these regions) as they approach the stack's edges (86). The flow distribution can be optimized based on the stack design and operating conditions, and one conceptual example of a gradient is shown in FIG. 10, with lighter shading indicating less flow restriction due to the electrochemical cell stack axial flow conditioners.

[0043] The sloped distribution plate (99) can be located either before or after the stack (53). Locating the distribution plate after the stack (53) and slightly offset may be preferred based on flow dynamics which may result in a smoother flow field gradient. A possible embodiment of a fixed sloped distribution plate (444) is shown in FIG.

[0044] There are multiple embodiments of this basic concept of an electrochemical cell stack axial flow conditioner, or even a graded distribution plate (99) or device. The electrochemical cell stack axial flow conditioner can be made in a variety of ways (just a few are mentioned), such as by using a plate with a varying distribution of holes (as described above), a variable thickness porous material, a variable thickness porous material, a set of screens that can include at least one stacked multiple screen element, or by using at least one stacked multiple screen element with circular holes in the center ranging from large to small and stacked on top of each other to create a graded pressure drop. Regardless of the physical implementation of this device or electrochemical cell stack axial flow conditioner, the embodiments relate to a process of varying the cathode flow axially across the face of the stack to improve system performance.

[0045] In addition to the fixed distributors (88) mentioned above, the flow distributors (88) can also be passively or actively controlled. One embodiment of a controllable flow distributor can include using two distribution plates arranged on top of each other with pairs of openings that either change the distribution of those openings or change the relative size of those openings when one plate is moved relative to the other. The movement of these plates relative to each other can be accomplished either manually (e.g., as part of a tuning process) or controlled by some active or passive device to achieve the desired flow and / or temperature distribution and system operation. Another example of passively or actively controlling the flow distributors (88) is a system that can change the size of the holes and the associated pressure drop based on the temperature coming through each section of the distribution plate (99 or other). Examples include utilizing materials with high thermal expansion, active control via piezoelectric elements, etc.

[0046] In some embodiments, control of the SOFC / GT system may be an important consideration for the system design. In relation to (51) control of the system, some embodiments may include, but are not limited to: • It may be beneficial for the control strategy to be robust, protecting the system in the event of component failure, and adapting to variations in system performance as environmental conditions change or the system ages. • Control strategies may maximize system performance and efficiency. • Control strategies may be able to adapt to changing electrical load demands.

[0047] Effective and robust control of a SOFC / GT system (51) may require a complex set of control strategies. Many of these strategies may employ known components. However, some embodiments are potentially novel and may add to the advantages of the described SOFC / GT system.

[0048] For clarification in some embodiments, the amount of power generated by the SOFC / GT system (51) can be controlled by adjusting the amount of fuel (49) fed to the system (51). The system (51) is likely to be controlled to operate as efficiently as possible. One way to improve efficiency would be to maximize the efficiency and power generation of the SOFC (since SOFCs generate power much more efficiently than GTs). Analysis shows that the efficiency of the SOFC could be maximized by maintaining the stack (53) at as high a temperature as allowed based on material constraints. This could be accomplished by implementing a component such as a supervisory control system (68) in a closed loop controller that monitors the maximum temperature of the stack and can also adjust the electrical load on the stack (53) to maintain the desired temperature.

[0049] Analysis also shows that the efficiency of a SOFC / GT system can be maximized by maintaining the turbine inlet temperature as high as possible based on material constraints. This can be achieved with a closed-loop controller that monitors the turbine inlet temperature and adjusts the GT speed to maintain the set temperature.

[0050] As an example, in some embodiments, the system (51) may start at 90% power, with both the stack (53) and turbine inlet temperatures at the desired temperature values. The system may transition from 90% power to 100% power by increasing the fuel flow rate accordingly. This fuel flow first passes through the stack (53), which is only mildly affected by the change in fuel concentration and continues to consume the same amount of fuel (49). However, more fuel may exit the stack (53) and enter the combustor (12), increasing the turbine inlet temperature. The turbine inlet temperature controller of the supervisory control system (68) may respond by increasing the speed / flow rate from the compressor (2) to dilute the added heat and reduce the turbine inlet temperature to the desired level. The increase in compressor flow rate through the stack (53) may increase the heat transported from the stack (53), resulting in a decrease in temperature within the stack. The maximum stack temperature controller in the supervisory control system (68) can increase the load on the stack (53) to dump more heat and bring the stack (53) back up to temperature. Increasing the stack load consumes more fuel (49), which results in less fuel flowing to the combustor, which in turn reduces the turbine inlet temperature. These two control loops may work together to achieve a steady state operating point where both the maximum stack temperature and the turbine inlet temperature reach their desired values ​​(although there may only be a single speed / stack load combination that will result in such operation). If configured as a closed loop control and properly designed and tuned, changing power levels will not result in significant oscillations. Using the closed loop control strategy described, a relatively simple control approach can be used to optimize the efficiency of the system.

[0051] In some embodiments, a method for high efficiency power generation may include, but is not limited to, the following steps: capturing thermal energy and excess fuel from the SOFC; feeding the captured SOFC thermal energy to the turbine flowpath; capturing turbine waste heat for electrochemical reactions in the SOFC; preheating the SOFC cathode flow; and determining and optimizing circulating heat from the cathode outlet for utilization in other processes. These steps may be completed manually by an operator or autonomously by passive or active control. In some embodiments, a parameter such as thermal energy capture rate may be achieved by passive control that measures waste heat flow rate or another system parameter such as temperature, fuel flow rate, fuel burn rate, etc.

[0052] As previously mentioned, various electrochemical cell types and systems may be used in embodiments, some of which are detailed below: (1) Solid Oxide Fuel Cell: Fuel gas, which may be hydrogen, methane, and / or syngas (H2+CO), is fed to the fuel electrode flow passages, and air or oxygen is fed to the oxygen electrode flow passages, where the oxygen is converted to oxygen ions that conduct through the ceramic electrolyte and oxidize the fuel at the fuel electrode, providing a highly efficient means of generating power from fuel.

[0053] (2) High-temperature steam electrolysis (or solid oxide electrolysis): Water vapor or a mixture of hydrogen and water vapor is fed to a fuel electrode and electricity is passed between the fuel electrode and the oxygen electrode, where oxygen ions are separated from the water vapor to form hydrogen, which is then conducted through the ceramic electrolyte and recombined at the oxygen electrode to form oxygen molecules. Often, a sweep gas (air or carbon dioxide) is passed through the flow passage of the oxygen electrode to sweep away the oxygen generated at the oxygen electrode. The oxygen generated at the oxygen electrode can also be recovered. This provides a highly efficient means of producing hydrogen from water vapor. (3) Reversible solid oxide cells: Solid oxide cells that can operate reversibly in both fuel cell and electrolysis modes are also possible. For example, reversible solid oxide cells can be used for long-term energy storage to support power grids with large amounts of intermittent renewable energy. The solid oxide cells produce hydrogen during periods of low demand and electricity during periods of high demand.

[0054] (4) High-temperature co-electrolysis: Water vapor and carbon dioxide (or a mixture of water vapor, carbon dioxide, and hydrogen) are supplied to a fuel electrode, and electricity is passed between the fuel electrode and the oxygen electrode. This separates oxygen ions from the water vapor and carbon dioxide at the fuel electrode to produce hydrogen and carbon monoxide. These oxygen ions are conducted through a ceramic electrolyte and recombine at the oxygen electrode to produce oxygen molecules. In many cases, a sweep gas (air or carbon dioxide) is passed through the flow path of the oxygen electrode to sweep out the oxygen generated at the oxygen electrode. The oxygen generated at the oxygen electrode can also be recovered. This allows for highly efficient production of synthesis gas (hydrogen + carbon monoxide) from water vapor and carbon dioxide, and this synthesis gas can be easily converted into liquid fuels or high-value-added chemicals using commercially available chemical synthesis technology.

