Abstract: An example method of decontaminating a fuel reactant stream for a fuel cell flows the fuel reactant stream through a fluidized ammonia dissolving media, while simultaneously flowing water through the fluidized ammonia dissolving media to separate contaminants from the fuel reactant stream into a separated contaminant and water stream. The separated contaminant and water stream from the fluidized bed is accumulated within an accumulator, circulated through a water-control loop, and decontaminated by flowing the stream through an ion exchange bed secured in fluid communication with the water-control loop. A decontaminated water stream from the ion exchange bed is circulated back through the ammonia dissolving media. A temperature of the fuel reactant stream is controlled upstream of the fuel reactant stream entering the separator scrubber to produce a predetermined temperature of the fuel reactant stream passing through the separator scrubber.

Abstract: A reformer system (11) having a hydrodesulfurizer (12) provides desulfurized natural gas feedstock to a catalytic steam reformer (16), the outflow of which is treated by a water gas shift reactor (20) and optionally a preferential CO oxidizer (58) to provide reformate gas (28, 28a) having high hydrogen and moderate carbon dioxide content. To avoid damage to the hydrodesulfurizer from overheating, any deleterious hydrogen reactants, such as the oxygen in peak shave gas or olefins, in the non-desulfurized natural gas feedstock (35) are reacted (38) with hydrogen (28, 28a; 71) to convert them to alkanes (e.g., ethylene and propylene to ethane and propane) and to convert oxygen to water in a catalytic reactor (38) having no sulfide sorbent, and cooled (46), below a temperature which would damage the reactor, by evaporative cooling with pressurized hot water (42). Hydrogen for the desulfurizer and the hydrogen reactions may be provided as recycle reformate (28, 28a) or from a mini-CPO (67), or from other sources.

Abstract: An example method of decontaminating a fuel reactant stream for a fuel cell flows the fuel reactant stream through a fluidized ammonia dissolving media, while simultaneously flowing water through the fluidized ammonia dissolving media to separate contaminants from the fuel reactant stream into a separated contaminant and water stream. The separated contaminant and water stream from the fluidized bed is accumulated within an accumulator, circulated through a water-control loop, and decontaminated by flowing the stream through an ion exchange bed secured in fluid communication with the water-control loop. A decontaminated water stream from the ion exchange bed is circulated back through the ammonia dissolving media. A temperature of the fuel reactant stream is controlled upstream of the fuel reactant stream entering the separator scrubber to produce a predetermined temperature of the fuel reactant stream passing through the separator scrubber.

Abstract: A fluidized contaminant separator and water-control loop (10) decontaminates a fuel reactant stream of a fuel cell (12). Water passes over surfaces of an ammonia dissolving media (61) within a fluidized bed (62) while the fuel reactant stream simultaneously passes over the surfaces to dissolve contaminants from the fuel reactant stream into a separated contaminant and water stream. A fuel-control heat exchanger (57) upstream from the scrubber (58) removes heat from the fuel stream. A water-control loop (78) directs flow of the separated contaminants and water stream from an accumulator (68) through an ion exchange bed (88) which removes contaminants from the stream. Decontaminated water is directed back into the scrubber (58) to flow through the fluidized bed (62). Separating contaminants from the fuel reactant stream and then isolating and concentrating the separated contaminants within the ion exchange material (88) minimizes costs and maintenance requirements.

Abstract: A sodium chloride electrolysis cell (9) receives a portion of its electrical power (47, 48: 50, 51) from a phosphoric acid fuel cell (44) which receives fuel at its anode inlet (43) from a water cooled catalytic reactor (26) that converts oxygen in the byproduct output (19) of the sodium chlorate electrolysis cell to hydrogen and water. A utility grid (53) may provide through a converter (55) power to support the electrochemical process in the sodium chlorate electrolysis cell. Temperature of the water cooled catalytic reactor is determined by the vaporization of pressurized hot water, the pressure of which may be adjusted by a controller (36) and a valve (38) in response to temperature (40).

Abstract: An integrated contaminant separator and water-control loop (10) decontaminates a fuel reactant stream of a fuel cell (12). Water passes over surfaces of an ammonia dissolving means (61) within a separator scrubber (58) while the fuel reactant stream simultaneously passes over the surfaces to dissolve contaminants from the fuel reactant stream into the water. An accumulator (68) collects the separated contaminant stream, and ion exchange material (69) integrated within the accumulator removes contaminants from the stream. A water-control pump (84) directs flow of a de-contaminated water stream from the accumulator (68) through a water-control loop (78) having a heat exchanger (86) and back onto the scrubber (58) to flow over the packed bed (62). Separating contaminants from the fuel reactant stream and then isolating and concentrating the separated contaminants within the ion exchange material (69) minimizes cost and maintenance requirements.

Abstract: A reformer system (11) having a hydrodesulfurizer (12) provides desulfurized natural gas feedstock to a catalytic steam reformer (16), the outflow of which is treated by a water gas shift reactor (20) and optionally a preferential CO oxidizer (58) to provide reformate gas (28, 28a) having high hydrogen and moderate carbon dioxide content. To avoid damage to the hydrodesulfurizer from overheating, any deleterious hydrogen reactants, such as the oxygen in peak shave gas or olefins, in the non-desulfurized natural gas feedstock (35) are reacted (38) with hydrogen (28, 28a; 71) to convert them to alkanes (e.g., ethylene and propylene to ethane and propane) and to convert oxygen to water in a catalytic reactor (38) having no sulfide sorbent, and cooled (46), below a temperature which would damage the reactor, by evaporative cooling with pressurized hot water (42). Hydrogen for the desulfurizer and the hydrogen reactions may be provided as recycle reformate (28, 28a) or from a mini-CPO (67), or from other sources.

