A gas-liquid separation apparatus includes a tank and a flow reducing component. An inlet is formed in a middle of the tank. A hydrogen outlet is formed in a top of the tank. A processing chamber connected to the inlet. The flow reducing component is formed in the processing chamber and maintained above the inlet. The flow reducing component forms a flow reducing space and a flow partition chamber in a part of the processing chamber above the inlet, a gas-liquid initial separation space in the processing chamber and below the flow reducing component, at least one connection hole and a connection channel. The flow partition chamber is connected to the flow reducing space through the at least one connection hole. The gas-liquid initial separation space is connected to the flow partition chamber through the connection channel. The flow reducing space is arranged to be connected to the hydrogen outlet.

In a process for the separation of a mixture containing hydrogen and carbon monoxide to produce gaseous hydrogen, the mixture is cooled down to a temperature below 180 C. and then separated at a temperature below 100 C. to produce a gas enriched in hydrogen and a fluid enriched in carbon monoxide, at least a part of the gas enriched in hydrogen is sent to a pressure swing adsorption separation apparatus operating at a temperature above 0 C. to produce a gas rich in hydrogen at a pressure of at least 20 bars, and at least a part of the gas rich in hydrogen is cooled in the heat exchanger down to a temperature below 100 C., reduced in pressure in a turbine down to a pressure of at least 8 bars and reheated in the heat exchanger to constitute a product rich in hydrogen at a pressure of at least 8 bars.

A plant and process for producing a hydrogen rich gas are provided, said process comprising the steps of: steam reforming a hydrocarbon feed into a synthesis gas; shifting the synthesis gas and conducting the shifted gas to a hydrogen purification unit, subjecting CO.sub.2-rich off-gas from the hydrogen purification unit to a carbon dioxide removal and recycling CO.sub.2-depleted off-gas rich in hydrogen to the process.

A chemical plant is provided which comprises an air separation section (ASU), a reformer section, a water-removal section and a refrigerated separation section. A first feed of atmospheric air is separated in the ASU to produce a refrigerant stream. A hydrocarbon feed is converted to a first syngas stream in the reformer section. Water is removed from the first syngas stream and at least a portion of the resulting dried first syngas stream is separated it into at least a product stream, and a by-product stream; by means of the refrigerated separation section. Importantly, the refrigerated separation section is cooled by a refrigerant stream (e.g., nitrogen) from the ASU. A process for producing a product stream, using the plant, is also provided.

Methods and systems for the dehydrogenation of hydrocarbons include a direct contact condenser to remove compounds from an offgas process stream. The reduction of compounds can decrease duty on the offgas compressor by removing steam and aromatics from the offgas. The dehydrogenation reaction system can be applicable for reactions such as the dehydrogenation of ethylbenzene to produce styrene, the dehydrogenation of isoamiline to produce isoprene, or the dehydrogenation of n-pentene to produce piperylene.

A zero-emission, closed-loop and hybrid solar-produced syngas power cycle is introduced utilizing an oxygen transport reactor (OTR). The fuel is syngas produced within the cycle. The separated oxygen inside the OTR through the ion transport membrane (ITM) is used in the syngas-oxygen combustion process in the permeate side of the OTR. The combustion products in the permeate side of the OTR are CO.sub.2 and H.sub.2O. The combustion gases are used in a turbine for power production and energy utilization then a condenser is used to separate H.sub.2O from CO.sub.2. CO.sub.2 is compressed to the feed side of the OTR. H.sub.2O is evaporated after separation from CO.sub.2 and fed to the feed side of the OTR.

The present disclosure relates to a device adapted to produce H.sub.2 and CO.sub.2 from supplied Hydrocarbon and water under high pressure.

The present invention relates a process and apparatus that recovers a helium rich stream from a mixed gas having low concentrations of helium therein. More specifically, the invention relates to an integrated process and apparatus for treating a mixed feed gas from an operating process that produces a liquid product from natural gas containing helium, such as processes that produce ammonia, methanol, or liquid hydrocarbons.

A plant and process for producing a hydrogen rich gas are provided, the process including the steps of: reforming a hydrocarbon feed in a reforming step thereby obtaining a synthesis gas including CH.sub.4, CO, CO.sub.2, H.sub.2 and H.sub.2O; shifting the synthesis gas in a shift configuration including a high temperature shift step; removal of CO.sub.2 upstream hydrogen purification unit, such as a pressure swing adsorption unit (PSA), and recycling off-gas from hydrogen purification unit and mix it with natural gas upstream prereformer feed preheater, prereformer, reformer feed preheater or ATR or shift as feed for the process.

A process for treating a flue gas produced in at least one upstream unit operating at a nominal operating pressure, the flue gas containing from 5 mol % to 90 mol % of CO2 on a wet basis and being at a pressure between 0.5 and 2 bar absolute. The process includes treating, via at least one downstream treatment unit, all or virtually all of the stream of flue gas originating from the upstream unit or upstream units, thereby producing, from the flue gas, a gaseous or liquid stream rich in CO2 which contains more than 50 mol % of CO2. Then enabling the stream of flue gas to communicate, between the upstream unit and the downstream unit with a stack opening to the atmosphere, and this outlet line is left open or partially open in nominal operation thereby equilibrating the pressure in the stream of flue gas to atmospheric pressure.