[0055] (5) High-temperature carbon dioxide electrolysis: Carbon dioxide is supplied to a fuel electrode, and electricity is passed between the fuel electrode and the oxygen electrode. This separates oxygen ions from the carbon dioxide at the fuel electrode to generate carbon monoxide, which then conducts through the ceramic electrolyte and recombines at the oxygen electrode to generate oxygen molecules. To sweep out the oxygen generated at the oxygen electrode, a sweep gas (air) is passed through the flow path of the oxygen electrode. The oxygen generated at the oxygen electrode can also be collected. This allows carbon monoxide (and oxygen) to be produced from carbon dioxide with high efficiency. Carbon monoxide produced from the electrolysis of CO2 can be used as a raw material for producing liquid fuels and / or high-value-added chemicals by commercially practical chemical synthesis technology. Oxygen produced from carbon dioxide can be used to support life (for example, on Mars). (6) Electrochemical oxygen separation from air: This is also a type of electrolysis in which air is pumped through a pair of electrode channels and electricity is passed between the electrodes to generate oxygen ions at one electrode, which are then conducted through a ceramic electrolyte to recombine at the opposite electrode to form oxygen molecules, after which the purified oxygen is recovered.

[0056] There are other types of electrochemical cells and electrochemical cell stacks that could use the proposed technology, including: (1) High-temperature proton-conducting ceramic electrolyte. In this type of electrochemical cell, the ceramic electrolyte is a proton conductor, and the operating temperature is in the range of 500-600 °C. In power generation in fuel cell mode, hydrogen and air are supplied to the opposing electrodes, hydrogen molecules are converted to hydrogen ions (protons) at the fuel electrode, the protons are conducted through the electrolyte membrane, and react with oxygen at the oxygen electrode to form water vapor. When producing hydrogen from water vapor, electricity is passed through the two electrodes, water vapor is sent to one electrode, hydrogen ions (protons) are separated from the water vapor at the fuel electrode, and the protons are conducted through the electrolyte membrane to the opposite electrode, where the protons recombine to form hydrogen molecules, and hydrogen is recovered.

[0057] (2) Molten Carbonate Fuel Cell. In this type of electrochemical system, the electrolyte membrane is a mixture of lithium carbonate and potassium carbonate, the conducting species is carbonate ion (CO3), and the operating temperature ranges from 600 to 700 °C. In the fuel cell mode for power generation, oxygen reacts with CO2 at the oxygen electrode to form carbonate ions, which are conducted through the electrolyte to the fuel electrode, and hydrogen reacts with carbonate at the fuel electrode to form water vapor and carbon dioxide. In the electrolysis mode, water vapor and carbon dioxide react at the fuel electrode to produce hydrogen and carbonate ions, which are conducted through the electrolyte to the oxygen electrode, and the carbonate ions are converted to carbon dioxide and oxygen at the oxygen electrode. (3) Phosphoric acid fuel cell. In this type of fuel cell, the electrolyte membrane is phosphoric acid, the conductive species is hydrogen ions (protons), and the operating temperature is in the range of 150 to 200°C.

[0058] (4) Proton exchange membrane fuel cells and electrolysers. In this type of electrochemical system, the electrolyte membrane is a polymer material, the conductive species is hydrogen ions (protons), and the operating temperature is typically in the range of 60-80°C. Higher operating temperatures (10-200°C) are possible with different types of polymer membranes. (5) Alkaline fuel cells and electrolyzers. In this type of electrochemical system, the electrolyte membrane is an aqueous potassium hydroxide solution, the conductive species is hydroxide ion (OH), and the operating temperature is in the range of 60-80°C.

[0059] Thus, it should be understood that the embodiments may generally include solid oxide electrochemical cells, power generating electrochemical cells, electrolysis cells, gaseous substance generating electrochemical cells, solid oxide fuel cells, or solid oxide electrolysis cells. Similarly, operating the system may include the steps of: providing a plurality of power generating electrochemical cell stacks, providing a plurality of gaseous substance generating electrochemical cell stacks, providing a plurality of connected individual solid oxide electrochemical cell stacks, providing a plurality of connected individual solid oxide fuel cell stacks, or providing a plurality of connected individual solid oxide electrolysis cell stacks. Furthermore, any of the above cells may be proton exchange membrane cells, direct methanol cells, alkaline cells, phosphoric acid cells, molten carbonate cells, solid oxide cells, solid oxide proton conducting cells, or high temperature proton exchange membrane cells. Similarly, operating the system may include the steps of providing a plurality of connected individual electrochemical cell stacks selected from the following: proton exchange membrane cell stacks, direct methanol cell stacks, alkaline cell stacks, phosphoric acid cell stacks, molten carbonate cell stacks, solid oxide cell stacks, solid oxide proton conducting cells, and high temperature proton exchange membrane cell stacks.

[0060] In considering each possible embodiment configuration, the following considerations may be helpful: (1) In many solid oxide fuel cell and electrolysis applications, the systems can be relatively large (scales from hundreds of kilowatts to hundreds of megawatts) and it is not practical to build a system with compromises on a single stack. Thus, it may be necessary to combine multiple stacks, or multiple modules made up of multiple stacks, into a system. Thus, a key system design consideration can be the means to couple multiple stacks into modules and to deliver reactant gases to each stack or module in the system. The present invention describes a useful approach to achieve this modularization.

[0061] (2) To maximize the efficiency of solid oxide fuel cells and electrolyzers, high reactant utilization (e.g., high fuel utilization in fuel cell mode operation, high steam utilization in electrolysis mode operation) may be required. For high temperature electrolysis, some hydrogen in the steam supply may be required to keep the nickel-based fuel electrodes in the metallic state. For this reason, a reactant recycling approach is often employed. This recycling can be accomplished by physical means (blowers) or passive means (ejectors). Another recycling approach is cascade, whereby spent fuel and / or air exiting one stack is fed to the fuel and / or air input of a second stack.

[0062] (3) To those skilled in the art, the electrodes of an electrochemical cell are commonly referred to as the anode and the cathode. The anode is typically the electrode where the oxidation reaction occurs, and the cathode is the electrode where the reduction reaction occurs. Thus, in the fuel cell mode, the fuel electrode is the anode and the oxygen electrode is the cathode. In the electrolysis mode, the fuel electrode is the cathode and the oxygen electrode is the anode. For simplicity and to avoid confusion, the terms fuel electrode and oxygen electrode are used in this application. (4) In the electrolysis mode, the system has a steam input or is operated in a manner that accomplishes a step that utilizes a steam input as part of the process.

[0063] One embodiment of an electrolysis type system is shown in FIG. 12. As can be seen, air is provided, such as by a blower (412). This air is conditioned by an air recuperator (411) and used in the process via an air heater (410). Before the air is used in the process, it is raised in temperature, such as by an air recuperator, and may be further raised in temperature via an air heater. The reheated air is provided to the electrodes, electrochemical cells, and cell stack as shown. The remainder is exhausted through a vent stack (403), possibly via some conditioning or dilution element (404). Steam is provided from a water source (401) to a steam generator (402), fed through a fuel recirculation ejector (408) to a fuel recirculator (407), and finally to a fuel heater (409) for use in the process. The heated fuel may be injected into the electrodes, electrochemical cells, and cell stack, possibly via a manifold (414), as shown. Similarly, air may be supplied via manifold (413) as shown conceptually. As can be seen throughout the preceding discussion of SOFCs, in this SOEC design, the electrodes and electrochemical cells may have air and fuel electrode outlets (418) which may also be manifolded as in manifolds (417) and (416). Again, if used for power generation, the system may be controlled by power electronics (18) perhaps to provide power to the grid (22). Additionally, gas production such as hydrogen and oxygen may occur via condenser or separator (405) and then provided to customers via supply (406). All may be contained within a containment vessel (9) with appropriate plenums as previously described.

