Abstract: A binderless X-type zeolite is used in a process for the reduction of the level of carbon dioxide and/or N2O in a gaseous mixture, the zeolite being obtained by converting the binder in a bound zeolite to zeolite such that the ratio of the adsorption capacity for carbon dioxide of the binderless zeolite to the adsorption capacity of the bound zeolite is greater than the weight ratio of the level of zeolite in the binderless zeolite to the level in the bound zeolite.

Abstract: A binderless X-type zeolite is used in a process for the reduction of the level of carbon dioxide and/or N2O in a gaseous mixture, the zeolite being obtained by converting the binder in a bound zeolite to zeolite such that the ratio of the adsorption capacity for carbon dioxide of the binderless zeolite to the adsorption capacity of the bound zeolite is greater than the weight ratio of the level of zeolite in the binderless zeolite to the level of zeolite in the bound zeolite.

Abstract: The present invention describes a pressure swing adsorption (PSA) apparatus and process for the production of purified hydrogen from a feed gas stream containing heavy hydrocarbons (i.e., hydrocarbons having at least six carbons). The apparatus comprises at least one bed containing at least three layers. The layered adsorption zone contains a feed end with a low surface area adsorbent (20 to 400 m2/g) which comprises 2 to 20% of the total bed length followed by a layer of an intermediate surface area adsorbent (425 to 800 m2/g) which comprises 25 to 40 % of the total bed length and a final layer of high surface area adsorbent (825 to 2000 m2/g) which comprises 40 to 78% of the total bed length.

Abstract: The present invention describes a pressure swing adsorption (PSA) apparatus and process for the production of purified hydrogen from a feed gas stream containing heavy hydrocarbons (i.e., hydrocarbons having at least six carbons). The apparatus comprises at least one bed containing at least three layers. The layered adsorption zone contains a feed end with a low surface area adsorbent (20 to 400 m2/g) which comprises 2 to 20% of the total bed length followed by a layer of an intermediate surface area adsorbent (425 to 800 m2/g) which comprises 25 to 40 % of the total bed length and a final layer of high surface area adsorbent (825 to 2000 m2/g) which comprises 40 to 78% of the total bed length.

Abstract: The present invention is a method for production of a hydrogen-rich fuel gas compatible for a fuel cell, comprising; reforming a hydrocarbon-containing fuel to a CO-containing, hydrogen-rich reformate, converting CO in the reformate to CO2 and hydrogen by a catalyzed water-shift reaction, removing residual CO in the reformate by adsorption on a copper halide adsorbent, and passing the essentially CO-free reformate as a hydrogen-rich fuel gas to a fuel cell.

Abstract: An improved adsorption process is provided for purifying hydrogen from a feed gas mixture including hydrogen and at least one impurity selected from the group consisting of carbon monoxide and nitrogen. The process includes providing an adsorption apparatus having a discharge end adsorption layer containing an adsorbent with a Henry's law constant (KH) at 70° F. for the impurity from about 0.5 to about 2.4 mmole/g/atm. The product gas collected from the adsorption apparatus is high purity (99.99+%) hydrogen.

Abstract: The present invention provides a pressure swing adsorption process. The process includes providing a pressure swing adsorption apparatus having a discharge end adsorption layer of activated carbon, feeding through the apparatus a feed gas including hydrogen, carbon monoxide and at least one of argon and oxygen, and collecting a product gas from the apparatus, wherein the product gas is high purity hydrogen. Also provided is a method for decreasing an amount of impurities in a product gas from a pressure swing adsorption process for separating hydrogen from impurities including carbon monoxide, and at least one of argon and oxygen.

Abstract: Carbon dioxide, water, nitrous oxide and optionally ethylene are removed from a feed air stream by a temperature swing adsorption using a first adsorbent such as alumina to adsorb water, a second adsorbent such as 13X zeolite to adsorb carbon dioxide, and a third adsorbent such as binderless calcium exchanged X zeolite to adsorb nitrous oxide and optionally ethylene, prior to cryogenic separation of the purified air stream.

Abstract: Carbon dioxide, water, carbon monoxide and hydrogen are removed from a gas stream such as air or nitrogen by adsorbing water and carbon dioxide on a solid absorbent of alumina, or zeolite and oxiding carbon monoxide over a solid catalyst to carbon dioxide and adsorbing the resulting carbon dioxide and chemisorbing the hydrogen on the catalyst, which may be palladium on alumina.

Abstract: Carbon monoxide is removed from air prior to cryogenic separation of oxygen and nitrogen. Feed air is compressed and the heat of compression is used without further heating to drive catalytic oxidation of CO to CO.sub.2 over a Pd and/or Pt on alumina catalyst followed by adsorption of water initially present and then either adsorption of hydrogen or oxidation of hydrogen to water and its removal by adsorption, along with carbon dioxide.

