Abstract: Disclosed herein are novel RHO zeolites useful as kinetically selective adsorbents for oxygen and/or nitrogen. The adsorbents can be used in pressure swing adsorption processes for selectively adsorbing oxygen and/or nitrogen from feed streams such as an air stream or crude argon stream. Also disclosed are novel methods of preparing RHO zeolites, including in particular mixed-cation RHO zeolites.

Abstract: Disclosed herein are new processes for adsorbing oxygen using adsorbent compositions comprising RHO zeolites kinetically selective for oxygen. The RHO zeolites can be used in pressure swing adsorption processes for separating oxygen from oxygen containing streams, such as for, but not limited to, purifying a crude argon feed stream or separating oxygen from an air feed stream.

Abstract: Disclosed herein are novel RHO zeolites useful as kinetically selective adsorbents for oxygen and/or nitrogen. The adsorbents can be used in pressure swing adsorption processes for selectively adsorbing oxygen and/or nitrogen from feed streams such as an air stream or crude argon stream. Also disclosed are novel methods of preparing RHO zeolites, including in particular mixed-cation RHO zeolites.

Abstract: Disclosed herein are new processes for adsorbing oxygen using adsorbent compositions comprising RHO zeolites kinetically selective for oxygen. The RHO zeolites can be used in pressure swing adsorption processes for separating oxygen from oxygen containing streams, such as for, but not limited to, purifying a crude argon feed stream or separating oxygen from an air feed stream.

Abstract: The present invention relates to a temperature enhanced pressure swing adsorption (TEPSA) process for removing at least two components including a less strongly adsorbed component and a more strongly adsorbed component from a gas mixture, said process comprising using one single heater and at least two adsorber vessels, in each of which repeated cycles comprising an adsorption phase and subsequent regeneration phases.

Abstract: A radial U-flow adsorption unit for air purification in a TSA process, having a gas outlet at one end and at least one gas inlet at the side, preferably at the same end of the unit as the gas outlet. The simpler design of the unit facilitates manufacture, installation and transport, and reduces the capital and operating costs.

Abstract: The present invention relates to a temperature enhanced pressure swing adsorption (TEPSA) process for removing at least two components including a less strongly adsorbed component and a more strongly adsorbed component from a gas mixture, said process comprising using one single heater and at least two adsorber vessels, in each of which repeated cycles comprising an adsorption phase and subsequent regeneration phases.

Abstract: A radial U-flow adsorption unit for air purification in a TSA process, having a gas outlet at one end and at least one gas inlet at the side, preferably at the same end of the unit as the gas outlet. The simpler design of the unit facilitates manufacture, installation and transport, and reduces the capital and operating costs.

Abstract: Process of reducing water, CO2 and N2O in feed air, which: a first adsorbent such as alumina (25-40% volume) and a second adsorbent such as X zeolite (60-75% volume) are used; the online time of the adsorbent is determined by determining the concentration measured by an analyzer for CO2 concentration at a position within the length of the second adsorbent when a maximum level of N2O is simultaneously obtained at the downstream end of the second adsorbent in the feed direction, wherein the online time is the time taken from commencing passing the feed air to the first and second adsorbents to the measurement by the analyzer of the determined concentration of CO2; at least the second adsorbent is regenerated by heated regeneration gas at a temperature of 140° C.-220° C.; and the molar ratio of the regenerating gas to feed air supplied during one iteration of the cycle is 0.08-0.5.

Abstract: Hydrogen and carbon monoxide impurities are removed from a dry gas comprising the impurities, wherein the dry gas is at least substantially free of carbon dioxide, by passing the dry gas with sufficient residence time, e.g. at least 1.5 s, through a layer of catalyst comprising a mixture of manganese oxide and copper oxide. The use of expensive noble metal catalysts to remove hydrogen may thereby be avoided. In addition, regeneration of the catalyst using oxygen-containing regeneration gas does not reduce the effectiveness of the catalyst.

Abstract: Hydrogen and carbon monoxide impurities are removed from a dry gas comprising the impurities, wherein the dry gas is at least substantially free of carbon dioxide, by passing the dry gas with sufficient residence time, e.g. at least 1.5 s, through a layer of catalyst comprising a mixture of manganese oxide and copper oxide. The use of expensive noble metal catalysts to remove hydrogen may thereby be avoided. In addition, regeneration of the catalyst using oxygen-containing regeneration gas does not reduce the effectiveness of the catalyst.