[0064] While the present technology has been described in connection with certain preferred embodiments, it is not intended to limit the scope of the present technology to the specific forms defined, but rather to cover alternatives, modifications, and equivalents as may be included within the spirit and scope of the present technology as defined by the invention specification. Examples of clauses and alternative claims include the following: [Clause 1] 1. An electrochemical cell system for use in either power generation or electrolysis mode, comprising: a plurality of connected individual electrochemical cell stacks, each of the plurality of connected individual electrochemical cell stacks including a plurality of first functional electrode elements, a plurality of second functional electrode elements, a stack first functional electrode inlet, a stack first functional electrode outlet, a stack second functional electrode inlet, and a stack second functional electrode outlet; a first functional electrode outlet manifold connected to each of the stack first functional electrode outlets; a second functional electrode inlet manifold connected to each of the stack second functional electrode inlets, the second functional electrode inlet manifold being substantially fully accommodating thermal expansion and contraction; a second functional electrode outlet manifold connected to each of the stack second functional electrode outlets, the second functional electrode outlet manifold being substantially fully accommodating thermal expansion and contraction; a containment vessel configured to removably contain at least a portion of the plurality of connected individual electrochemical cell stacks; and a containment vessel interior space that is fully dimensionally accommodating thermal expansion and contraction, the containment vessel interior space being configured to establish substantially equivalent environmental inlet conditions for each of the plurality of first functional electrode elements; and a multiple electrochemical cell stack-stack first functional electrode inlet plenum.

[0065] [Clause 2] a compression stack mount external to at least a portion of the vessel; and a thermal barrier configured to substantially thermally isolate at least a portion of the container exterior compression stack mount. [Clause 3] 13. The electrochemical cell system of claim 1 or any other clause, further comprising an electrochemical cell support manifold.

[0066] [Article 4] The electrochemical cell support manifold comprises: a first functional electrode outlet manifold stack mount; a second functional electrode inlet manifold stack mount; a second functional electrode outlet manifold stack mount; and a second functional electrode outlet manifold stack mount. [Article 5] 13. The electrochemical cell system of claim 1 or any other clause, wherein the electrochemical cell comprises a power generating electrochemical cell. [Article 6] 13. The electrochemical cell system of claim 1 or any other clause, wherein the electrochemical cell comprises a gaseous substance generating electrochemical cell.

[0067] [Article 7] 7. The electrochemical cell system of clause 6 or any other clause, further comprising a steam input. [Article 8] 8. The electrochemical cell system of clause 7 or any other clause, further comprising an electrochemical cell slide element that is substantially completely accommodating thermal expansion and contraction. [Article 9] 13. The electrochemical cell system of claim 1 or any other clause, further comprising at least one electrochemical cell stack axial flow regulator. [Article 10] 10. The electrochemical cell system of clause 9 or any other clause, wherein the at least one electrochemical cell stack axial flow conditioner comprises at least one gradient distribution plate.

[0068] [Article 11] 1. An electrochemical cell system for use in either power generation or electrolysis mode, comprising: a plurality of connected individual electrochemical cell stacks, each of the plurality of connected individual electrochemical cell stacks including a plurality of first functional electrode elements, a plurality of second functional electrode elements, a stack first functional electrode inlet, a stack first functional electrode outlet, a stack second functional electrode inlet, and a stack second functional electrode outlet; a containment vessel configured to removably contain at least a portion of the plurality of connected individual electrochemical cell stacks; 1. An electrochemical cell system comprising: a containment vessel interior space for a multiple electrochemical cell stack; a stack first functional electrode inlet plenum; and

[0069] [Article 12] The electrochemical cell system of claim 11 or any other clause, wherein the containment vessel internal space multiple electrochemical cell stack stack first functional electrode inlet plenum is configured to completely surround and contain each of the plurality of stack first functional electrode inlets, each of the plurality of stack second functional electrode inlets, and each of the plurality of stack second functional electrode outlets. [Article 13] 12. The electrochemical cell system of claim 11 or any other clause, wherein each of the first functional electrode elements comprises an oxygen electrode element and each of the second functional electrode elements comprises a fuel electrode element.

[0070] [Article 14] 14. The electrochemical cell system of claim 13 or any other claim, wherein each of said oxygen electrode elements comprises a cathode element and each of said fuel electrode elements comprises an anode element. [Article 15] 14. The electrochemical cell system of claim 13 or any other claim, wherein each of said oxygen electrode elements comprises an anode element and each of said fuel electrode elements comprises a cathode element. [Article 16] 12. The electrochemical cell system of claim 11 or any other clause, wherein each of the first functional electrode elements comprises a fuel electrode element and each of the second functional electrode elements comprises an oxygen electrode element.

[0071] [Article 17] 14. The electrochemical cell system of claim 13 or any other clause, wherein each of said anode elements comprises a cathode element and each of said anode elements comprises an anode element. [Article 18] 14. The electrochemical cell system of claim 13 or any other claim, wherein each of said oxygen electrode elements comprises an anode element and each of said fuel electrode elements comprises a cathode element.

[0072] [Article 19] a first functional electrode outlet manifold connected to each of the stack first functional electrode outlets; a second functional electrode inlet manifold connected to each of the stack second functional electrode inlets; a second functional electrode outlet manifold connected to each of the stack second functional electrode outlets; The electrochemical cell system of claim 11 or any other clause, wherein the containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum is configured to surround each of the second functional electrode inlet manifolds and the second functional outlets.

[0073] [Article 20] The electrochemical cell system of clause 19 or any other clause, wherein the second functional electrode inlet manifold and the second functional outlet manifold include manifolds that are substantially completely dimensionally accommodating for thermal expansion and contraction, and the containment vessel internal space multiple electrochemical cell stack stack first functional electrode inlet plenum includes an internal space that is completely dimensionally accommodating for thermal expansion and contraction. [Article 21] 12. The electrochemical cell system of claim 11 or any other claim, wherein the plurality of connected individual electrochemical cell stacks comprises a plurality of fluidly connected individual electrochemical cell stacks.

[0074] [Article 22] 12. The electrochemical cell system of claim 11 or any other claim, wherein the plurality of connected individual electrochemical cell stacks comprises a plurality of electrically connected individual electrochemical cell stacks. [Article 23] 12. The electrochemical cell system of claim 11 or any other claim, wherein the plurality of connected individual electrochemical cell stacks comprises a plurality of individual electrochemical cell stacks in fluid and electrical connection. [Article 24] The electrochemical cell system of claim 11 or any other clause, wherein the containment vessel internal space multiple electrochemical cell stack stack first functional electrode inlet plenum is configured to establish substantially equivalent environmental inlet conditions for each of the plurality of first functional electrode elements.

[0075] [Article 25] The electrochemical cell system of clause 241 or any other clause, further comprising a first functional electrode outlet manifold. [Article 26] 26. The electrochemical cell system of clause 25 or any other clause, wherein the first functional electrode outlet manifold comprises an electrochemical cell support outlet manifold. [Article 27] 25. The electrochemical cell system of clause 24 or any other clause, further comprising a substantially differential coefficient of thermal expansion mount. [Article 28] The electrochemical cell system of clause 27 or any other clause, wherein the substantially differential thermal expansion coefficient mount includes a stack shelf on which each of the plurality of connected individual electrochemical cell stacks is mounted.

[0076] [Article 29] 28. The electrochemical cell system of clause 27 or any other clause, wherein the substantially differential coefficient of thermal expansion mount comprises a manifold stack mount. [Article 30] The manifold stack mount comprises: a first functional electrode outlet manifold stack mount; a second functional electrode inlet manifold stack mount; 30. The electrochemical cell system of claim 29 or any other claim, comprising a manifold stack mount selected from: a first functional electrode outlet manifold stack mount; and a second functional electrode outlet manifold stack mount. [Article 31] 20. The electrochemical cell system of clause 19 or any other clause, wherein the first functional electrode outlet manifold comprises a first functional electrode outlet manifold stack mount.

[0077] [Article 32] 25. The electrochemical cell system of clause 24 or any other clause, further comprising a compression stack mount. [Article 33] The compression stack mount comprises: A compression tie rod; 33. The electrochemical cell system of claim 32 or any other claim comprising a compression element. [Article 34] 34. The electrochemical cell system of clause 33 or any other clause, wherein the compression stack mount further comprises a spring element.

