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Tpc Group LLC

Honeywell International Inc.

Hyradix Incorporated

John Joseph Senetar

Richard A Johnson, Ii

Joseph A Montalbano

Gavin Paul Towler

Lawrence W Miller

Daniel A Kauff

Kurt M Vanden Bussche

Jillian M Horn

Bryan K Glover

Andrea G Bozzano

Kishore J Doshi

Joseph G Duff

Clifford Alan Maat

Hsueh Sung Tung

Daniel C Merkel

Paolo Palmas

David A Wegerer

Robert L Mehlberg

Stephen A Cottrell

Haluk Kopkalli

Yuon Chiu

Lev Davydov

Joseph Edward Zimmermann

Linda Shi Cheng

Wolfgang A Spieker

Michael O Nutt

Dale James Shields

Guy B Woodle

Michael A Stine

Mark M Davis

Jeannie Mee Blommel

Joseph H Gregor

John R Harness

Ernest James Boehm

Christopher R Schindlbeck

Nasim Ghazinoor

Charles P Luebke

Ian G Horn

Steven Lee Krupa

Sathit Kulprathipanja

Avram Michael Buchbinder

Wei Pan

Timur V Voskoboynikov

Christopher D DiGiulio

Robert J Sanger

Adam J Kanyuh

Paul C Steacy

Dana K Sullivan

Matthew C Cole

Daniel R Sioui

Joe R Haas

Andrew B Chin

Yogesh Kumar Gupta

Christopher Procopi

Robert P Adams

Gary S Sandhu

Gurjit S Sandhu

Aleksey Y Pelekh

Benjamin F Ketter

Michael J Tobin

Andrew Piotrowski

Jillian Marie Horn

Sterling T Miller

A fluidized catalytic reactor connected to a start-up heater is provided. The start-up heater provides sufficient heat to a catalyst containing stream to gradually increase the feed temperature. This allows for a critical volumetric flow rate to be achieved so that catalyst can be recovered from product instead of being entrained in product.

Process and apparatus for reacting feed with a fluidized catalyst with a reduction in catalyst loss during startup

A process for preparing an olefin stream for oligomerization comprises fractionating an olefin stream to provide a light gas stream and an olefin rich stream. Oxygenates are absorbed from the olefin rich stream into a water wash stream to provide an oxygenate rich water wash stream and a washed olefin stream. The washed olefin stream can then be oligomerized.

Process for preparing an olefin stream for oligomerization with water wash

A process for preventing hazardous conditions at startup and shutdown of a reactor by sending an inert gas such as nitrogen to strip entrained oxygen from the catalyst when reactor temperatures are below about 240° C. During normal operation the entrained oxygen reacts with hydrocarbons to produce oxides but at the lower temperatures that are present at startup or shutdown these reactions do not occur sufficiently leaving oxygen that can cause hazardous conditions as temperatures increase upon startup. When the temperature is in the safe operating zone above 240° C., the nitrogen gas is stripped by air or other oxygen containing gas.

Stripping of regenerated catalyst during start-up and shutdown

A fluidized catalytic reactor system cycles from 0.05-5% of catalyst at a time through a rejuvenation unit to be heated in the presence of oxygen to maintain catalyst activity. The use of the rejuvenation unit that may be 2% of the size of the main catalyst regeneration unit allows for reduction in equipment size and in catalyst inventory. The catalyst that is sent to the rejuvenation unit may be spent catalyst but may be partially or fully regenerated catalyst. The rejuvenation unit may be heated by combusting fuel or by hot flue gas.

Regeneration of a dehydrogenation catalyst slip-stream

A process and apparatus for indirect heating of catalyst in the regeneration zone is disclosed. A hot flue gas flows within a heating tube and the catalyst to be heated flows outside the heating tube. The hot flue gas is generated by igniting a fuel stream. The hot flue gas is generated directly in the heating tube or is generated in a separate burner outside the heating tube.

Process and apparatus for indirect catalyst heating

A composition of fuel gas that when mixed with spent catalyst and oxygen has an induction time that allows bubbles to break up while combusting in the regenerator. Bubble breakage in a dense bed avoids generation of a flame that can generate hot spots in the regenerator which can damage equipment and catalyst. The fuel gas can be obtained from paraffin dehydrogenation products, so it can sustain operation of the unit even in remote locations. Heavier streams can be mixed with lighter streams to obtain a fuel gas composition with a desirable induction time to avoid such hot spots. Mixing of a depropanizer bottom stream and/or deethanizer overhead stream with lighter gas streams such as cold box light gas or PSA tail gas can provide the desired fuel gas composition.

