Abstract: This invention is directed to a process for producing olefin product from an oxygenate feed that includes dimethyl ether (DME). The process uses an olefin forming catalyst that contains a porous crystalline material, preferably a porous crystalline aluminosilicate molecular sieve material. The process produces high quantities of light olefin (i.e., ethylene, propylene, and mixtures thereof).

Abstract: Disclosed herein is a method of recovery of the activity of a molecular sieve catalyst following use of the catalyst in an OTO conversion process. This is achieved by a regeneration apparatus and a method of regenerating a molecular sieve catalyst, comprising two stages. In a pretreatment stage, the catalyst is pretreated under pretreatment conditions by heating the catalyst to a temperature of between 320° C. to 700° C. in an oxygen depleted medium for a residence time of between 1 minute to two hours; and, in a regeneration stage, the catalyst is regenerated under regeneration conditions by heating the catalyst at a temperature of between 200° C. to 700° C. in an oxidizing medium for a residence time of between 1 to 60 minutes.

Abstract: This invention is directed to a method for determining a source of carbon feed used in manufacturing product produced from the carbon feed. The invention further provides a method for tracking products, particularly MTO products, derived from a particular carbon feed. In general, the method involves a variety of steps that include one or more of determining, comparing, inventorying, and tracking the 13C:12C ratio (or HD:H2 ratio) of the product that is being tracked to the measured or predetermined 13C:12C ratio (or HD:H2 ratio) of the feed used to make the product.

Abstract: Disclosed herein is a method of controlling production of olefins in an oxygenates-to-olefins reaction by combining in a reactor methanol and a molecular sieve, a AlPO or SAPO in certain embodiments, under conditions to produce at least ethylene and propylene having a first ethylene/propylene ratio; adding to the reactor a first amount of a C1 to C5 aldehyde; and withdrawing from the reactor a first amount of ethylene and propylene having a second ethylene/propylene ratio, wherein the second ethylene/propylene ratio is greater than the first ethylene/propylene ratio. The aldehyde is added at the same time, or co-feed, with the methanol under the same reaction conditions.

Abstract: This invention is to a process for separating condensed water and entrained solids from an olefin stream so that fouling of the separation equipment by the entrained solids is reduced or eliminated. The process involves injecting an antifouling agent into a water condensing or quench system in an amount to maintain a zeta potential of fouling liquid and a zeta potential of the surface of the quench system both in a positive range or both in a negative range.

Abstract: Disclosed herein is a method of recovery of the activity of a molecular sieve catalyst following use of the catalyst in an OTO conversion process. This is achieved by a regeneration apparatus and a method of regenerating a molecular sieve catalyst, comprising two stages. In a pretreatment stage, the catalyst is pretreated under pretreatment conditions by heating the catalyst to a temperature of between 320° C. to 700° C. in an oxygen depleted medium for a residence time of between 1 minute to two hours; and, in a regeneration stage, the catalyst is regenerated under regeneration conditions by heating the catalyst at a temperature of between 200° C. to 700° C. in an oxidizing medium for a residence time of between 1 to 60 minutes.

Abstract: Disclosed herein is a method of converting oxygenates to olefins comprising contacting an oxygenate stream with an acidic high silica chabazite catalyst in one or more oxygenate-to-olefins reactors; circulating greater than from 80% of the catalyst to one or more catalyst regenerators to form regenerated catalyst; circulating the regenerated catalyst, preferably the same amount of regenerated catalyst, back to the oxygenate-to-olefins reactor to contact an oxygenate stream; and isolating a stream of olefins from the one or more oxygenate-to-olefins reactors.

Abstract: In a method of synthesizing an aluminophosphate or silicoaluminophosphate molecular sieve, a synthesis mixture is prepared by mixing a plurality of starting materials including at least a source of water, a source of phosphorus, a source of aluminum, optionally, a source of silicon and, and at least one organic directing agent for directing the formation of said molecular sieve. The starting materials are maintained at a temperature between 25° C. and 50° C., preferably between 30° C. and 45° C., during the mixing and until preparation of the starting mixture is complete, whereafter the synthesis mixture is heated to a crystallization temperature between about 100° C. and about 350° C. until crystals of the molecular sieve are produced. When crystallization is complete, the molecular sieve is recovered.

Abstract: The present invention relates to a method for converting a feed including an oxygenate to a product including a light olefin. In particular, this invention relates to converting an oxygenate feedstock with a silicoaluminophosphate catalyst to a product including a light olefin in a reaction apparatus. More particularly, this invention provides a means by which an optimum level of coke can be determined and utilized to generate an optimum or near-optimum yield of light olefins such as ethylene and propylene in a oxygenates to olefins system.

Abstract: This invention is to a process for separating condensed water and entrained solids from an olefin stream so that fouling of the separation equipment by the entrained solids is reduced or eliminated. The process involves injecting an antifouling agent into a water condensing or quench system in an amount to maintain a zeta potential of fouling liquid and a zeta potential of the surface of the quench system both in a positive range or both in a negative range.

