Abstract: Disclosed is a new PSA cycle that treats N2-contaminated natural gas at relatively high pressure, and yields a first product enriched in less strongly adsorbed components such as, for example, N2, and others (e.g., helium=He), and a second product that is enriched in more-strongly adsorbed components including, for example, CH4 and others (e.g., ethane=C2H6). The new PSA cycle is characterized by: low power consumption and low adsorbent mass, and therefore relatively small adsorbers. Briefly, a five-adsorber, PSA process separates a gas mixture into a first gas product, which is enriched in a first less-strongly adsorbed component, and a second gas product, which is enriched in more-strongly adsorbed components. The second gas product may be obtained by combining effluents obtained from a series of discrete steps.

Abstract: A multi-step process for removing CO2 from a process gas stream having CO2 and other gaseous components commences by adjusting the temperature of a CO2 laden process gas stream to be between about 80° and about 500° C. A first part of the temperature adjusted process gas stream is taken and contacted with a adsorbent in thermal contact with a heat-exchange surface. The remainder of said temperature adjusted process gas stream is taken and contacted with said heat-exchange surface to transfer heat to said adsorbent, thus causing any adsorbed CO2 to be desorbed for collection, and to cool said process gas stream remainder and removing any condensate from said cooled process gas stream remainder. The cooled process gas stream remainder is passed in contact with a cooled section of said adsorbent to adsorb CO2 therefrom, producing a CO2 depleted process gas stream. The desorbed CO2 is withdrawn for collection.

Abstract: Methane product gas is produced from landfill gas and gob gas either by a three-stage process of PSA-TSA-PSA or PSA-PSA-PSA, or a two-stage process of PSA-PSA.

Abstract: Methane product gas is produced from landfill gas and gob gas either by a three-stage process of PSA-TSA-PSA or PSA-PSA-PSA, or a two-stage process of PSA-PSA.

Abstract: Hydroxylamine is formed in a reactor through a partial hydrogenation of nitric oxide gas (NO) with hydrogen gas (H2) in an aqueous medium with nitrogen gas (N2) as an inert gas. The formation of the hydroxylamine forms nitrous oxide gas (N2O). The gases and the water vapor are flowed away from the reactor in a vent gas stream enabling recycling of the gases. The N2O is removed from the vent gas stream to reduce flammability. Once the N2O is removed, the NO, H2, and N2 are recycled and re-used in the reactor to form additional hydroxylamine. The N2O removed from the vent gas stream is of high purity and can be commercially sold or economically discarded.

Abstract: Hydroxylamine is formed in a reactor through a partial hydrogenation of nitric oxide gas (NO) with hydrogen gas (H2) in an aqueous medium with nitrogen gas (N2) as an inert gas. The formation of the hydroxylamine forms nitrous oxide gas (N2O). The gases and the water vapor are flowed away from the reactor in a vent gas stream enabling recycling of the gases. The N2O is removed from the vent gas stream to reduce flammability. Once the N2O is removed, the NO, H2, and N2 are recycled and re-used in the reactor to form additional hydroxylamine. The N2O removed from the vent gas stream is of high purity and can be commercially sold or economically discarded.

Abstract: A multi-step process for removing CO2 from a process gas stream having CO2 and other gaseous components commences by adjusting the temperature of a CO2 laden process gas stream to be between about 80° and about 500° C. A first part of the temperature adjusted process gas stream is taken and contacted with a adsorbent in thermal contact with a heat-exchange surface. The remainder of said temperature adjusted process gas stream is taken and contacted with said heat-exchange surface to transfer heat to said adsorbent, thus causing any adsorbed CO2 to be desorbed for collection, and to cool said process gas stream remainder and removing any condensate from said cooled process gas stream remainder. The cooled process gas stream remainder is passed in contact with a cooled section of said adsorbent to adsorb CO2 therefrom, producing a CO2 depleted process gas stream. The desorbed CO2 is withdrawn for collection.

