A thermo-electrochemical reactive capture apparatus includes an anode and a cathode, wherein the anode includes a first catalyst, wherein the cathode includes a second catalyst, a porous ceramic support positioned between the anode and the cathode, an electrolyte mixture in pores of the ceramic support, and a steam flow system on an outer side of the cathode. The outer side of the cathode is opposite an inner side of the cathode and the inner side of the cathode is adjacent to the ceramic support. In addition, the electrolyte mixture is configured to be molten at a temperature below about 600° C.

The present disclosure describes a system and method for maintaining oxygen purity in portable oxygen concentrators, even with asymmetric generation of oxygen enriched gas volumes from different sieve beds of the concentration system. The present system and method compensate for asymmetric oxygen enriched gas generation using asymmetric delivery of purge volumes. Purge valves are used to deliver the asymmetric purge gas volumes, enables the system to maintain oxygen purity without additional power consumption, even when a portable oxygen concentrator does not include a product tank. The present system and method are configured such that asymmetry in enriched oxygen generation can be monitored and the asymmetric purge gas compensation can be applied independently from other control mechanisms of a portable oxygen concentrator.

When the product gas producing operation is stopped, a stand-by operation is executed in which a product gas filling up a reforming processing unit is circulated, in a state in which an adsorbent of adsorption towers is maintained in a state in which adsorption target components are desorbed, and the heating of a reformer by a heating burner is maintained, and when the stand-by operation is stopped and the product gas producing operation is started, initial operation processing is executed in which immediately after the start, a source gas and steam are supplied to the reformer to produce a reformed gas, and the reformed gas from the reforming processing unit supplied to the adsorption towers to produce the product gas, and then the product gas producing operation in which the product gas is collected in a product gas tank is executed.

The disclosure discloses an energy-saving system for purifying and recycling oxygen from high-temperature oxygen-enriched flue gas, including a water washing mechanism for introducing high-temperature oxygen-enriched flue gas, a compressor set connected with the water washing system through a pipeline, a compressor outlet heat exchanger connected with the compressor set through a pipeline, a gas-liquid separation tank connected with the compressor outlet heat exchanger through a pipeline, a temperature swing adsorption isobaric drying mechanism and a pressure swing adsorption purification mechanism connected with the gas-liquid separation tank through pipelines, a dedusting and filtering mechanism for introducing gas treated by the temperature swing adsorption isobaric drying mechanism and the pressure swing adsorption purification mechanism, and a cooling mechanism for cooling the water washing mechanism and the compressor outlet heat exchanger.

The present invention relates to a separation and recovery system and method of hydrogen from a coke oven gas (COG) in a steel industry, and more particularly, to a separation and recovery system and method of hydrogen from a coke oven gas (COG) in a steel industry, the system including a pre-processing unit removing impurities including tar, moisture, oil, hydrogen sulfide, and dusts from the coke oven gas (COG), a membrane separation unit including a polymer separation membrane module to generate a hydrogen concentrated gas stream by membrane-separating the coke oven gas (COG) processed in the pre-processing unit, and an adsorption unit separate and recover the hydrogen by allowing the hydrogen concentrated gas stream to contact an absorbent.

Described herein are various embodiments of an oxygen concentrator system. In some embodiments, oxygen concentrator system includes one or more components that improve the useful lifetime of gas separation adsorbents.

When a product gas producing operation is stopped, a purge operation is executed in which steam purge processing and product gas purge processing are sequentially performed. The steam purge is supplying, instead of a source gas, a product gas from a product gas tank to a reformer using a compressor, and supplying a reformed gas from a reforming processing unit to a plurality of adsorption towers, which perform a pressure swing adsorption operation, while the reformer is heated by a heating burner and steam is supplied to the reformer. The product gas purge is supplying the product gas from the product gas tank to the reformer using the compressor, and supplying the product gas from the reforming processing unit to the plurality of adsorption towers, which perform the pressure swing adsorption operation, while the supply of the steam is stopped and the heating of the reformer is maintained.

The present disclosure relates to a purge system for a vapor compression system, where the purge system includes an emission canister configured to receive a gas flow. The gas flow includes a mixture of non-condensable gases and refrigerant of the vapor compression system. An adsorbent material is disposed within the emission canister and configured to adsorb the refrigerant and enable the non-condensable gases to flow toward an exhaust of the emission canister, where the adsorbent material is a silica gel.

A membrane including a polymer substrate having pore channels and a metal-organic framework disposed on the polymer substrate. Methods of producing the membrane are described. Methods of separating gases using the membrane are also provided.

A system and method for flexible production of argon from a cryogenic air separation unit is provided. The cryogenic air separation unit is capable of operating in a ‘no-argon’ or ‘low-argon’ mode when argon demand is low or non-existent and then switching to operating in a ‘high-argon’ mode when argon is needed. The recovery of the argon products from the air separation unit is adjusted by varying the percentages of dirty shelf nitrogen and clean shelf nitrogen in the reflux stream directed to the lower pressure column. The cryogenic air separation unit and associated method also provides an efficient argon production/rejection process that minimizes the power consumption when the cryogenic air separation unit is operating in a ‘no-argon’ or ‘low-argon’ mode yet maintains the capability to produce higher volumes of argon products at full design capacity to meet argon product demands.