The invention relates to a gas-liquid separator (2) for separating at least one liquid component, in particular H.sub.2O, from a gaseous component, in particular H.sub.2, the separator comprising at least one container (6) which is supplied with a medium via an inlet (16), at least the liquid component of the medium being separated in at least one container (6) and the separated component of the medium being discharged from the at least one container (6) via a discharge valve (46) with the remaining gaseous component of the medium, in particular H.sub.2, being recirculated into an outflow line (5) via a first outlet (18). According to the invention, in addition to the liquid component, in particular H.sub.2O, a gaseous component N.sub.2 is separated from the medium by the gas-liquid separator (2).

A hydrogen generator for use with an inner combustion engine or other apparatus, even of a movable type, such as a home gas kitchen, said hydrogen generator comprises a system for separating hydrogen from ammonia, said system comprising a NH.sub.3 tank, an ammonia sucking pump, and a cracking oven containing a catalyst, an electric resistance and a H.sub.2/N.sub.2 separating centrifuge and including a suction device comprising a filter followed by a bottle for providing a feeding volume necessary for the produced hydrogen to compensate for user system requirement variations.

A hydrogen generator for use with an inner combustion engine or other apparatus, even of a movable type, such as a home gas kitchen, said hydrogen generator comprises a system for separating hydrogen from ammonia, said system comprising a NH.sub.3 tank, an ammonia sucking pump, and a cracking oven containing a catalyst, an electric resistance and a H.sub.2/N.sub.2 separating centrifuge and including a suction device comprising a filter followed by a bottle for providing a feeding volume necessary for the produced hydrogen to compensate for user system requirement variations.

The present disclosure generally relates to separating entrained solid particles from an input airflow in a gas turbine engine. A cyclonic separator receives the input airflow from a compressor and separates a first portion of the input airflow. The cyclonic separator remove solid particles from the first portion of the input airflow to provide a first cleaned airflow to a first cooling system. A clean air offtake downstream from the cyclonic separator separates a second cleaned airflow from a remaining portion of the input air stream and provides the second cleaned airflow to a second cooling system. The remaining portion of the input airflow is provided to a combustor.

A system and method in at least one embodiment for separating fluids including liquids and gases into subcomponents by passing the fluid through a vortex chamber into an expansion chamber and then through at least a portion of a waveform pattern present between at least two rotors and/or disks. In further embodiments, a system and method is offered for harnessing fields created by a system having rotating rotors and/or disks having waveform patterns on at least one side to produce current within a plurality of coils. In at least one embodiment, the waveform patterns include a plurality of hyperbolic waveforms axially aligned around a horizontal center of the system.

A system and method in at least one embodiment for separating fluids including liquids and gases into subcomponents by passing the fluid through a vortex chamber into an expansion chamber and then through at least a portion of a waveform pattern present between at least two rotors and/or disks. In further embodiments, a system and method is offered for harnessing fields created by a system having rotating rotors and/or disks having waveform patterns on at least one side to produce current within a plurality of coils. In at least one embodiment, the waveform patterns include a plurality of hyperbolic waveforms axially aligned around a horizontal center of the system.

Recovering helium from a gaseous stream includes contacting an acid gas removal membrane with a gaseous stream to yield a permeate stream and a residual stream, removing a majority of the acid gas from the residual stream to yield a first acid gas stream and a helium depleted clean gas stream, removing a majority of the acid gas from the permeate stream to yield a second acid gas stream and a helium rich stream, and removing helium from the helium rich stream to yield a helium product stream and a helium depleted stream. A helium removal system for removing helium from a gaseous stream including hydrocarbon gas, acid gas, and helium includes a first processing zone including a first acid gas removal unit, a second processing zone including a second acid gas removal unit, a third processing zone, and a helium purification unit.

Recovering helium from a gaseous stream includes contacting an acid gas removal membrane with a gaseous stream to yield a permeate stream and a residual stream, removing a majority of the acid gas from the residual stream to yield a first acid gas stream and a helium depleted clean gas stream, removing a majority of the acid gas from the permeate stream to yield a second acid gas stream and a helium rich stream, and removing helium from the helium rich stream to yield a helium product stream and a helium depleted stream. A helium removal system for removing helium from a gaseous stream including hydrocarbon gas, acid gas, and helium includes a first processing zone including a first acid gas removal unit, a second processing zone including a second acid gas removal unit, a third processing zone, and a helium purification unit.

Selective recovery of C2 to C4 hydrocarbons is achieved through the use of a converging-diverging nozzle, or de Laval nozzle. The vapor stream comprising C2 to C4 hydrocarbons is fed into an inlet of a de Laval nozzle having a throat. The vapor stream may have an initial temperature of between 0 C. and 100 C., and an initial pressure of between 200 psig and 500 psig. In the de Laval nozzle, the vapor stream expands after passing through the throat of the de Laval nozzle, producing a vapor stream having re-duced temperature and pressure. Then, C2 to C4 hydrocarbons condense from the reduced-temperature vapor stream as liquid droplets, which may be recovered. Fractionation of C2 to C4 hydrocarbons by means of a de Laval nozzle is possible; the technique allows select-ive recovery of propane from a mixture of propane and ethane.

Selective recovery of C2 to C4 hydrocarbons is achieved through the use of a converging-diverging nozzle, or de Laval nozzle. The vapor stream comprising C2 to C4 hydrocarbons is fed into an inlet of a de Laval nozzle having a throat. The vapor stream may have an initial temperature of between 0 C. and 100 C., and an initial pressure of between 200 psig and 500 psig. In the de Laval nozzle, the vapor stream expands after passing through the throat of the de Laval nozzle, producing a vapor stream having re-duced temperature and pressure. Then, C2 to C4 hydrocarbons condense from the reduced-temperature vapor stream as liquid droplets, which may be recovered. Fractionation of C2 to C4 hydrocarbons by means of a de Laval nozzle is possible; the technique allows select-ive recovery of propane from a mixture of propane and ethane.