Abstract: A method for removing one or more strongly adsorbed components (SAC) from a process gas stream having SAC and other gaseous components adjusts the temperature of the SAC-laden process gas stream to be between about 80° and about 500° C. The temperature-adjusted process gas stream is contacted with a heat-exchange surface to transfer heat to an adsorbent, thus causing adsorbed SAC to be desorbed for collection, and to cool the process gas stream and remove any condensate from the cooled process gas stream. The cooled process gas stream is contacted with a cooled section of the adsorbent to adsorb SAC therefrom, producing a SAC-depleted process gas stream and a SAC-laden adsorbent. Desorbed SAC is withdrawn for collection and any adsorbent fines are withdrawing for collection.

Abstract: A natural gas feed stream containing significant quantities of nitrogen and/or carbon dioxide can be increased to a content of greater than 95 percent by volume of natural gas, and preferably greater than about 98 percent, by passing the natural gas feed stream sequentially through three adsorbent beds that are cycled through seven phases comprising: an adsorption phase to adsorb a first gas, a first depressurization phase to remove feed gas from the voids in the adsorbent bed, a recycle phase to remove a second gas from the adsorbent by the passage of a second depressurization gas therethrough and to produce a recycle gas, a second depressurization phase to reduce the adsorbent bed pressure to about ambient and to produce the second depressurization gas, an evacuation phase where the pressure in the adsorbent is further reduced and an enriched primary gas product stream recovered, a pressurization phase where the pressure in the adsorbent bed is increased using secondary product gas from a bed in an adsorpti

Abstract: The present invention is directed to a catalytic process for the synthesis of ammonia in an ammonia synthesis reactor wherein a dilute ammonia stream is withdrawn from the reactor and subjected to a treatment step to concentrate ammonia adsorbed (or extracted) from said dilute ammonia stream.Specifically, the invention is an improvement in the ammonia concentration treatment step. This improvement includes passing the dilute ammonia stream from the reactor into an adsorber in which is housed particulate adsorbent effective in adsorbing ammonia from the dilute ammonia stream passed through the adsorber. Desirably, adsorber conditions include a pressure close to those prevailing in the dilute ammonia stream withdrawn from the reactor with the temperature being as low as that of the feed to the reactor. Next, an effluent stream diminished in ammonia content is withdrawn from the adsorber. Finally, enriched ammonia is recovered from the adsorber.

Abstract: The present process is directed to the efficient recovery of helium gas from gas streams which contain about 25 percent by volume or more helium. The process comprises two stages of pressure swing adsorption, each stage being comprised of a plurality of interconnected adsorbent beds. In the first stage of pressure swing adsorption which is comprised of about five phases, the helium content of the gas stream is increased to 95 percent by volume or more. A secondary product gas stream from the first stage of pressure swing adsorption is fed to the second stage of pressure swing adsorption. The second stage of pressure swing adsorption increases the helium content of this primarily non-helium product gas to more than about 50 percent by volume. This gas now with a helium content of more than about 50 percent by volume is fed along with the gas stream as the input gas to the first stage of pressure swing adsorption.

Abstract: The disclosed hybrid membrane and pressure swing adsorption process can recover helium from source streams of about 0.5 to 5 percent by volume helium and concentrate the helium to a concentration of greater than about 98 percent by volume. The process comprises a membrane separation followed by two stages of pressure swing adsorption which are used in series. The source gas will primarily contain hydrocarbons but will contain some nitrogen. The membrane unit will contain a semipermeable membrane which is permeably selective for helium and will to the extent feasible reject hydrocarbons. The permeate gas will be increased in helium content by 2 to 10 times. Part of the residue gas is used in the regeneration of the adsorbent beds in the first stage of pressure swing adsorption. Each stage of pressure swing adsorption will contain a plurality of adsorbent beds, and will be cycled through multiple phases.

Abstract: The disclosed pressure swing adsorption processes can recover helium from source streams of less than about 10 percent by volume helium and concentrate the helium to a concentration of greater than about 98 percent by volume. Two stages of pressure swing adsorption are used in series. The source of the helium gas will be natural gas wells. The source gas will contain hydrocarbons but in most instances the primary gas other than helium will be nitrogen. Each stage of pressure swing adsorption will contain a plurality of adsorbent beds, and preferably about four. In each stage the adsorbent beds will be cycled through multiple phases. In the first stage the adsorbent beds will sequentially undergo the phases of adsorption, recycle, depressurization, evacuation, helium pressurization and recycle feed pressurization.