[0078] [Article 35] 33. The electrochemical cell system of clause 32 or any other clause, wherein the compression stack mounts include at least a portion of the compression stack mounts external to the vessel. [Article 36] 35. The electrochemical cell system of clause 34 or any other clause, wherein the spring element comprises at least a portion of a spring element external to the container. [Article 37] 36. The electrochemical cell system of clause 35 or any other clause, further comprising a thermal barrier configured to substantially thermally isolate at least a portion of the container exterior compression stack mount.

[0079] [Article 38] 36. The electrochemical cell system of clause 35 or any other clause, wherein at least a portion of the external vessel compression stack mounts include non-hot compression stack mounts. [Article 39] 42. The electrochemical cell system of clause 41 or any other clause, further comprising a second functional electrode outlet manifold connected to each of said stack second functional electrode outlets. [Article 40] 40. The electrochemical cell system of clause 39 or any other clause, wherein the second functional electrode outlet manifold comprises interconnected second functional electrode outlet manifolds.

[0080] [Article 41] 41. The electrochemical cell system of claim 40 or any other claim, wherein the containment vessel interior space multiple electrochemical cell stack first functional electrode inlet plenum is configured to surround at least a portion of the second functional electrode outlet manifold. [Article 42] 40. The electrochemical cell system of clause 39 or any other clause, wherein the second functional electrode outlet manifold comprises a second functional electrode outlet manifold that is substantially completely accommodating for thermal expansion and contraction. [Article 43] 12. The electrochemical cell system of claim 11 or any other claim, wherein the electrochemical cell comprises a solid oxide electrochemical cell.

[0081] [Article 44] 44. The electrochemical cell system of claim 43 or any other clause, wherein the solid oxide electrochemical cell comprises a solid oxide fuel cell. [Article 45] 44. The electrochemical cell system of clause 43 or any other clause, wherein the solid oxide electrochemical cell comprises a solid oxide electrolysis cell. [Article 46] 12. The electrochemical cell system of claim 11 or any other clause, wherein the electrochemical cell comprises an electrochemical cell selected from a proton exchange membrane cell, a direct methanol cell, an alkaline cell, a phosphoric acid cell, a molten carbonate cell, a solid oxide cell, a solid oxide proton conducting cell, and a high temperature proton exchange membrane cell.

[0082] [Article 47] 12. The electrochemical cell system of claim 11 or any other claim, wherein the electrochemical cell comprises a power generating electrochemical cell. [Article 48] 12. The electrochemical cell system of claim 11 or any other claim, wherein the electrochemical cell comprises a gaseous substance generating electrochemical cell. [Article 49] A compressor and 48. The electrochemical cell system of claim 47 or any other claim, further comprising a turbine.

[0083] [Article 50] 50. The electrochemical cell system of clause 49 or any other clause, further comprising a turbine recuperator. [Article 51] 50. The electrochemical cell system of clause 49 or any other clause, further comprising a cathode recuperator. [Article 52] 50. The electrochemical cell system of clause 49 or any other clause, further comprising a desulfurizer.

[0084] [Article 53] 50. The electrochemical cell system of clause 49 or any other clause, further comprising a combustor. [Article 54] 50. The electrochemical cell system of claim 49 or any other clause, further comprising a reformer. [Article 55] 50. The electrochemical cell system of clause 49 or any other clause, further comprising an anode heat exchanger.

[0085] [Article 56] 49. The electrochemical cell system of clause 48 or any other clause, further comprising a steam input. [Article 57] 57. The electrochemical cell system of clause 56 or any other clause, further comprising a cathode recuperator. [Article 58] 57. The electrochemical cell system of clause 56 or any other clause, further comprising an anode heat exchanger.

[0086] [Article 59] The plurality of connected individual electrochemical cell stacks comprises: a stack of electrochemical cells electrically connected in series; a stack of electrochemical cells fluidly connected in series; a stack of electrochemical cells electrically connected in parallel; a stack of electrochemical cells fluidly connected in parallel; All permutations and combinations of the above, 12. The electrochemical cell system of claim 11 or any other clause comprising a plurality of connected individual electrochemical cell stacks selected from:

[0087] [Article 60] 12. The electrochemical cell system of claim 11 or any other clause, further comprising an electrochemical cell stack mount that is fully accommodating for thermal expansion and contraction. [Article 61] 61. The electrochemical cell system of clause 60 or any other clause, wherein the fully thermal expansion and contraction accommodating electrochemical cell stack mount includes roller elements. [Article 62] 61. The electrochemical cell system of clause 60 or any other clause, wherein the fully thermal expansion and contraction accommodating electrochemical cell stack mount includes a sliding element.

[0088] [Article 63] 12. The electrochemical cell system of clause 11 or any other clause, further comprising at least one electrochemical cell stack axial flow conditioner. [Article 64] 64. The electrochemical cell system of clause 63 or any other clause, wherein the at least one electrochemical cell stack axial flow conditioning device comprises at least one electrochemical cell axial flow conditioning plate. [Article 65] 65. The electrochemical cell system of clause 64 or any other clause, wherein said at least one electrochemical cell axial flow conditioning plate comprises at least one gradient distribution plate.

[0089] [Article 66] 66. The electrochemical cell system of clause 65 or any other clause, wherein said at least one gradient distribution plate comprises at least one fixed gradient distribution plate. [Article 67] 64. The electrochemical cell system of clause 63 or any other clause, wherein the at least one electrochemical cell stack axial flow conditioning device comprises a variable thickness porous material. [Article 68] 64. The electrochemical cell system of clause 63 or any other clause, wherein the at least one electrochemical cell stack axial flow conditioner comprises at least one stacked multi-screen component.

[0090] [Article 69] providing a plurality of connected individual electrochemical cell stacks, each stack of the plurality of connected individual electrochemical cell stacks having a plurality of first functional electrode elements, a plurality of second functional electrode elements, a stack first functional electrode inlet, a stack first functional electrode outlet, a stack second functional electrode inlet, and a stack second functional electrode outlet; completely enclosing the plurality of connected individual electrochemical cell stacks with a containment vessel; and placing a stack first functional electrode inlet plenum in an internal space of a containment vessel and storing the stack first functional electrode inlets therein.

[0091] [Article 70] The electrochemical cell process of claim 69 or any other claim, wherein the step of providing a containment vessel internal space multiple electrochemical cell stack stack first functional electrode inlet plenum includes a step of completely surrounding and containing each of the plurality of stack first functional electrode inlets and each of the plurality of stack second functional electrode outlets. [Article 71] 70. The electrochemical cell process of clause 69 or any other clause, wherein each of the first functional electrode elements comprises an oxygen electrode element and each of the second functional electrode elements comprises a fuel electrode element.

[0092] [Article 72] 72. The electrochemical cell process of clause 71 or any other clause wherein each of said oxygen electrode elements comprises a cathode element and each of said fuel electrode elements comprises an anode element. [Article 73] 72. The electrochemical cell process of clause 71 or any other clause wherein each of said oxygen electrode elements comprises an anode element and each of said fuel electrode elements comprises a cathode element. [Article 74] 70. The electrochemical cell process of clause 69 or any other clause, wherein each of the first functional electrode elements comprises a fuel electrode element and each of the second functional electrode elements comprises an oxygen electrode element.

[0093] [Article 75] 72. The electrochemical cell process of clause 71 or any other clause wherein each of said fuel electrode elements comprises a cathode element and each of said oxygen electrode elements comprises an anode element. [Article 76] 72. The electrochemical cell process of clause 71 or any other clause wherein each of said oxygen electrode elements comprises an anode element and each of said fuel electrode elements comprises a cathode element.

[0094] [Article 77] providing a first functional electrode outlet manifold; connecting the first functional electrode outlet manifold to each of the stack first functional electrode outlets; providing a second functional electrode inlet manifold; connecting the second functional electrode inlet manifold to each of the stack second functional electrode inlets; providing a second functional electrode outlet manifold; connecting the second functional electrode outlet manifold to each of the stack second functional electrode outlets; Alternatively, the step of providing a stack first functional electrode inlet plenum in the containment vessel interior space includes: encircling at least a portion of the second functional electrode inlet manifold; and surrounding at least a portion of the second functional electrode outlet manifold.

