Uop Lcc

Union Carbide Corporation

Chevron Research Company

Chevron Research & Technology Company

Mark T Staniulis

Regis J Pellet

Peter K Coughlin

Jule A Rabo

Gary N Long

Robert L Chiang

Albert S Behan

Alan P Risch

Stephen R Dunne

Donald Henry Mohr

Alan P Cohen

Charles R Wilson

Donald F Best

James G Vassilakis

Jenny L Pai

Douglas E Crozier

Charles P Wilson

A process and apparatus for the recovery and purification of a contaminated refrigerant withdrawn from a refrigeration or refrigerant recovery system which employs a compressor and an adsorbent selective for the adsorption of halogenated hydrocarbons. The adsorbent is selected from the group consisting of silicalite, faujasites, steamed and rare earth exchanged zeolite Y, mordenite, ZSM-5 and mixtures thereof, and more particularly the group consisting of a low cerium rare earth exchanged zeolite Y-84, a low cerium rare earth exchanged zeolite LZ-210, Breck Structure Six, ECR-32, and mixtures thereof. A significant increase in the capacity of these adsorbents over conventional adsorbents combined with the use of novel process steps to recover, purify and return a purified refrigerant to the refrigeration system result in significant cost savings at reduced risk of release of halogenated hydrocarbons to the environment.

Recovery and purification of refrigerants

Process for recovery and purification of refrigerants with solid sorbents

Reforming to produce aromatics from aliphatics, using a bond zeolite catalyst containing a Group VIII metal such as platinum, has been found to be extremely sensitive to water, even at water concentrations as low as 3 ppm in the feed, unless certain catalysts having a low water sensitivity index are used. The water sensitivity index (WSI) is described and methods for making catalysts with a low WSI are described. The sulfur content of the feed to the reforming/aromatics production process is preferably below 50 parts per billion. The catalysts used in the reforming process is preferably a high crush strength catalyst and is preferably prepared by steps including treating L zeolite with a binding enhancement agent prior to binding with a binder such as silica, silica/alumina or alumina.

Reforming using a bound zeolite catalyst

Normal methods of impregnating silicalite with noble metals leads either to metal loadings under 8% at high (greater than 60%) dispersion or loading of over 8% noble metal at low dispersion. To obtain silicalite impregnated with a noble metal at more than 8 weight percent loading and with at least 60% dispersion it has been found necessary to pretreat the silicalite with a base and to impregnate the base treated silicalite with a noble metal compound in two stages separated by calcination. Platinized silicalite so prepared may be dispersed in a poly(tetrafluoroethylene) matrix and used as a fixed bed to catalyze isotopic exchange gaseous hydrogen and water vapor arising from a mass of liquid water flowing over the fixed catalyst bed.

Noble metal exchange of hydrophobic molecular sieves

Cracking catalysts and their use in cracking processes are disclosed. The cracking catalyst are prepared using mixtures of catalytic cracking catalysts and selected silicoaluminophosphate molecular sieves of U.S. Pat. No. 4,440,871.

Catalytic cracking catalysts and cracking process using mixed catalyst

This invention relates to a method for catalytically reducing one or more nitrogen oxides from a gaseous stream containing one or more nitrogen oxides and one or more sulfur oxides which comprises contacting said gaseous stream and ammonia with a microporous non-zeolitic molecular sieve composition at effective reduction conditions, wherein said microporous non-zeolitic molecular sieve composition is (i) optionally acid treated with an inorganic or organic acid, (ii) hydrogen-forming cation exchanged and (iii) optionally metal cation exchanged, prior to said contacting in said method.

Catalytic reduction of nitrogen oxides

This invention relates to a method for catalytically reducing one or more nitrogen oxides from a gaseous stream containing one or more nitrogen oxides and optionally one or more sulfur oxides which comprises contacting said gaseous stream and ammonia with a microporous molecular sieve composition at effective reduction conditions in which the amount of ammonia in said method is excessive over the stoichiometric amount necessary for catalytically reducing one or more nitrogen oxides from said gaseous stream, wherein said microporous molecular sieve composition is (i) optionally acid treated with an inorganic or organic acid, (ii) hydrogen-forming cation exchanged and (iii) optionally metal cation exchanged, prior to said contacting in said method, and wherein at least a portion of excessive ammonia in said method is oxidized without substantial adverse effect on catalytically reducing one or more nitrogen oxides from said gaseous stream.

Catalytic cracking catalysts and their use in catalytic cracking processes are disclosed. The instant catalytic cracking catalysts are useful for cracking a hydrocarbon feedstock to produce lower boiling hydrocarbons. The catalysts comprise an effective amount of at least one non-zeolitic molecular sieve characterized in its calcined form by an adsorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20.degree. C. The non-zeolitic molecular sieve is characterized as containing framework tetrahedral components of aluminum and phosphorus and at least one additional framework tetrahedral component, e.g., the non-zeolitic molecular sieve may be a silicoaluminophosphate as described in U.S. Pat. No. 4,440,871.

Catalytic cracking catalysts and cracking process using non-zeolitic

A method for enhancing the binding of certain negatively surface charged molecular sieves to a silica binder is disclosed. As modified, molecular sieves having enhanced binding characteristics are also taught.

Silica bonding of molecular sieves

Catalytic cracking processes utilizing selected specific silicoaluminophosphate molecular sieves of U.S. Pat. No. 4,440,871. Processes using such catalysts provide product mixtures different from those obtained by use of catalysts based on zeolitic aluminosilicates. In preferred embodiments, SAPO-37 is utilized.

Catalytic cracking process using silicoaluminophosphate molecular sieves

Reforming to produce aromatics from aliphatics, using a bound zeolite catalyst containing a Group VIII metal such as platinum, has been found to be extremely sensitive to water, even at water concentrations as low as 3 ppm in the feed, unless certain catalysts having a low water sensitivity index are used. The water sensitivity index (WSI) is described and methods for making catalysts with a low WSI are described. The sulfur content of the feed to the reforming/aromatics production process is preferably below 50 parts per billion. The catalyst used in the reforming process is preferably a high crush strength catalyst and is preferably prepared by steps including treating L zeolite with a binding enhancement agent prior to binding with a binder such as silica, silica/alumina or alumina.

Cracking catalysts and their use in cracking processes are disclosed. The cracking catalysts are prepared using novel non-zeolitic molecular sieves and, optionally, traditional zeolitic aluminosilicate cracking components.

Catalytic cracking catalysts comprising non-zeolitic molecular sieves

Catalytic cracking catalysts, the process of their preparation and the process of their use. Cracking catalysts are disclosed for improving the octane number of gasoline products. The catalysts comprise a zeolitic aluminosilicate having a mole ratio of oxides in the dehydrated state of

Catalytic cracking catalysts for high octane gasoline products

Cracking catalysts and their use in cracking processes are disclosed. The cracking catalyst are prepared using mixtures of catalytic cracking catalysts containing zeolitic aluminosilicates effective in catalytic cracking and selected silicoaluminophosphate molecular sieves of U.S. Pat. No. 4,440,871.

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Peekskill, NY, United States of America

Mark T Staniulis