Abstract: A natural gas feed stream containing significant quantities of nitrogen can be increased to a content of greater than 95 percent by volume of natural gas, and preferably greater than about 98 percent, by passing the natural gas feed stream sequentially through at least four adsorbent beds which are cycled through six phases comprising an adsorption phase to adsorb natural gas, a recycle phase to remove feed gas from the voids in the adsorbent bed and nitrogen from the adsorbent by the passage of a depressurization gas therethrough to produce a recycle gas, a depressurization phase to reduce the adsorbent bed pressure to about ambient and to produce the depressurization gas, an evacuation phase where the pressure in the adsorbent is further reduced and an enriched natural gas product stream recovered, a pressurization phase where the pressure in the adsorbent bed is increased using nitrogen gas from a bed in an adsorption phase, and further pressurizing the adsorbent bed in a recycle feed pressurization phase

Abstract: System and method for monitoring the level of a VOC or other vapor contaminant emitted in a gas stream or the like being vented at a specified pressure from an emission source. A medium of a bed of solid particles is provided within a vessel having an inlet and an outlet which is effective for separating the contaminant from the gas stream. The inlet pressure of the vessel is maintained at the specified pressure of the gas stream being vented from the emission source. The separated contaminants are concentrated in the medium which exhibits an increase in mass corresponding to the amount of the contaminant that was contained in the gas stream.

Abstract: A pressure swing adsorption (PSA) process for splitting oxygen from a feed gas comprising 95% oxygen and 5% argon to achieve an oxygen purity of at least about 99.7% is provided. A column used in the PSA process includes therein a bed of silver mordenite, an adsorbent determined to be selective to argon. In a preferred embodiment, the feed gas has a pressure of about 10.7 atm and a flow rate of about 8.8-9.2 vol. per cycle/vol of column.

Abstract: A continuous cyclic thermal swing adsorption process for the regeneration of a fixed adsorption bed and the purification of an incoming feed liquid stream, with the utilization of at least one product recycle stream, the feed stream comprising a solvent containing at least one dissolved solute, the process comprising contacting a first feed liquid stream maintained at a first temperature, the first feed stream comprising a mixture of a recycled pure, product liquid stream and optionally, at least some of the incoming feed liquid stream, with an at least partially saturated fixed adsorption bed to thereby regenerate the fixed adsorption bed while removing an enriched product liquid stream from the fixed adsorption bed; recycling an effective amount of the enriched product liquid stream having a desired solute concentration to a first storage means; contacting a second feed liquid stream, the second feed stream comprising a mixture of the incoming feed liquid stream and the recycled enriched product liquid stre

Abstract: A pressure swing adsorption cycle comprised of blowdown, purge, pressurization, feed, pressure equalization and rinse steps provided recovery from an atmospheric air feed, essentially dry and free of carbon dioxide, of a high yield of high purity nitrogen gas and a high yield of a product gas rich in oxygen as well as recovery of a residual feed byproduct gas for recycle with the air feed.

Abstract: Complementary pressure swing adsorption is a method of purifying and quantitatively recovering a plurality of components from a multicomponent gaseous mixture. A plurality of adsorption columns is used, each containing an adsorbent which is selective for one of the components to be recovered, but not the others. Blowdown and purge effluent from each column is used as high-pressure feed for a complementary column containing a different adsorbent. Nitrogen and oxygen may be separated from air, for use on tactical aircraft or in hospitals and various industries.

Abstract: The present invention is a multi-step process for generating energy from a source heat flow. Such a process comprises passing a heated media having a mixture of a low volatility component and a high volatility component into a phase separator. The vaporous working fluid is withdrawn from the phase separator and passed into a work zone, such as a turbine, wherein the fluid is expanded. The expanded vaporous working fluid is withdrawn from the work zone and passed into a direct contact condenser or absorber. The separated weak solution is withdrawn from the phase separator and passed into counter-current heat exchange relationship in an interchanger with a portion of media from the direct contact condenser or absorber. The media from the direct contact condenser or absorber is withdrawn and passed into a fluid pressurizing zone.