[0095] [Article 78] thermally expanding and contracting at least a portion of the second functional electrode inlet manifold within the containment vessel interior volume multiple electrochemical cell stack stack first functional electrode inlet plenum substantially completely and accommodatively; and thermally expanding and contracting at least a portion of the second functional electrode outlet manifold within the containment vessel internal space of the multiple electrochemical cell stack stack first functional electrode inlet plenum to substantially completely accommodate the second functional electrode outlet manifold.

[0096] [Article 79] 70. The electrochemical cell process of clause 69 or any other clause, wherein the step of providing the plurality of connected individual electrochemical cell stacks includes the step of fluidly connecting the plurality of connected individual electrochemical cell stacks. [Article 80] 70. The electrochemical cell process of clause 69 or any other clause, wherein the step of providing the plurality of connected individual electrochemical cell stacks includes the step of electrically connecting the plurality of connected individual electrochemical cell stacks.

[0097] [Article 81] The step of providing the plurality of connected individual electrochemical cell stacks comprises: fluidly connecting the plurality of connected individual electrochemical cell stacks; and electrically connecting the plurality of connected individual electrochemical cell stacks. [Article 82] The electrochemical cell process of claim 69 or any other claim, wherein the step of establishing a multiple electrochemical cell stack stack first functional electrode inlet plenum in the containment vessel interior space includes the step of establishing substantially equivalent environmental inlet conditions for each of the first functional electrode elements.

[0098] [Article 83] 83. The electrochemical cell process of clause 82 or any other clause, further comprising the step of providing a first functional electrode outlet manifold. [Article 84] The electrochemical cell process of clause 83 or any other clause, wherein the step of installing the first functional electrode outlet manifold includes supporting the electrochemical cell stack by the first functional electrode outlet manifold. [Article 85] The electrochemical cell process of clause 82 or any other clause, further comprising mounting the plurality of connected individual electrochemical cell stacks by substantially differential coefficient of thermal expansion mounts.

[0099] [Article 86] The electrochemical cell process of claim 85 or any other claim, wherein the step of mounting the plurality of connected individual electrochemical cell stacks by the substantially differential coefficient of thermal expansion mounts includes utilizing a stack shelf upon which each of the plurality of connected individual electrochemical cell stacks is mounted. [Article 87] The electrochemical cell process of claim 85 or any other claim, wherein the step of mounting the plurality of connected individual electrochemical cell stacks by the substantially differential coefficient of thermal expansion mounts includes utilizing a manifold stack mount.

[0100] [Article 88] The step of utilizing the manifold stack mount comprises: utilizing a first functional electrode outlet manifold stack mount; utilizing a second function electrode inlet manifold stack mount; Utilizing a second functional electrode outlet manifold stack mount. [Article 89] The electrochemical cell process of clause 77 or any other clause, wherein the step of installing the first functional electrode outlet manifold includes installing a first functional electrode outlet manifold stack mount.

[0101] [Article 90] 83. The electrochemical cell process of clause 82 or any other clause, further comprising the step of compressing each of the connected individual electrochemical cell stacks. [Article 91] The step of compressing each of the connected individual electrochemical cell stacks comprises: using a compression tie rod; 9. The electrochemical cell process of claim 90 or any other claim, including the step of using a compression element. [Article 92] The electrochemical cell process of clause 91 or any other clause, wherein the step of using a compression element includes the step of using a spring element.

[0102] [Article 93] 91. The electrochemical cell process of claim 90 or any other claim, wherein compressing each of the connected individual electrochemical cell stacks comprises at least partially compressing each of the connected individual electrochemical cell stacks outside of a container. [Article 94] The electrochemical cell process of clause 92 or any other clause, wherein the step of using a spring element includes using a spring element external to at least a portion of the vessel. [Article 95] The electrochemical cell process of claim 93 or any other clause, further comprising the step of substantially thermally isolating the containment vessel interior space from a multiple electrochemical cell stack stack first functional electrode inlet plenum during the step of at least partially compressing each of the connected individual electrochemical cell stacks external to the containment vessel.

[0103] [Article 96] 94. The electrochemical cell process of claim 93 or any other claim, wherein the step of at least partially ex-container compressing each of the connected individual electrochemical cell stacks comprises non-hot compressing each of the connected individual electrochemical cell stacks. [Article 97] 83. The electrochemical cell process of clause 82 or any other clause, further comprising the step of providing a second functional electrode outlet manifold. [Article 98] The electrochemical cell process of clause 97 or any other clause, wherein the step of providing a second function electrode outlet manifold includes using an electrochemical cell stack interconnected second function electrode outlet manifold.

[0104] [Article 99] The electrochemical cell process of claim 98 or any other clause, wherein the step of providing a first functional electrode inlet plenum in the containment vessel interior space includes a step of encircling at least a portion of the second functional electrode outlet manifold. [Article 100] The electrochemical cell process of claim 69 or any other claim, wherein the step of installing the second functional electrode outlet manifold includes a step of thermally expanding and contracting the second functional electrode outlet manifold to be substantially completely contained within the containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum.

[0105] [Article 101] 70. The electrochemical cell process of clause 69 or any other clause, wherein the step of providing a plurality of connected individual electrochemical cell stacks comprises providing a plurality of connected individual solid oxide electrochemical cell stacks. [Article 102] 102. The electrochemical cell process of claim 101 or any other claim, wherein providing the plurality of connected individual solid oxide electrochemical cell stacks comprises providing a plurality of connected individual solid oxide fuel cell stacks. [Article 103] 102. The electrochemical cell process of claim 101 or any other claim, wherein providing the plurality of connected individual solid oxide electrochemical cell stacks comprises providing a plurality of connected individual solid oxide electrolysis cell stacks.

[0106] [Article 104] 70. The electrochemical cell process of claim 69 or any other clause, wherein the step of providing a plurality of connected individual electrochemical cell stacks includes providing a plurality of connected individual electrochemical cell stacks selected from proton exchange membrane cell stacks, direct methanol cell stacks, alkaline cell stacks, phosphoric acid cell stacks, molten carbonate cell stacks, solid oxide cell stacks, solid oxide proton conducting cells, and high temperature proton exchange membrane cell stacks. [Article 105] 70. The electrochemical cell process of claim 69 or any other claim, wherein the step of providing a plurality of connected individual electrochemical cell stacks comprises providing a plurality of power generating electrochemical cell stacks.

[0107] [Article 106] 70. The electrochemical cell process of claim 69 or any other claim, wherein the step of providing a plurality of connected individual electrochemical cell stacks comprises providing a plurality of gaseous substance producing electrochemical cell stacks. [Article 107] Utilizing a compressor in part of the process; Utilizing a turbine in a portion of the process.

[0108] [Article 108] The electrochemical cell process of clause 107 or any other clause, further comprising utilizing a turbine recuperator in a portion of the process. [Article 109] The electrochemical cell process of clause 107 or any other clause, further comprising utilizing a cathode recuperator in a portion of the process. [Article 110] The electrochemical cell process of clause 107 or any other clause, further comprising utilizing a desulfurizer in a portion of the process.

[0109] [Article 111] The electrochemical cell process of clause 107 or any other clause, further comprising utilizing a combustor in a portion of the process. [Article 112] The electrochemical cell process of clause 107 or any other clause, further comprising utilizing a reformer in a portion of the process. [Article 113] 108. The electrochemical cell process of claim 107 or any other claim, further comprising the step of utilizing an anode heat exchanger in a portion of the process.

[0110] [Article 114] 109. The electrochemical cell process of claim 108 or any other claim, further comprising utilizing a steam input in a portion of the process. [Article 115] The electrochemical cell process of claim 114 or any other claim, further comprising the step of utilizing a cathode recuperator in a portion of the process. [Article 116] 115. The electrochemical cell process of claim 114 or any other claim, further comprising the step of utilizing an anode heat exchanger in a portion of the process.