Abstract: A fluidized contaminant separator and water-control loop (10) decontaminates a fuel reactant stream of a fuel cell (12). Water passes over surfaces of an ammonia dissolving media (61) within a fluidized bed (62) while the fuel reactant stream simultaneously passes over the surfaces to dissolve contaminants from the fuel reactant stream into a separated contaminant and water stream. A fuel-control heat exchanger (57) upstream from the scrubber (58) removes heat from the fuel stream. A water-control loop (78) directs flow of the separated contaminants and water stream from an accumulator (68) through an ion exchange bed (88) which removes contaminants from the stream. Decontaminated water is directed back into the scrubber (58) to flow through the fluidized bed (62). Separating contaminants from the fuel reactant stream and then isolating and concentrating the separated contaminants within the ion exchange material (88) minimizes costs and maintenance requirements.

Abstract: A sodium chlorate electrolysis cell (9) receives a portion of its electrical power (47, 48; 50, 51) from a phosphoric acid fuel cell (45) which receives fuel at its anode inlet (43) from a water cooled catalytic reactor (26) that converts oxygen in the byproduct output (21) of the sodium chlorate electrolysis cell to hydrogen and water. A utility grid (53) may provide through a converter (55) power to support the electrochemical process in the sodium chlorate electrolysis cell. Temperature of the water cooled catalytic reactor is determined by the vaporization of pressurized hot water, the pressure of which may be adjusted by a controller (36) and a valve (38) in response to temperature (40).

Abstract: An integrated contaminant separator and water-control loop (10) decontaminates a fuel reactant stream of a fuel cell (12). Water passes over surfaces of an ammonia dissolving means (61) within a separator scrubber (58) while the fuel reactant stream simultaneously passes over the surfaces to dissolve contaminants from the fuel reactant stream into the water. An accumulator (68) collects the separated contaminant stream, and ion exchange material (69) integrated within the accumulator removes contaminants from the stream. A water-control pump (84) directs flow of a de-contaminated water stream from the accumulator (68) through a water-control loop (78) having a heat exchanger (86) and back onto the scrubber (58) to flow over the packed bed (62). Separating contaminants from the fuel reactant stream and then isolating and concentrating the separated contaminants within the ion exchange material (69) minimizes cost and maintenance requirements.

Abstract: A reformer system (11) having a hydrodesulfurizer (12) provides desulfurized natural gas feedstock to a catalytic steam reformer (16), the outflow of which is treated by a water gas shift reactor (20) and optionally a preferential CO oxidizer (58) to provide reformate gas (28, 28a) having high hydrogen and moderate carbon dioxide content. To avoid damage to the hydrodesulfurizer from overheating, any deleterious hydrogen reactants, such as the oxygen in peak shave gas or olefins, in the non-desulfurized natural gas feedstock (35) are reacted (38) with hydrogen (28, 28a; 71) to convert them to alkanes (e.g., ethylene and propylene to ethane and propane) and to convert oxygen to water in a catalytic reactor (38) cooled (46), below a temperature which would damage the reactor, by evaporative cooling with pressurized hot water (42). Hydrogen for the desulfurizer and the hydrogen reactions may be provided as recycle reformate (28, 28a) or from a mini-CPO (67), or from other sources.

Abstract: An integrated fuel cell stack assembly (26) and selective oxidizer bed assembly (200) is provided. The fuel cell stack assembly (26) also includes a number of fuel cells. A fuel inlet manifold (22) and fuel inlet plenum to cell stack (38) manifold are arranged in fluid communication with the fuel stack assembly (26) for supplying to and exhausting from, respectively, the fuel supply in the fuel cells in the fuel stack assembly (26). The bed resides in said fuel inlet manifold. The bed includes a selective oxidation catalyst with a heat exchange fluid conduit routed therethrough. Oxygen-containing gas is supplied into the bed via the input plenum. The temperature of the internal selective oxidizer bed is controlled by the fluid conduit in the bed to reduce carbon monoxide in the fuel.

Abstract: A process gas selective oxidizer assemblage for use in a fuel cell power plant includes one or more catalyzed selective oxidizer process gas flow fields and one or more adjacent non-catalyzed heat exchanger process gas flow fields. The catalyzed selective oxidizer process gas flow fields may be formed with catalyzed pellets or with a monolithic catalyzed open cell foam component. The heat exchanger process gas flow fields are formed by non-catalyzed monolithic open cell foam components which have coolant fluid passages disposed therein. Planar metal sheets form a common wall between the selective oxidizer process gas flow fields and the heat exchanger process gas flow fields. The use of the open cell foam to form the heat exchanger process gas flow fields provides enhanced heat transfer between the reformate gas and the coolant fluid.

Abstract: A fuel gas catalyst bed for use in a fuel cell power plant is formed from a monolithic open cell foam component, the open cell lattice of which forms gas passages through the catalyst bed. The monolithic component has a lattice of internal open cells which are both laterally and longitudinally interconnected so as to produce a diffuse gas flow pattern through the catalyst bed. All areas of the monolithic component which form the gas flow pattern are provided with an underlying high porosity wash coat layer. The porous surface of the wash coat layer is provided with a nickel catalyst layer, or a noble metal catalyst layer, such as platinum, rhodium, palladium, or the like, over which the gas stream being treated flows. The base foam lattice can be a metal such as aluminum, stainless steel, a steel-aluminum alloy, a nickel alloy, a ceramic, or the like material which can be wash coated.