Tpc Group LLC

Uop Lcc

Jillian M Horn

Joseph G Duff

Michael O Nutt

Clifford Alan Maat

John Joseph Senetar

Mark P Kaminsky

Liana Caciula

Charles P Luebke

Dana K Sullivan

Jeannie Mee Blommel

George Pappas

Robert P Adams

Robert Z Confair

Gus K Georgeton

Clifford A Maat

John J Senetar

The process to recover heat in oxidative dehydrogenation of butene to butadiene is presented. The process utilizes heat recovered in oxidative dehydrogenation of butene to butadiene to generate steam. The process utilizes the circulated water stream generated in oxidative dehydrogenation of butene to butadiene for steam generation. A feedstream comprising butene is mixed with steam and preheated air at the inlet of the oxidative dehydrogenation reactor.

Heat recovery in the process of production of butadiene

A process is presented for the production of butadienes. The process includes the separation of oxygenates from the product stream from an oxidative dehydrogenation reactor. The process includes quenching the product stream and solvent and oxygenates from the product stream. The oxygenates are stripped from the solvent with an inert gas to reduce the energy consumption of the process, and the solvent is recycled and reused in the process.

Use of C4 absorber overhead for stripping aldehydes

A process is presented for the oxidative dehydrogenation of butenes to butadienes. The process includes the use of parallel reactors, wherein the reactors are operated at different pressures. A butene feedstream is split into several portions wherein each portion is passed to a different reactor. Each reactor generates an effluent stream, and the effluent stream is cooled to generate steam for use in a lower pressure reactor.

Staged pressure for butadiene reactors to enhance energy recovery

A method of oxidatively dehydrogenating a n-butenes to butadiene includes oxidatively dehydrogenating dehydrogenation reactant in a first adiabatic, catalytic reaction zone to provide a first-stage effluent stream enriched in butadiene at a first-stage effluent temperature above the first-stage inlet temperature, cooling the first-stage effluent stream in a first heat transfer zone to a second-stage inlet temperature lower than said first-stage effluent temperature to provide a second gaseous feed stream comprising superheated steam, n-butene and butadiene, wherein the second stage inlet temperature is lower than said first stage effluent temperature and oxidatively dehydrogenating n-butene in the second stream to provide a product stream further enriched in butadiene at a second stage effluent temperature above said second-stage inlet temperature. The first reaction zone temperature rise and the second reaction zone temperature rise are at least 200&#xb0; F. (111&#xb0; C.) and the first heat transfer zone temperature reduction is at least 50% of the value of the first reaction zone temperature rise.

High throughput oxidative dehydrogenation process

A method of oxidatively dehydrogenating a dehydrogenation reactant includes providing a first gaseous feed stream to a first adiabatic, catalytic reaction zone with less than a stoichiometric amount of oxygen and superheated steam, oxidatively dehydrogenating dehydrogenation reactant in said first adiabatic, catalytic reaction zone and subsequently cooling the effluent, adding additional oxygen and reacting the effluent stream in at least one subsequent adiabatic reaction zone. The dehydrogenation system enables higher conversion and yield per pass and in some cases greatly reduces steam usage and energy costs. In a preferred integrated process, ethylene is converted to n-butene which is then oxidatively dehydrogenated to butadiene.

Multi-stage oxidative dehydrogenation process with inter-stage cooling

The present invention discloses a process to treat a ferrite based catalyst useful in the oxidative dehydrogenation of monololefins and diolefins which process includes a preheat step prior to use of the catalyst in the OXO-D reactor. The catalyst is preferably a zinc ferrite catalyst for the production of butadiene. It has been observed that substantially no nitrogen oxide emissions result from the use of this treated catalyst in the reactor unit during the oxidative dehydrogenation reaction.

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Oxidative dehydrogenation includes: (a) providing a gaseous feed stream to a catalytic reactor, the feed stream comprising a dehydrogenation reactant, oxygen, superheated steam, hydrocarbon moderator gas and optionally nitrogen, wherein the molar ratio of moderator gas to oxygen in feed stream is typically from 4:1 to 1:1 and the molar ratio of oxygen to nitrogen in the feed stream is at least 2; (b) oxidatively dehydrogenating the reactant in the reactor to provide a dehydrogenated product enriched effluent product stream; and (c) recovering dehydrogenated product from the effluent product stream. One preferred embodiment is a process for making butadiene including dimerizing ethylene to n-butene in a homogeneous reaction medium to provide a hydrocarbonaceous n-butene rich feed stream and oxidatively dehydrogenating the n-butene so formed.

Oxidative dehydrogenation process with hydrocarbon moderator gas and reduced nitrogen feed

Disclosed herein is a process for the regeneration of oxidative dehydrogenation (OXO-D) catalyst in an alternate or separate regeneration reactor by employing controlled steam:air and time/pressure/temperature conditions. The process avoids destruction of the catalyst, and wear/tear on an OXO-D reactor. The regenerated catalyst is an iron based oxide catalyst which can be zinc or zinc-free. The iron based oxide catalyst is regenerated in the regeneration reactor by feeding an air/steam stream over a set amount of time, preferably about 6 days to yield a regenerated OXO-D catalyst. The regenerated catalyst is activated and re-utilized to produce butadienes.

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Decatur, GA, United States of America

Jillian M Horn