[0111] [Article 117] The step of providing the plurality of connected individual electrochemical cell stacks comprises: providing a series-connected electrochemical cell stack; providing a series fluidly connected electrochemical cell stack; providing a stack of electrochemical cells electrically connected in parallel; providing a parallel fluidly connected electrochemical cell stack; All the above permutations and combinations; 70. The electrochemical cell process of claim 69 or any other claim, comprising a step selected from:

[0112] [Article 118] 70. The electrochemical cell process of claim 69 or any other clause, further comprising the step of thermally expanding and contracting the plurality of connected individual electrochemical cell stacks substantially completely contained within the containment vessel interior space multiple electrochemical cell stack stack first functional electrode inlet plenum. [Article 119] The electrochemical cell process of claim 118 or any other clause, wherein the step of thermally expanding and contracting to accommodate substantially completely the plurality of connected individual electrochemical cell stacks within the containment vessel interior space includes rolling components within the containment vessel.

[0113] [Article 120] The electrochemical cell process of claim 118 or any other clause, wherein the step of thermally expanding and contracting within the containment vessel interior space to accommodate substantially all of the plurality of connected individual electrochemical cell stacks includes the step of sliding components within the containment vessel. [Article 121] 70. The electrochemical cell process of clause 69 or any other clause, further comprising the step of establishing a differential axial flow in at least one electrochemical cell stack.

[0114] [Article 122] The electrochemical cell process of claim 121 or any other claim, wherein the step of establishing a differential axial flow in at least one electrochemical cell stack includes utilizing at least one electrochemical cell axial flow conditioning plate. [Article 123] 123. The electrochemical cell process of claim 122 or any other claim, wherein the step of utilizing at least one electrochemical cell axial flow conditioning plate includes utilizing at least one gradient distribution plate. [Article 124] 124. The electrochemical cell process of claim 123 or any other claim, wherein the step of utilizing at least one gradient distribution plate includes the step of utilizing at least one fixed gradient distribution plate.

[0115] [Article 125] The electrochemical cell process of claim 121 or any other claim, wherein the step of establishing a differential axial flow in at least one electrochemical cell stack includes utilizing a variable thickness porous material. [Article 126] The electrochemical cell process of claim 121 or any other claim, wherein said step of establishing a differential axial flow in at least one electrochemical cell includes utilizing at least one stacked multi-screen component.

[0116] As can be readily understood from the foregoing, the basic concept of the various embodiments of the present invention can be embodied in a variety of ways, including both the integrated solid oxide fuel cell-gas turbine technology and the apparatus for achieving the appropriate integrated solid oxide fuel cell-gas turbine. In this application, the integrated solid oxide fuel cell-gas turbine technology is disclosed as part of the results shown to be achieved by the various apparatus described, and as steps inherent in the utilization. These are merely natural results of utilizing the apparatus as intended and described. Furthermore, while several apparatuses are disclosed, it should be understood that these do not only achieve a particular method, but can be varied in many ways. Importantly, with respect to all of the foregoing, it should be understood that all of these aspects are encompassed by the present disclosure.

[0117] The discussion contained in this application is intended to serve as a basic description. The reader should be aware that the specific discussion may not explicitly describe all possible embodiments, and many alternatives are implicitly described. It may also not fully describe the general nature of various embodiments of the invention, and may not explicitly indicate that each feature or element may actually represent a broader function or a wide variety of alternative or equivalent elements. By way of example, terms of degree, approximation, and / or relative terms may be used. These include words such as "substantially," "about," and "only." These words and word types are understood in their dictionary sense as terms that encompass a sufficient or significant amount, quantity, size, and the like, and terms that encompass most, but not the entirety, of what is specified. Furthermore, when terms of degree, approximation, and / or relative terms such as "substantially" are used or are used in this application, they should be understood to encompass more precise, even quantitative values, including various levels of precision, and the potential for claims that address multiple quantitative options and alternatives. For example, the existence of a condition of substantially perfect inflation-deflation compatibility in the final range of use can be specified using percentage values ​​including 99%, 97%, 95%, or 90% of the specified compatibility or condition. Again, these are implicitly included in this disclosure and should (and are believed to) be understood by those skilled in the art. Furthermore, if this application is written in apparatus-oriented terms, each element of the apparatus implicitly performs a function. Not only are apparatus claims included for the described apparatus, but method or process claims may also be included to address the functionality of the embodiment and the functions performed by each element. Nothing in this specification or language is intended to limit the scope of claims that may be included in a subsequent patent application.

[0118] It should also be understood that various modifications may be made without departing from the essence of the various embodiments of the present invention. Such modifications are also implicitly included in this specification. They remain within the scope of the various embodiments of the present invention. The broad disclosure, including the explicit embodiments shown, the wide variety of implicit alternative embodiments, and the broad methods or processes, etc., is encompassed by this disclosure and may be relied upon when drafting the claims of a subsequent patent application. It should be understood that such changes in language and broader or more detailed claims may be achieved at a later date (such as by the required deadline) or if the applicant subsequently seeks a patent application based on this application. With this understanding, the reader should appreciate that the present disclosure is understood to support a subsequently filed patent application that may seek examination of the broadest claims possible within the applicant's rights and may be designed to obtain a patent covering multiple aspects of the embodiments of the present invention, both alone and as an overall system.

[0119] Moreover, each of the various elements of the embodiments of the invention and claims can also be achieved in various ways. Moreover, when an element is used or implied, it should be understood that the element encompasses individual structures as well as multiple structures that may or may not be physically connected. The present disclosure should be understood to encompass each such variation, whether it is a variation of any apparatus embodiment, a variation of a method or process embodiment, or simply a variation of any of these elements. In particular, since the present disclosure is directed to elements of the various embodiments of the invention, it should be understood that the terms of each element may be expressed by equivalent apparatus terms or method terms, and only the function or result may be the same. Such equivalent terms, broader terms, or more general terms should be considered to be encompassed in the description of each element or action. Such terms can be substituted as necessary to make clear the broad scope of the implicit application of the embodiments of the invention. By way of example, it should be understood that all actions can be expressed as a means for performing that action or as an element that causes that action. Similarly, each physical element disclosed should be understood to encompass a disclosure of the action that the physical element facilitates. With regard to this last aspect, as an example, the disclosure of a "compressor" should be understood to encompass the disclosure of the act of "compressing," whether or not it is explicitly discussed, and conversely, if the act of "compressing" were effectively disclosed, such disclosure should be understood to encompass the disclosure of a "compressor" and even a "means for compressing." Such variations and alternative terms are to be understood as expressly included herein. Moreover, each such means (whether or not explicitly described as such) should be understood to encompass all elements capable of performing a given function, and all descriptions of elements performing a described function should be understood as non-limiting examples of means for performing that function.As another non-limiting example, elements of the claims should be understood to also be expressed as either components, programming, subroutines, logic, or elements that provide, or are configured to provide, or are configured and arranged to provide, a particular result, application, objective, situation, function, or operation, or as components that are capable of accomplishing a particular activity, result, application, objective, situation, function, or operation, or as components, programming, subroutines, logic, or elements that are configured and arranged to accomplish a particular activity, result, application, objective, situation, function, or operation, all of which should be understood to be within the scope of this disclosure and this specification.

[0120] Any patents, publications, or other documents mentioned in this patent application are hereby incorporated by reference. Any priority cases claimed by this application are attached hereto and incorporated by reference. Furthermore, for each term used, it is to be understood that a common dictionary definition is incorporated for each term, unless its use in this application is inconsistent with a widely held interpretation, and all definitions, alternative terms, and synonyms as contained in the Random House Webster's "Unabridged Dictionary," Second Edition, are incorporated herein by reference. Finally, all references listed in any reference list or other information statement submitted with this application are attached hereto and incorporated by reference. However, in each of the above, it is expressly stated that to the extent that such information or statements incorporated by reference may be deemed inconsistent with the patenting of various embodiments of the invention, such statements shall not be deemed to have been made by the applicant.