Abstract: Reduction of water, CO2 and N2O in an air stream comprising: passing said air stream at a feed temperature through a first adsorbent, whose Henry's Law selectivity for CO2/N2O is at least 12.5, and a second adsorbent, whose Henry's Law constant for CO2 is less than 1020 mmol/g/atom and whose Henry's Law selectivity for CO2/N2O is at most 5; and passing a heated regenerating gas at a temperature which is between 20° C. and 80° C. to at least the second adsorbent, and passing a second regenerating gas at a temperature less than the temperature of the heated regenerating gas to the first and second adsorbents in a direction opposite to the feed direction; the second adsorbent occupying from 25% to 40% of the total volume of the adsorbents, and the temperature of the heated regenerating gas being 10° C. to 60° C. higher than the feed temperature.

Abstract: Reduction of water, CO2 and N2O in an air stream comprising: passing said air stream at a feed temperature through a first adsorbent, whose Henry's Law selectivity for CO2/N2O is at least 12.5, and a second adsorbent, whose Henry's Law constant for CO2 is less than 1020 mmol/g/atom and whose Henry's Law selectivity for CO2/N2O is at most 5; and passing a heated regenerating gas at a temperature which is between 20° C. and 80° C. to at least the second adsorbent, and passing a second regenerating gas at a temperature less than the temperature of the heated regenerating gas to the first and second adsorbents in a direction opposite to the feed direction; the second adsorbent occupying from 25% to 40% of the total volume of the adsorbents, and the temperature of the heated regenerating gas being 10° C. to 60° C. higher than the feed temperature.

Abstract: The concentration of adsorbate in the feed gas to an on-stream bed of a cyclical swing adsorption process is monitored and the data processed to predict the time required to complete the on-stream mode of that bed and the purge flow rate and/or other regeneration mode operating condition of the concurrently off-stream bed is modified in response to changes in said predicted time whereby the regeneration mode of the off-steam bed is completed at the same time as the on-stream mode of the concurrent on-stream bed.

Abstract: Base treated aluminas exhibit improved CO2 capacity over untreated aluminas. Base treated aluminas prepared by physically mixing alumina and base during forming have (1) a higher surface area, (2) less hydrothermal aging, (3) improved CO2 capacity and (4) lower cost than base treated aluminas produced by aqueous impregnation. A method for removing at least CO2 and water from a gas stream includes providing an adsorbent formed from a process comprising physically mixing activated alumina solids and solid salts of alkali metals, alkaline earth metals or ammonium ion; and contacting the gas stream with the adsorbent.

Abstract: At least one section of structured packing where the length of the section is about 1 m to about 6 m; and where the specific surface area of the structured packing of the section is greater than 500 m2/m3, is used in a vapour/liquid contact column operating in locations where environmental conditions adversely affect steady state operation of the column to reduce maldistribution of liquid in the column under motion. The structured packing section has particular application offshore on a buoyant platform where tilt of the column out of vertical alignment due to the rolling motion of the platform can significantly affect the efficiency of the column.

Abstract: The concentration of adsorbate in the feed gas to an on-stream bed of a cyclical swing adsorption process is monitored and the data processed to predict the time required to complete the on-stream mode of that bed and the purge flow rate and/or other regeneration mode operating condition of the concurrently off-stream bed is modified in response to changes in said predicted time whereby the regeneration mode of the off-steam bed is completed at the same time as the on-stream mode of the concurrent on-stream bed.

Abstract: An improved control scheme is set forth for an adsorption process that removes water and carbon dioxide (CO2) from a feed gas using a hybrid of both temperature swing (i.e. TSA) and pressure swing (PSA) to regenerate the adsorbent. The control scheme comprises adjusting the quantity of heat to be provided by the regeneration gas as a function of temperature data taken within a strategic portion of the water selective adsorbent zone. The strategic portion corresponds to the location for the desired transition from regeneration by temperature swing, to regeneration by pressure swing. In a preferred embodiment of the present invention, said quantity of regeneration heat is also adjusted as a function of the water content of the feed gas.

Abstract: An improved thermal swing adsorption process is set forth which addresses the problem of water ingress into the adsorbent by periodically heating the adsorbent to a temperature greater than the temperature used in the normal regeneration cycle.

Abstract: An adsorber vessel for use in the adsorption of a component from a gas and subsequent regeneration by thermally induced desorption of the component comprises an inlet for regeneration gas having an inlet nozzle containing at least one heater element, and an outlet for regeneration gas, the inlet and outlet for regeneration being separated by a flow path including a flow chamber containing a body of adsorbent, and wherein the body of adsorbent has a first end which is adjacent the inlet for regeneration gas and a second end which is remote from the inlet for regeneration gas, and the or each heater element is located so as not to penetrate through the first end of the body of adsorbent.