Abstract: A crystalline microporous silicoaluminophosphate (SAPO) molecular sieve is prepared by: (a) providing a reaction mixture having a molar composition within the following ranges: P:Al from 0.75 to 1.25, Si:Al2 from 0.01 to 0.32, H2O:Al2 from 25 to 50, and R:Al2 from 1 to 3, where R designates a structure directing agent (template), and wherein the molar ratios for the aluminum, phosphorus, and silicon sources are calculated based on the oxide forms; (b) heating the mixture to a crystallization temperature of between 150° C. to 250° C. to form the crystalline molecular sieve within the reaction mixture; and (c) following crystallization in step (b), aging the crystalline molecular sieve in an alkaline liquid at a temperature below the crystallization temperature from 0.5 hour for up to 120 hours. Aging can affect both catalyst life and catalyst activity.

Abstract: In a method of synthesizing an aluminophosphate or silicoaluminophosphate molecular sieve, a synthesis mixture is prepared by mixing a plurality of starting materials including at least a source of water, a source of phosphorus, a source of aluminum, optionally, a source of silicon and, and at least one organic directing agent for directing the formation of said molecular sieve. The starting materials are maintained at a temperature between 25° C. and 50° C., preferably between 30° C. and 45° C., during the mixing and until preparation of the starting mixture is complete, whereafter the synthesis mixture is heated to a crystallization temperature between about 100° C. and about 350° C. until crystals of the molecular sieve are produced. When crystallization is complete, the molecular sieve is recovered.

Abstract: In a method of synthesizing an aluminophosphate or silicoaluminophosphate molecular sieve, a synthesis mixture is prepared by mixing a plurality of starting materials including at least a source of water, a source of phosphorus, a source of aluminum, optionally, a source of silicon and, and at least one organic directing agent for directing the formation of said molecular sieve. The starting materials are maintained at a temperature between 25° C. and 50° C., preferably between 30° C. and 45° C., during the mixing and until preparation of the starting mixture is complete, whereafter the synthesis mixture is heated to a crystallization temperature between about 100° C. and about 350° C. until crystals of the molecular sieve are produced. When crystallization is complete, the molecular sieve is recovered.

Abstract: This invention is directed to a method for determining a source of carbon feed used in manufacturing product produced from the carbon feed. The invention further provides a method for tracking products, particularly MTO products, derived from a particular carbon feed. In general, the method involves a variety of steps that include one or more of determining, comparing, inventorying, and tracking the 13C:12C ratio (or HD:H2 ratio) of the product that is being tracked to the measured or predetermined 13C:12C ratio (or HD:H2 ratio) of the feed used to make the product.

Abstract: This invention is to a process for separating condensed water and entrained solids from an olefin stream so that fouling of the separation equipment by the entrained solids is reduced or eliminated. The process involves injecting an antifouling agent into a water condensing or quench system in an amount to maintain a zeta potential of fouling liquid and a zeta potential of the surface of the quench system both in a positive range or both in a negative range.

Abstract: This invention is to a process for separating condensed water and entrained solids from an olefin stream so that fouling of the separation equipment by the entrained solids is reduced or eliminated. The process involves injecting an antifouling agent into a water condensing or quench system in an amount to maintain a zeta potential of fouling liquid and a zeta potential of the surface of the quench system both in a positive range or both in a negative range.

Abstract: This invention is directed to a process for producing olefin product from an oxygenate feed that includes dimethyl ether (DME). The process uses an olefin forming catalyst that contains a porous crystalline material, preferably a porous crystalline aluminosilicate molecular sieve material. The process produces high quantities of light olefin (i.e., ethylene, propylene, and mixtures thereof).

Abstract: In a method of synthesizing an aluminophosphate or silicoaluminophosphate molecular sieve, a synthesis mixture is prepared by mixing a plurality of starting materials including at least a source of water, a source of phosphorus, a source of aluminum, optionally, a source of silicon and, and at least one organic directing agent for directing the formation of said molecular sieve. The starting materials are maintained at a temperature between 25° C. and 50° C., preferably between 30° C. and 45° C., during the mixing and until preparation of the starting mixture is complete, whereafter the synthesis mixture is heated to a crystallization temperature between about 100° C. and about 350° C. until crystals of the molecular sieve are produced. When crystallization is complete, the molecular sieve is recovered.

Abstract: A process for reforming a hydrocarbon feed containing precursors of ethylbenzene, e.g., C8 isoalkane and/or C8 isoalkene precursors of ethylbenzene, that results in the formation of reduced amounts of ethylbenzene. The process is carried out in a catalytic reforming unit comprised of a plurality of operatively connected reactors comprising at least one lead reforming reactor and a tail reforming reactor. The process is carried out by reforming the feed in at least one lead reactor which contains a first reforming catalyst and a catalyst effective for converting ethylbenzene and further reforming the product of the lead reactor in the tail reactor that contains a second reforming catalyst.

Abstract: A process for selectively producing para-xylene from a feedstock enriched in C8 isoalkanes and/or isoalkenes is disclosed. The feed is contacted with Group VIII metal loaded molecular sieve catalyst of low acidity under dehydrocyclization conditions wherein the molecular sieve has a channel size ranging from about 5-8 Angstroms and a 10 to 12 membered ring structure containing at least two elements selected from the group consisting of Si, Al, P, Ge, Ga and Ti.