Abstract: A method that includes (a) providing a stream containing ethane and oxygen to an ODH reactor; (b) converting a portion of the ethane to ethylene and acetic acid in the ODH reactor to provide a stream containing ethane, ethylene, acetic acid, oxygen and carbon monoxide; (c) separating a portion of the acetic acid from the stream to provide an acetic acid stream and a stream containing ethane, ethylene, oxygen and carbon monoxide; (d) providing the stream to a CO Oxidation Reactor containing a catalyst that includes a group 11 metal to convert carbon monoxide to carbon dioxide and reacting acetylene to produce a stream containing ethane, ethylene and carbon dioxide; and (e) providing a portion of the stream and a portion of the acetic acid stream to a third reactor containing a catalyst that includes a metal selected from group 10 and group 11 metals to produce vinyl acetate.

Abstract: A fixed bed reactor system for the oxidative dehydrogenation of ethane, comprising a catalyst bed wherein the catalyst capacity profile increases along the length of catalyst bed from the upstream end to the downstream end. The catalyst bed may include one or more sections, across one or more fixed bed reactors, that are identified by a change in catalyst capacity. Catalyst capacity, or the ability to convert ethane into ethylene, may be altered by changing the dilution ratio, void fraction, and or the 35% conversion temperature. A method for loading a fixed bed reactor with an increasing catalyst capacity is also described.

Abstract: Embodiments described in examples herein provide methods and systems for increasing a yield from an oxidative dehydrogenation (ODH) reactor. An exemplary method includes controlling a temperature of a feed gas composition at less than 250° C. The feed gas composition is flowed through a feed preheater to form a heated feed gas, wherein in the feed preheater the feed gas composition is heated to between 150° C. and 250° C. The heated feed gas is flowed into the ODH reactor less than 15 seconds after leaving the feed preheater.

Abstract: The present disclosure relates to limiting the production of acetic acid in an oxidative dehydrogenation process to convert ethane to ethylene. The process of oxidative dehydrogenation includes feeding acetic acid, along with ethane and oxygen into an oxidative dehydrogenation reactor where contact with a catalyst leads to conversion of the ethane into ethylene and acetic acid. By including acetic acid in the feed, the amount of acetic acid produced may be limited and the ratio of ethylene produced to ethane consumed may increase.

Abstract: A method of converting one or more alkanes to one or more alkenes that includes providing a first stream containing one or more alkanes and oxygen to an oxidative dehydrogenation reactor; converting at least a portion of the one or more alkanes to one or more alkenes in the oxidative dehydrogenation reactor to provide a second stream exiting the oxidative dehydrogenation reactor containing one or more alkanes, one or more alkenes, and one or more of oxygen, carbon monoxide and acetylene; and providing the second stream to a second reactor containing a catalyst that includes CuO and ZnO and reacting the second stream to provide a third stream exiting the second reactor containing one or more alkanes, one or more alkenes, and lower or undetectable levels of oxygen and acetylene compared to the second stream.

Abstract: A method that includes (a) providing a stream containing ethane and oxygen to an ODH reactor; (b) converting a portion of the ethane to ethylene and acetic acid in the ODH reactor to provide a stream containing ethane, ethylene, acetic acid, oxygen and carbon monoxide; (c) separating a portion of the acetic acid from the stream to provide an acetic acid stream and a stream containing ethane, ethylene, oxygen and carbon monoxide; (d) providing the stream to a CO Oxidation Reactor containing a catalyst that includes a group 11 metal to convert carbon monoxide to carbon dioxide and reacting acetylene to produce a stream containing ethane, ethylene and carbon dioxide; and (e) providing a portion of the stream and a portion of the acetic acid stream to a third reactor containing a catalyst that includes a metal selected from group 10 and group 11 metals to produce vinyl acetate.

Abstract: Oxidative dehydrogenation is an alternative to the energy extensive steam cracking process presently used for the production of olefins from paraffins, but has not been implemented commercially partially due to the unstable nature of hydrocarbon/oxygen mixtures, and partially due to the cost involved in the construction of new facilities. An oxidative dehydrogenation chemical complex designed to reduce costs by including integration of an oxygen separation module that also addresses safety concerns and reduces emission of greenhouse gases is described.

Abstract: Oxidative dehydrogenation is an alternative to the energy extensive steam cracking process presently used for the production of olefins from paraffins, but has not been implemented commercially partially due to the unstable nature of hydrocarbon/oxygen mixtures, and partially due to the cost involved in the construction of new facilities. An oxidative dehydrogenation chemical complex designed to reduce costs by including integration of an oxygen separation module that also addresses safety concerns and reduces emission of greenhouse gases is described.

Abstract: Oxidative dehydrogenation is an alternative to the energy extensive steam cracking process presently used for the production of olefins from paraffins, but has not been implemented commercially partially due to the unstable nature of hydrocarbon/oxygen mixtures, and partially due to the cost involved in the construction of new facilities. An oxidative dehydrogenation chemical complex designed to reduce costs by including integration of an oxygen separation module that also addresses safety concerns and reduces emission of greenhouse gases is described.

Abstract: Oxidative dehydrogenation is an alternative to the energy extensive steam cracking process presently used for the production of olefins from paraffins, but has not been implemented commercially partially due to the unstable nature of hydrocarbon/oxygen mixtures, and partially due to the cost involved in the construction of new facilities. An oxidative dehydrogenation chemical complex designed to reduce costs by including integration of an oxygen separation module that also addresses safety concerns and reduces emission of greenhouse gases is described.

Abstract: A valve and method for use is provided. The valve has a valve body having an outer perimeter and an inner perimeter defining a flow path therethrough. The valve has a closure member within the inner perimeter configured to selectively close and open the flow path. The valve has a valve seat located at least partially within the inner perimeter and configured to engage a portion of the closure member when the closure member is in a closed position. The valve has a stem configured to support the closure member within the flow path wherein a portion of the stem has an actuator offset. The valve has a bearing pedestal configured to support the stem. The valve has a closure member-stem connector configured to rotationally couple the closure member to the stem while allowing the closure member to move relative to the stem along a longitudinal axis of the stem.

Abstract: An actuator for a valve assembly is provided. The actuator has an actuator body and at least one piston configured to travel within the actuator body. The actuator has an output shaft located at least partially within the actuator body and configured to couple to a valve stem of a valve wherein the output shaft has a plurality of teeth protruding from a pinion. The actuator has at least one rack configured to move with each of the at least one piston, the rack having a piston end and a terminal end and wherein the rack has a plurality of rack teeth configured to engage the plurality of teeth on the output shaft. The terminal end of the rack is configured to be maintained a minimum distance beyond an engagement point, wherein the engagement point is located between the rack teeth and the teeth in all operating positions.