[0121] [List of References Incorporated by Reference] I. U.S. Patents Patent Number Patent Owner 10644331 Boeing Company 6641084 Boeing Company 6834831 Samco Corporation 7380749 Boeing Company 7410713 General Electric Company 7966830 Boeing Company 8016228 Boeing Company 6213234 Capstone Green Energy Corporation 6230494 APPTIVE TECHNOLOGIES LIMITED. 6609582 Delphi Technologies Inc. 6655235 CommScope EMEA Limited CommScope Technologies LLC 7743861 Delphi Technologies Inc. 5449568 United States Department of Energy 6365290 Fuel Cell Energy Inc. 5968680 Honeywell International Inc. Hybrid Power Generation Systems, LLC 7153599 General Electric Company 7595124 General Electric Company 7118818 LG Fuel Cell Systems, Inc. 9570766 LG Electronics Inc. 9666885 LG Electronics Inc. 10107190 Mitsubishi Power Limited 10490832 Mitsubishi Power Limited 10533495 Mitsubishi Power Limited 10804549 Mitsubishi Power Limited 10914233 Mitsubishi Power Limited 9422862 Mitsubishi Power Limited 9482110 Mitsubishi Power Limited 9482159 Mitsubishi Power Limited 9638102 Mitsubishi Power Limited 9768454 Mitsubishi Power Limited 9777629 Mitsubishi Power Limited 9806358 Mitsubishi Power Limited 9831505 Mitsubishi Power Limited 9926844 Mitsubishi Power Limited 9945265 Mitsubishi Power Limited 9979033 Mitsubishi Power Limited 7781115 Siemens Energy Inc. 5413879 Siemens AG 5532573 Westinghouse Electric Company LLC 5955039 Siemens Energy Inc. 6255010 Siemens Energy Inc. 7709118 Siemens Energy Inc. 5693201 ZTEK Corporation 5948221 ZTEK Corporation 5976332 ZTEK Corporation 5413879 Domelacchi et al. 5449568 Micheli et al. 5532573 Brown et al. 5693201 Sue et al. 5948221 Sue 5955039 Dowdy 5968680 Wolf et al. 5976332 Sue et al. 6213234 Rosen et al. 6230494 Botti et al. 6255010 George et al. 6365290 Gesell-Ayag et al. 6609582 Botti et al. 6641084 Huber et al. 6655235 Botti et al. 6834831 Daggett 7118818 Agnew et al. 7153599 Bunker et al. 7380749 Hucke et al. 7410713 Baran et al. 7595124 Varadarajan et al. 7709118 Lundberg 7743861 Greeve 7781115 Lundberg 7966830 Daggett 8016228 Hucke et al. 9422862 Ozawa 9482110 Ozawa 9482159 Ozawa 9570766 Bozzolo et al. 9638102 Kobayashi et al. 9666885 Bozzolo et al. 9768454 Nagaie et al. 9777629 Nakamoto et al. 9806358 Nakamoto et al. 9831505 Nakamoto et al. 9926844 Fujita 9945265 Nakamoto et al. 9979033 Manabe et al. 10107190 Manabe et al. 10490832 Manabe et al. 10533495 Nakamoto et al. 10644331 Stoia et al. 10804549 Nakamoto et al. 10914233 Manabe et al.

[0122] II. Non-Patent Literature U.S. Provisional Patent Application No. 63 / 297525, filed January 7, 2022. The first inventor is named Ector.

[0123] Accordingly, applicants should be understood to have support to assert and claim embodiments that include at least the following: i) each of the integrated solid oxide fuel cell-gas turbine apparatuses disclosed and described herein; ii) related methods disclosed and described; iii) similar, equivalent, and even implicit variations of each of these apparatus and methods; iv) alternative designs thereof that accomplish each of the functions shown as disclosed and described; v) alternative designs and methods that accomplish each function shown as implicit to accomplish what is disclosed and described; vi) each feature, component, and step shown as a separate and independent invention; and vii) the various systems disclosed. or components; viii) uses enhanced by such processes, methods, systems, or components; ix) each system, method, element shown or described as applied to a particular field or apparatus; x) methods and apparatus substantially as described herein and illustrated with reference to any of the accompanying examples; xi) apparatus for performing the methods described herein, including means for performing the steps; xii) various combinations and permutations of each disclosed element; xiii) each claim or concept potentially dependent as a dependency on each one of the independent claims or concepts presented; and xiv) all inventions described herein.

[0124] Further, with respect to computer aspects, and aspects amenable to programming or other electronic automation, in characterizing those and all other aspects of the various embodiments of the present invention, whether characterized as devices, capabilities, elements, or otherwise, should be understood as all of these may be implemented via software, hardware, or firmware structures, such as configured to a general purpose computer, a programmed chip or chipset, an ASIC, an application specific controller, subroutines, logic, or other known programmable or circuit specific structures, and all such aspects should be understood to be defined at least by structures including hardware circuits, firmware, programmed application specific components, and a general purpose computer programmed to accomplish the identified aspect, as will be well recognized by those skilled in the art. For such items implemented by programmable functionality, applicant should be understood to have support to claim and state at least the following inventions: xv) a process executed with the aid of or on a computer, machine, or computing machine as described throughout the above discussion, xvi) a programmable apparatus as described throughout the above discussion, xvii) a computer readable memory encoded with data for instructing a computer comprising means or elements that function as described throughout the above discussion, xviii) a computer, machine, or computing machine configured as disclosed and described herein, xix) each or a combination of subroutines, processor logic, and / or programs as disclosed and described herein, xx) a carrier medium carrying computer readable code for controlling a computer to perform each of the methods described herein or in any claim, separately, separately and in combination, xxi) a computer program for performing each of the methods disclosed, separately, separately, xxii) a computer program including all and each combination of means for performing each of the steps disclosed, separately and in combination, xxiii) a storage medium for storing each of the computer programs disclosed.xxiv) signals carrying the disclosed computer programs; xxv) processors executing instructions that operate to achieve the specified steps and activities; xxvi) circuitry (including configurations of transistors, gates, etc.) that operates to sequence and / or cause actions as detailed; xxvii) computer readable media that store instructions to perform the specified steps and activities; xxviii) related methods disclosed and described; xxix) similar, equivalent, and even implicit variations of each of these systems and methods; xxx) alternative designs thereof that achieve each of the indicated functions as disclosed and described; xxxi) alternative designs and methods thereof that achieve each of the indicated functions implicitly to achieve what is disclosed and described; xxxii) each feature, component, and step shown as a separate and independent invention; and xxxiii) various combinations of each and any of the above, without limiting other aspects.

[0125] With respect to claims now or later presented for examination, it should be understood that for practical reasons and to avoid a significant expansion of the examination burden, applicants may at any time present only the first claim, or only the first claim with perhaps only the first dependency. Our firm and third parties interested in the potential scope of this or any subsequent application should understand that broader claims may be presented at a later date in this application, any application claiming the benefit of this application, or any continuing application, notwithstanding any preliminary amendment, other amendment, claim language, or arguments presented, and thus there is no intention to abandon or surrender any potential subject matter throughout the pendency of the litigation. It should be understood that if or when broader claims are presented, to the extent that amendments, claim language, or arguments presented in this or any subsequent application are deemed to have been made to avoid that prior art, it may be necessary to reconsider any relevant prior art previously considered, since such reasons may be precluded by the later presented claims, etc. Examiners, as well as those interested in existing or later potential coverage, or those considering whether there has ever been a suggestion of a surrender or possible surrender of potential coverage, should recognize that no such surrender or disclaimer is intended and exists in this or any subsequent application. Restrictions such as those created in Hakim v. Cannon Avent Group, PLC, 479 F.3d 1313 (Fed. Cir 2007), etc., are expressly not intended in this or any subsequent related matter. Furthermore, it should be understood that there is a degree of support required under new matter law, including but not limited to EPC § 123(2) and 35 U.S.C. § 132 or other laws, to permit various dependencies or other elements presented under one independent claim or concept to be added as dependencies or elements under other independent claims or concepts. It should also be understood that in drafting the claims, whether in this or any subsequent application, applicant intends to capture as complete and broad a coverage as is legally available.To the extent that insubstantial substitutions are made, to the extent that applicant has not in fact drafted the claims to literally encompass certain embodiments, and to other applicable extents, applicant should not be understood to have in any way intended or actually waived such inclusion, because applicant may simply not have been able to foresee all eventualities, and one of ordinary skill in the art should not be reasonably expected to have drafted the claims to literally encompass such alternative embodiments.

