The present disclosure provides a method for a mobile pressure swing adsorption oxygen production device, comprising a first PSA section, a second PSA section and a third PSA section which are operated in series; the first PSA section adsorbs oxygen in raw air by a velocity-selective adsorbent; the second PSA section adsorbs nitrogen etc. in desorption gas of the first PSA section by a nitrogen balance-selective adsorbent; the third PSA section removes nitrogen from oxygen-rich gas flowing out of the second PSA section; the first PSA section sequentially undergoes at least adsorption A and vacuumizing VC in one cycle; the second PSA section sequentially undergoes at least adsorption A, pressure-equalizing drop ED, backward discharge BD and pressure-equalizing rise ER; and the third PSA section sequentially undergoes at least adsorption A, pressure-equalizing drop ED, backward discharge BD and pressure-equalizing rise ER.

Systems and processes for use of concentric adsorbent beds with rotary valve assemblies are provided.

Biogas containing H.sub.2S and CO.sub.2 is upgraded by removing H.sub.2S using PTSA and CO.sub.2 using two stages of gas separation membranes. The first stage permeate may optionally be used a regeneration gas stream. The second stage permeate may optionally be used a cool down gas stream. The PTSA unit includes two or more adsorbent beds each selective for water, VOCs, and H.sub.2S over CO.sub.2 and for H.sub.2S over methane.

Systems and methods are provided for combined cycle power generation while reducing or mitigating emissions during power generation. Recycled exhaust gas from a molten carbonate fuel cell power generation reaction can be separated by using a swing adsorption process so as to generate a high purity CO.sub.2 stream while reducing or minimizing the energy required for the separation and without having to reduce the temperature of the exhaust gas. A high temperature adsorption reactor adsorbs the CO.sub.2 and recovers H.sub.2 from an exhaust gas of a first molten carbonate fuel cell at a high temperature and at a low pressure. The reactor passes along the adsorbed CO.sub.2 to a cathode and the recovered H.sub.2 to an anode of a second molten carbonate fuel cell for further power generation. This can allow for improved energy recovery while also generating high purity streams of CO.sub.2 and H.sub.2.

An evaporative emission control canister system comprises an initial adsorbent volume having an effective incremental adsorption capacity at 25 C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25 C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, an effective butane working capacity (BWC) of less than 3 g/dL, and a g-total BWC of between 2 grams and 6 grams. The evaporative emission control canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than 210 liters of purge applied after the 40 g/hr butane loading step.

Through the procedures of pretreatment, temperature swing adsorption (TSA) coarse desorption, pressure swing adsorption (PSA) purification and hydrogen purification, the hydrogenous waste gas from various procedures in the manufacturing process of semiconductor (especially silicon wafer), including the off-gas from chemical vapor deposition (CVD), doping (diffusion and ion implantation), photolithography and cleaning, the combusted and washed discharged gas of the off-gas in other procedures after field treatment and centralized treatment, or the hydrogenous waste gas entering the hydrogen discharge system are purified to meet the standard for the electronic grade hydrogen required for the manufacturing process of semiconductor, the recycling of hydrogen resources is realized, and the yield of hydrogen is greater than or equal to 70-85%. The present invention solves the technical difficulty the normal-pressure waste hydrogen recovered in the manufacturing process of semiconductor can't be returned to the manufacturing process of semiconductor for reuse.

Provided are apparatus and systems for performing a swing adsorption process. This swing adsorption process may involve performing the swing adsorption process in a swing adsorption process skid. The process may be utilized for swing adsorption processes, such as TSA and/or PSA, which are utilized to remove one or more contaminants from a gaseous feed stream.

A method for producing oxygen by adsorbing a stream of atmospheric air, using a VPSA, including at least one adsorber, each adsorber undergoing a single pressure cycle including the following steps: a) producing a first stream of gas having an oxygen content T1 while loading the adsorber of the stream of atmospheric air upstream; b) producing a second stream of gas including an oxygen content T2<T1: c) producing a third stream of gas including an oxygen content T3<T2<T1 while simultaneously extracting a nitrogen-enriched residual stream; d) eluting the adsorber, from which the three streams of gas produced in steps a), b), and c) are taken with the second stream of gas produced in step b); e) repressurizing the adsorber consecutively with at least two streams, first and second repressurizing streams, with increasing oxygen content.

An evaporative emission control canister system comprises an initial adsorbent volume having an effective incremental adsorption capacity at 25? C. of greater than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, and at least one subsequent adsorbent volume having an effective incremental adsorption capacity at 25? C. of less than 35 grams n-butane/L between vapor concentration of 5 vol % and 50 vol % n-butane, an effective butane working capacity (BWC) of less than 3 g/dL, and a g-total BWC of between 2 grams and 6 grams. The evaporative emission control canister system has a two-day diurnal breathing loss (DBL) emissions of no more than 20 mg at no more than 210 liters of purge applied after the 40 g/hr butane loading step.

Systems and methods are provided for using a multi-stage capture process for capture of CO.sub.2 from air. A first or initial sorption process is used to sorb CO.sub.2 from air. After sorption from the air is complete, the desorption step of the initial stage is used to form a secondary CO.sub.2-containing stream that is passed into one or more additional sorption stages. This secondary CO.sub.2-containing stream can be at a concentration of roughly 1.0 vol % or more. Sorption of CO.sub.2 from the secondary CO.sub.2-containing stream is performed using a different contacting method, such as a contacting method that is higher efficiency. The second or later CO.sub.2 sorption stage can produce a CO.sub.2-containing output stream with a CO.sub.2 concentration of 80 vol % or more, or 90 vol % or more, or 95 vol % or more. This high purity output stream can then be sequestered and/or used for further processing.