Abstract: A process is set forth for the production of a carbon monoxide stream from a feed stream comprising carbon monoxide, hydrogen, carbon dioxide, methane, nitrogen and moisture. The process comprises contacting the feed stream at elevated pressure with a layered adsorbent bed comprising (i) a pretreatment adsorbent in order to adsorb moisture preferentially over methane, nitrogen and carbon dioxide and (ii) a main adsorbent in order to adsorb carbon monoxide preferentially over hydrogen, carbon dioxide, methane and nitrogen. A key to the present invention is that a carbon-based adsorbent is used as the pretreatment adsorbent.

Abstract: The present invention is a process for adsorbing carbon dioxide from a carbon dioxide containing gas mixture comprising contacting the gas mixture with an activated carbon adsorbent having a density in the range of approximately 0.56 to 0.61 g/cc (35 to 38 lbs./ft.sup.3) and adsorbing the carbon dioxide on the activated carbon adsorbent.

Abstract: A carbonaceous adsorbent membrane is prepared by contacting a hydrophobic carbonaceous adsorbent membrane with an aqueous solution of one or more oxidizing acids and one or more metals selected from the group consisting of copper (+2), chromium (+3), and nickel (+2). The treated membrane is rinsed and dried to yield a hydrophilic carbonaceous adsorbent membrane which is useful for removing water from water-containing gas mixtures.

Abstract: An adsorbent and method for removing water from gaseous HCl. MgCl.sub.2 supported on an activated carbon or silica gel substrate activated by heating to a temperature between 150.degree. C. (302.degree. F.) and 300.degree. C. (572.degree. F.) under vacuum will remove water at partial pressures of below 0.5 torr. Activation of the MgCl.sub.2 supported adsorbent can also be effected by heating the adsorbent between 270.degree. C. (518.degree. F.) and 400.degree. C. (752.degree. F.) under nitrogen.

Abstract: A process for removing nitrogen oxides, as well as water and carbon dioxide, from gas streams containing at least 0.2 ppm by volume of nitrogen oxides by passing the gas stream through an alumina adsorbent and a zeolite adsorbent, preferably 13X-zeolite. The process has utility in front end cleanup of air prior to cryogenic distillation of the air where nitrogen oxides would otherwise freeze under the cryogenic processing.

Abstract: A pressure swing adsorption process for absorbing CO.sub.2 from a gaseous mixture containing CO.sub.2 comprising introducing the gaseous mixture at a first pressure into a reactor containing a modified alumina adsorbent maintained at a temperature ranging from 100.degree. C. and 500.degree. C. to adsorb CO.sub.2 to provide a CO.sub.2 laden alumina adsorbent and a CO.sub.2 depleted gaseous mixture and contacting the CO.sub.2 laden adsorbent with a weakly adsorbing purge fluid at a second pressure which is lower than the first pressure to desorb CO.sub.2 from the CO.sub.2 laden alumina adsorbent. The modified alumina adsorbent which is formed by depositing a solution having a pH of 3.0 or more onto alumina and heating the alumina to a temperature ranging from 100.degree. C. and 600.degree. C., is not degraded by high concentrations of water under process operating conditions.

Abstract: A process and apparatus for drying and removing carbon dioxide from a hydrogen and carbon monoxide containing synthesis gas by using adsorption vessels containing a first layer of 13 X-zeolite and a second layer of 3 A-zeolite in which the 3 A-zeolite precludes the formation of water of reaction when dry and carbon dioxide-free synthesis gas is used to regenerate the adsorption vessel countercurrent to feed flow of the synthesis gas.

Abstract: In the purification of air to remove water and carbon dioxide and other contaminants prior to cryogenic separation of oxygen and nitrogen, water and carbon dioxide are adsorbed on a solid adsorbent and are periodically desorbed to regenerate the adsorbent by the passing of a heated regenerating gas such that the quantity of heat added to the regenerating gas to produce desorption is no more than 90 percent of the heat of adsorption liberated during the adsorption of the water and carbon dioxide. The process is applicable to removing other contaminants from other gas streams also.

Abstract: Temperature swing adsorption to remove CO.sub.2 from a gas stream is conducted using alumina to adsorb all the water and at least most of the carbon dioxide from the gas stream. Optionally a downstream zone of zeolite may be provided to remove further carbon dioxide and hydrocarbons.

Abstract: A process is set forth for the selective removal of water, CO.sub.2, ethane and C.sub.3 + hydrocarbons from gas streams, particularly a natural gas stream comprising primarily methane. The process comprises contacting the gas stream with an adsorbent material consisting exclusively of one or more compounds which are basic (i.e. compounds which, when contacted with a pH neutral aqueous solution, cause such solution to have a pH greater than 7.0) and which are mesoporous (i.e. compounds which have moderately small pores providing a surface area less than 500 m.sup.2 /g). The key to the present invention is the use of a single homogenous adsorbent without sacrificing performance. Typical mesoporous adsorbents which are useful in the present invention include zinc oxide, magnesium oxide and, in particular, activated alumina.