[0126] Additionally, the transitional terms "comprising," "including," "containing," "characterized by," and "having," where used, are used to maintain "open-ended" claims herein in accordance with traditional claim interpretation, including that discussed in MPEP § 2111.03. Thus, unless the context otherwise requires, the terms "comprise" or "comprises" or "comprising," variations thereof, such as "include" or "including," variations thereof, such as "contain" or "contains" and "containing," variations thereof, such as "characterizing by" or "characterizing by," variations thereof, such as "have" or "having," and variations thereof, should be understood to mean the inclusion of a stated element or step or group of elements or steps, but not the exclusion of other elements or steps or group of elements or steps. Such terms should be interpreted in the broadest manner so as to afford the applicant the broadest scope legally permissible. The phrase "or any other claim" is used to support a claim that is dependent on other claims, such as other dependent claims, other independent claims, earlier-filed claims, later-filed claims, etc. As a clarifying example, if a claim is dependent on "claim 9 or any other claim," etc., it could be re-drafted to be dependent on claim 1, claim 8, or even claim 11 (if such claims exist) if desired and still fit within the present disclosure. It should be understood that this language also provides support for any combination of elements in the claims, and may even incorporate any desired appropriate predicate basis for particular claim combinations, such as combinations of method, apparatus, process, etc. claims.

[0127] Finally, the claims as set forth at any point shall be incorporated herein by reference as part of this specification for the various embodiments of this application, and Applicant expressly reserves the right to use all or a portion of the incorporated content of such claims as additional description in support of the claims or any or all of their elements or components, and Applicant further expressly reserves the right to move any or all of the incorporated content of such claims or any of their elements or components from this specification to the claims, or vice versa, as necessary to define the subject matter for which protection is sought by this application or by any subsequent continuation, divisional or continuation-in-part application, or to obtain the benefit of, or obtain a fee reduction under, or comply with, the patent laws, rules or regulations of any country or treaty, and such incorporated content by reference shall survive the entire term of this application, including any subsequent continuation, divisional, continuation-in-part, or reissue or extension.

Claims

1. 1. An electrochemical cell system for use in either power generation or electrolysis mode, comprising: a plurality of connected individual electrochemical cell stacks, each of the plurality of connected individual electrochemical cell stacks including a plurality of first functional electrode elements, a plurality of second functional electrode elements, a stack first functional electrode inlet, a stack first functional electrode outlet, a stack second functional electrode inlet, and a stack second functional electrode outlet; a first functional electrode outlet manifold connected to each of the stack first functional electrode outlets; a second functional electrode inlet manifold connected to each of the stack second functional electrode inlets, the second functional electrode inlet manifold being substantially fully accommodating thermal expansion and contraction; a second functional electrode outlet manifold connected to each of the stack second functional electrode outlets, the second functional electrode outlet manifold being substantially fully accommodating thermal expansion and contraction; a containment vessel configured to removably contain at least a portion of the plurality of connected individual electrochemical cell stacks; and a containment vessel interior space that is fully dimensionally accommodating thermal expansion and contraction and configured to establish substantially identical environmental inlet conditions for each of said plurality of first functional electrode elements.

2. at least a portion of the vessel exterior compression stack mount; 10. The electrochemical cell system of claim 1, further comprising: a thermal barrier configured to substantially thermally isolate at least a portion of the container exterior compression stack mount.

3. 10. The electrochemical cell system of claim 1 further comprising an electrochemical cell support manifold.

4. The electrochemical cell support manifold comprises: a first functional electrode outlet manifold stack mount; a second functional electrode inlet manifold stack mount; a second functional electrode outlet manifold stack mount; and a second functional electrode outlet manifold stack mount.

5. 2. The electrochemical cell system according to claim 1, wherein the electrochemical cells include power generating electrochemical cells.

6. 2. The electrochemical cell system of claim 1, wherein the electrochemical cell comprises a gaseous substance producing electrochemical cell.

7. 7. The electrochemical cell system of claim 6 further comprising a steam input.

8. 8. The electrochemical cell system of claim 7 further comprising an electrochemical cell slide element that is substantially completely accommodating thermal expansion and contraction.

9. 10. The electrochemical cell system of claim 1 further comprising at least one electrochemical cell stack axial flow conditioner.

10. 10. The electrochemical cell system of claim 9, wherein said at least one electrochemical cell stack axial flow control device comprises at least one gradient distribution plate.

11. 1. An electrochemical cell system for use in either power generation or electrolysis mode, comprising: a plurality of connected individual electrochemical cell stacks, each of the plurality of connected individual electrochemical cell stacks including a plurality of first functional electrode elements, a plurality of second functional electrode elements, a stack first functional electrode inlet, a stack first functional electrode outlet, a stack second functional electrode inlet, and a stack second functional electrode outlet; a containment vessel configured to removably contain at least a portion of the plurality of connected individual electrochemical cell stacks; a containment vessel interior space; a multi-electrochemical cell stack; and a stack first functional electrode inlet plenum.

12. 12. The electrochemical cell system of claim 11, wherein each of said first functional electrode elements comprises an oxygen electrode element and each of said second functional electrode elements comprises a fuel electrode element.

13. 13. The electrochemical cell system of claim 12 further comprising a manifold that is substantially completely dimensionally accommodating for thermal expansion and contraction, wherein said containment vessel internal space multiple electrochemical cell stack stack first functional electrode inlet plenum comprises an internal space that is completely dimensionally accommodating for thermal expansion and contraction.

14. 12. The electrochemical cell system of claim 11, wherein said containment vessel interior multi-electrochemical cell stack-stack first functional electrode inlet plenum is configured to establish substantially identical environmental inlet conditions for each of said plurality of first functional electrode elements.

15. 15. The electrochemical cell system of claim 14 further comprising a first functional electrode outlet manifold.

16. 15. The electrochemical cell system of claim 14 further comprising a substantially differential coefficient of thermal expansion mount.

17. 15. The electrochemical cell system of claim 14 further comprising a compression stack mount.

18. 20. The electrochemical cell system of claim 17, wherein the compression stack mounts include at least a portion of an exterior container compression stack mount.

19. 20. The electrochemical cell system of claim 18, wherein the at least a portion of the external-container compression stack mount comprises an at least a portion of the external-container spring element.

20. 20. The electrochemical cell system of claim 18, further comprising a thermal barrier configured to substantially thermally isolate at least a portion of the enclosure exterior compression stack mount.

21. 12. The electrochemical cell system of claim 11, wherein the electrochemical cell comprises an electrochemical cell selected from a proton exchange membrane cell, a direct methanol cell, an alkaline cell, a phosphoric acid cell, a molten carbonate cell, a solid oxide cell, a solid oxide proton conducting cell, and a high temperature proton exchange membrane cell.

22. 12. The electrochemical cell system of claim 11 further comprising an electrochemical cell stack mount that is fully accommodating for thermal expansion and contraction.

23. 12. The electrochemical cell system of claim 11 further comprising at least one electrochemical cell stack axial flow conditioner.

24. providing a plurality of connected individual electrochemical cell stacks, each stack of the plurality of connected individual electrochemical cell stacks having a plurality of first functional electrode elements, a plurality of second functional electrode elements, a stack first functional electrode inlet, a stack first functional electrode outlet, a stack second functional electrode inlet, and a stack second functional electrode outlet; completely enclosing the plurality of connected individual electrochemical cell stacks with a containment vessel; and providing a multiple electrochemical cell stack-stack first functional electrode inlet plenum within a containment vessel interior space and storing the multiple stack first functional electrode inlets therein.

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