An igniter apparatus which generates a high speed buoyancy induced vortex to funnel hydrogen and air from the surrounding onto the igniter core where an igniter core heats up to the auto ignition temperature by the exothermic catalytic oxidation of hydrogen on its surface. Water (vapor) is formed as the product, which inhibits the oxidation reaction, if not stripped away from the catalyst surface. The high velocity of the vortex ensures the stripping of the boundary layer of steam that is formed by the reaction, thus ensuring more active sites are available for hydrogen oxidation. The vortex is formed by channeling an upward draft into a vortex by guided fins. The upward draft is formed by a plate, which is also coated with a hydrogen recombination catalyst. The plate becomes hot by the same catalytic oxidation reaction in the presence of air containing hydrogen.

The present disclosure provides systems and methods for producing olefins via an oxidative coupling of methane (OCM) process. The systems and methods may comprise the use of a staged process comprising at least one non-adiabatic section that is in thermal communication with a heat transfer medium and at least one substantially adiabatic section. The systems and methods may also comprise the use of a diluent stream which may improve methane conversion in an OCM reactor and an ethylene/ethane ratio in a post-bed cracking unit. The methods and systems may further comprise injecting oxygen (O.sub.2) and a paraffin into a gas stream containing a radical transfer agent to provide a reaction mixture. The reaction mixture may be held in a vessel for a time period greater than an auto-ignition delay time (AIDT), such that the reaction mixture may ignite to liberate heat and convert to a product mixture comprising olefins.

A chemical reactor that combines a pressure vessel, heat exchanger, heater, and catalyst holder into a single device is disclosed. The chemical reactor described herein reduces the cost of the reactor and reduces its parasitic heat losses. The disclosed chemical reactor is suitable for use in ammonia (NH.sub.3) synthesis.

Catalyst support systems for ammonia oxidation burners comprising a top flange and an inner wall. The top flange comprises a planar section, a rounded outer edge, and a rounded inner edge, the rounded outer edge and the rounded inner edge being separated by the planar section. The inner wall comprises a carrier plate, a gauze shelf, and a bottom plate shelf, the gauze shelf and the bottom plate shelf being attached to the carrier plate. The carrier plate is attached to the top flange by means of the rounded inner edge.

A tube heat exchange reactor for carrying out an endothermic catalytic reaction. The tube heat exchange reactor includes: an outer tube with a first and a second end, where the first end is an inlet end and where the second end is a closed end, an inner tube coaxially arranged within the outer tube and spaced apart from the outer tube, where at least a part of the inner tube holds a bed of catalyst material susceptible for induction heating and where the inner tube has an inlet end and an outlet end, an induction coil placed within the annular space confined between the outer and the inner tube, and a power source arranged to supply alternating current to the induction coil in order to generate an alternating magnetic field within at least a part of the inner tube.

Systems and methods are provided for performing hydrocarbon reforming within a reverse flow reactor environment (or another reactor environment with flows in opposing directions) while improving management of CO.sub.2 generated during operation of the reactor. The improved management of CO.sub.2 is achieved by making one or more changes to the operation of the reverse flow reactor. The changes can include using an air separation unit to provide an oxygen source with a reduced or minimized content of nitrogen and/or operating the reactor at elevated pressure during the regeneration stage. By operating the regeneration at elevated pressure, a regeneration flue gas can be generated that is enriched in CO.sub.2 at elevated pressure. The CO.sub.2-enriched stream can include primarily water as a contaminant, which can be removed by cooling while substantially maintaining the pressure of the stream. This can facilitate subsequent recovery and use of the CO.sub.2.

Systems and methods are provided for using a high heat capacity gas as at least a portion of the diluent during the regeneration step of a reverse flow reactor process. Instead of using nitrogen or air as the primary diluent gas, CO.sub.2 and/or H.sub.2O can be added as diluent gas for the regeneration step in the reaction cycle. Increasing the heat capacity of the diluent gas provides a reduction in the peak temperature within the reactor relative to the amount of fuel combusted during regeneration. This can allow for a reduction in the volume of diluent used during regeneration and/or an increase in the amount of fuel used. Reducing the volume of diluent can reduce the pressure drop during regeneration, which can provide a corresponding reduction in the amount of compression required for recycle of the diluent. Increasing the amount of fuel can allow for a corresponding increase in the amount of endothermic reaction performed during the reaction step.

A fuel reformer module (8005) for initiating catalytic partial oxidation (CPOX) to reform a hydrocarbon fuel oxidant mixture (2025, 3025) to output a syngas reformate (2027) to solid oxide fuel cell stack (2080, 5040). A solid non-porous ceramic catalyzing body (3030) includes a plurality of catalyst coated fuel passages (3085). A thermally conductive element (9005, 10005, 11005, 13005), with a coefficient of thermal conductivity of 50 W/m K or greater is thermally conductively coupled with the catalyzing body. A first thermal sensor (8030) is thermally conductively coupled with the thermally conductive element. A second thermal sensor is thermally conductively coupled with a surface of the fuel cell stack. A control method independently modulates an oxidant input flow rate, based on first thermal sensor signal values, a hydrocarbon fuel input flow rate, based on second thermal sensor signal values.

Methods and apparatus for compact and easily maintainable waste reformation. Some embodiments include a rotary oven reformer adapted and configured to provide synthesis gas from organic waste. Some embodiments include a rotary oven with simplified operation both as to reformation of the waste, usage of the synthesized gas and other products, and easy removal of the finished waste products, preferably in a unit of compact size for use in austere settings. Yet other embodiments include Fischer-Tropsch reactors of synthesized gas. Some of these reactors include heat exchanging assemblies that provide self-cleaning effects, efficient utilization of waste heat, and ease of cleaning.

Integrated liquid fuel catalytic partial oxidation (CPOX) reformer and fuel cell systems can include a plurality or an array of spaced-apart CPOX reactor units, each reactor unit including an elongated tube having a gas-permeable wall with internal and external surfaces. The wall encloses an unobstructed gaseous flow passageway. At least a portion of the wall has CPOX catalyst disposed therein and/or comprising its structure. The catalyst-containing wall structure and open gaseous flow passageway enclosed thereby define a gaseous phase CPOX reaction zone, the catalyst-containing wall section being gas-permeable to allow gaseous CPOX reaction mixture to diffuse therein and hydrogen rich product reformate to diffuse therefrom. The liquid fuel CPOX reformer also can include a vaporizer, one or more igniters, and a source of liquid reformable fuel. The hydrogen-rich reformate can be converted to electricity within a fuel cell unit integrated with the CPOX reactor unit.