Process for recycling supplemental fuel for regenerating catalyst

A process for recovering catalyst from a fluidized catalytic reactor effluent is disclosed comprising reacting a reactant stream by contact with a stream of fluidized catalyst to provide a vaporous reactor effluent stream comprising catalyst and products. The vaporous reactor effluent stream is contacted with a liquid coolant stream to cool it and transfer the catalyst into the liquid coolant stream. A catalyst lean vaporous reactor effluent stream is separated from a catalyst rich liquid coolant stream. A return catalyst stream is separated from the catalyst rich liquid coolant stream to provide a catalyst lean liquid coolant stream, and the return catalyst stream is transported back to said reacting step.

Process and apparatus for recovering catalyst from a product stream

Higher temperature regenerated dehydrogenation catalyst is mixed with the lower temperature spent dehydrogenation catalyst from a dehydrogenation reaction to heat the spent catalyst. Air or other oxygen containing gas may be introduced to facilitate mixing. The mixing of hot regenerated catalyst with cooler spent catalyst increases the temperature of the spent catalyst and makes the coke on catalyst and in the supplemental fuel gas instantly ready to combust without the delay necessary to heat up the spent catalyst to combustion temperature. The regenerated dehydrogenation catalyst may be mixed with the spent dehydrogenation catalyst before the mixture of catalyst is contacted with the supplemental fuel gas. Combustion with fuel gas should be conditioned to avoid generation of a flame.

Process and apparatus for regenerating catalyst with supplemental fuel

A process and apparatus cool and remove catalyst from a hot vaporous reactor effluent stream by feeding the hot vaporous reactor effluent stream comprising catalyst and a first quench liquid stream to a first quench chamber. The hot vaporous reactor effluent stream is directly contacted with the first quench liquid stream to cool the hot reactor effluent stream and wash catalyst therefrom into the first quench liquid stream. The first quench liquid stream and the vaporous reactor effluent stream are passed together through a bed while disengaging catalyst from the vaporous reactor effluent stream and transferring catalyst into the first quench liquid stream.

Process and apparatus for quenching a reactor effluent stream

A fluidized catalytic reactor utilizes an ascending temperature profile. The apparatus and process deliver cooler spent catalyst to a first catalyst distributor and a hotter regenerated catalyst to a second catalyst distributor that are spaced apart from each other. The reactant stream first encounters the first stream of catalyst and then encounters the second stream of catalyst. The process and apparatus stage the addition of hot catalyst to the reactant stream. The process and apparatus may be particularly advantageous in an endothermic reaction because the hotter catalyst will encounter reactants that have cooled due to the progression of endothermic reactions.

Process and apparatus for reacting feed with a fluidized catalyst over a temperature profile

A process for cracking an olefinic feed comprising diolefins and monoolefins is provided. The process comprises selectively hydrogenating the olefinic feed in a hydrogenation reactor to convert the diolefins to monoolefins to provide a hydrogenated effluent stream. The hydrogenated effluent stream is vaporized to provide a vaporized hydrogenated effluent stream. The vaporized hydrogenated effluent stream is passed to an olefin cracking reactor to provide a cracked olefin stream comprising Cand Colefins. The cracked olefin stream is passed to a recycle column to provide one of an overhead vapor stream comprising Chydrocarbons or a side draw vapor stream comprising C. At least a portion of the overhead vapor stream or the side draw vapor stream is recycled to the olefin cracking reactor.

Process for cracking an olefinic feed comprising diolefins and monoolefins

We have discovered that addition of water to a mixture of oxygenates increases their volatility relative to methanol. A process and apparatus are disclosed for separating methanol from other oxygenates. Water is separated from a stream comprising water, methanol and at least one other oxygenate to provide a water rich stream and a methanol and oxygenate rich stream. The methanol and oxygenate rich stream and water are fed to a column to provide an oxygenate rich stream and a methanol and water extract stream. The methanol and water can then be readily separated from each other.

Process and apparatus for separating methanol from other oxygenates

This present disclosure relates to apparatuses for methylation of aromatics in an aromatics complex for producing a xylene isomer product. More specifically, the present disclosure relates to apparatuses for producing para-xylene by the selective methylation of toluene and/or benzene in an aromatics complex using processed toluene instead of crude toluene.

Apparatuses for mixing of staged methanol injection

A process is presented for the production of butadiene from a mixture of butane/butene feed. The process provides high conversion of the feed by oxidative dehydrogenation of the feed. The process enables recovery of a good portion of heat inputted from the reaction effluent. The process overcomes equilibrium limitations by oxidative dehydrogenation of butane/butene feed to produce butadiene.

Process for butadiene production via oxidative dehydrogenation followed by direct dehydrogenation

Processes and an apparatus for reducing heavy oxygenate recycle for an MTO reaction zone. After separating product and water from the MTO reaction effluent, an oxygenate rich stream is passed to a conversion zone in which methanol in the oxygenate rich stream is converted into DME. A DME rich stream is separated from heavy oxygenates and is recycled back to the MTO reaction zone. The conversion zone may include a reactive distillation column, or the conversion zone may include a reactor vessel and a separate separation vessel.

Processes for reduced oxygenated recycle in an MTO conversion

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Naperville, IL, United States of America

John Joseph Senetar