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Air Company Holdings, Inc.

Zhanping Xu

Pengfei Chen

Brian J Nowak

Nicholas F Urbanski

Steven J Lesniak

Christopher Naunheimer

Kurt A Detrick

Robert L Bunting, Jr

Lubo Zhou

Daniel R Monkelbaan

Sean G Mueller

Robert J Miller

Joseph Agnello

Rebecca Mudrock

Thomas C Heldwein

Aaron J Muck

Robert L Mehlberg

Trung S Pham

Avram Michael Buchbinder

David S Lafyatis

Peter H Shafe

Gregory J Schrad

James G Hagen

Emadoddin Abbasi

Dennis H Bielinski

Robert L Bunting

Daniel R M0nkelbaan

Jihad Mohammed Dakka

Paolo Palmas

Brian W Hedrick

Lev Davydov

Phillip F Daly

Susie C Martins

Sathit Kulprathipanja

Douglas A Nafis

Dennis E O'Brien

Stafford Wheeler Sheehan

Robert J Sanger

Sanford Allan Victor

Christian D Freet

Daniel A Kauff

Thomas J Godry

Eric Leeton

James W Althoff

Mitchell John Kowalczyk

Raymond E Tucker

Chi Chen

Xiaoming Wen

Nicholas W Bridge

Weikai Gu

Kevin J Richardson

Peter J Wantuck

John Christian Maley

Richard S Hatami

Nicholas J Steinke

J Mark Houdek

Ouda Salem

Doug Stewart

Sean Glennon Thomas Mueller

Jagan Reddy

Konstantina Kritikos

Richard Isherwood

Stephanie Fuyue Li

Shree Prakash Pathak

Kevin A Richardson

Matthew J Westby

Andrew J Criscione

Robert L Bunting Jr

G Robert Buntin

Jr Robert L Bunting

Mark J Houdek

Mitchel J Kowalczyk

Daniel R M0NKELBAAN

A dynamic catalytic conversion reactor having a plurality of operating zones is disclosed that adjusts operation based on incoming hydrogen from a fluctuating renewable energy source. The dynamic reactor is configured to turn on and off supply of feed gas to certain zones based on hydrogen supply, and maintains catalyst activity within all operating and idle zones by applying one of a number of gas flow options through the idle zones. Methods and systems of using the dynamic reactor are also disclosed.

Dynamic catalytic conversion reactor and systems and methods using the same

Heat exchangers (also referred to as exchangers herein) are provided that fit within a bottom sump of a distillation column. These heat exchangers may be at least partially submerged in the bottoms fluid of the distillation column so that the exterior surface of the heat exchanger can contribute to the total area of the heat exchanger. The internal configuration of the exchanger allows for annular coaxial flow of the hot fluid (condensing vapor stream) and eliminates the need for top and bottom channel heads.

Vapor distribution system in a concentric reboiler

A high capacity and high efficiency co-current and cross-flow vapor-liquid contacting apparatus and process is useful in distillation columns and other vapor-liquid contacting processes. The apparatus is characterized by an arrangement of contacting modules and perforated receiving pans in horizontal stages. The modules define a co-current contacting volume and in an exemplary configuration the modules include a liquid distributor and a demister. Liquid dispensed from the modules on a perforated receiving pan are contacted with upflowing vapor through perforations therein.

Vapor-liquid contacting apparatus and process with cross contacting

A high capacity and high efficiency vapor-liquid contacting apparatus and process is useful in distillation columns and other vapor-liquid contacting processes. The apparatus is characterized by a half module comprising a downcomer against a shell of a vessel for transporting liquid to a subjacent stage which utilizes a demister to effect vapor-liquid separation at the downcomer outlet.

Vapor-liquid contacting apparatus and process with downcomer at shell

Distillation trays having improved efficiency and capacity are described. The improvement is accomplished with unique downcomer spout arrangements and bubble promoters which provide equal liquid distribution to all areas of the tray. The ratio of the open area of a contacting zone including part of a bubble promoter and associated deck zone over the open area of the downcomer spout zone on the adjacent tray for distributing liquid to the zone is essentially the same across the tray.

Distillation trays

Trays having increased capacity and efficiency are described. The trays have a deck, and downcomers extending through the deck. There are a plurality of bubble promoters on the deck. Each bubble promoter defines a zone on the deck, and the zone has an opening in the deck. The opening is positioned adjacent to a solid support for the tray. The bubble promoters provide areas through which vapor can pass, turning blocked areas of the tray into active areas. Mass transfer columns containing the trays are also described.

Bubble promoter

Hydroprocessing reactor internals height reduction is achieved by placing a mixing chamber above the collection tray. The mixing chamber has spillways on the top (top spillways) and the side of the mixing chamber (side spillways) for fluid entry. The design of the spillways has a significant impact on pressure drop. The pressure drop is reduced by having wide shallow spillways rather than narrow and deep spillways without impacting mixing performance. With both side and top spillways, the height of the mixing chamber can be reduced significantly with minimal impact on fluid mixing and pressure drop.

Compact quench zone reactor internals

The invention involves a scale collection device that is located within downflow reactor head for removing solids from feed streams to increase reactor operating cycle time without impact on effective reactor space for catalyst loading. More particularly, a filtering zone is located in an upper portion of a reactor vessel above a rough liquid distribution tray and a distribution tray.

Scale collection device for downflow reactors

The invention involves a scale collection device that is located within downflow reactor head for removing solids from feed streams to increase reactor operating cycle time without impact on effective reactor space for catalyst loading and reactor pressure drop. More particularly, a scale collection device is in an upper portion of a reactor vessel above a rough liquid distribution tray and a vapor-liquid distribution tray.

The hydroprocessing reactor quench zone internals comprise a collection tray, a mixing chamber, a ring quench distributer, a rough liquid distribution tray, and a vapor-liquid distribution tray. The rough liquid distribution tray has a central pan for receiving vapor and liquid out of the mixing chamber and multiple fluid distribution troughs attached to the central pan that extended radially outwards with the outer end close to the reactor shell. The fluid distribution troughs can include at least one longitudinal baffle, or at least one cross baffle, or both, and optionally an end baffle. The baffles improve the liquid and/or vapor flow in the rough liquid distribution tray.

Hydroprocessing reactor internals having reduced height

The present invention relates to an apparatus for gas-liquid contacting and gas distribution in a bubble contactor. More specifically, the present invention relates to a gas-liquid distribution device that may be used in an ionic liquid co-current gas and liquid up-flow regenerator designed to distribute gas uniformly across the regenerator cross section through restriction orifices on a distribution plate with liquid upcomers.

Apparatus for gas-liquid contacting

Multiple downcomer trays having increased active area for vapor-liquid contact and separation are described. The increased active area of the tray is achieved by adding raised bubble promoters surrounded by perforated vertical contactors on the tray deck. The bubble promoters and surrounding vertical contactors are located under the downcomers from the tray above. The bubble promoter and surrounding vertical contactor promote uniform fluid flow and contact.

Multiple downcomer trays

A high capacity and high efficiency co-current and cross-flow vapor-liquid contacting apparatus and process is useful in distillation columns and other vapor-liquid contacting processes. The apparatus is characterized by an arrangement of offset contacting modules in horizontal stages. The modules define a co-current contacting volume and in an exemplary configuration the modules include a liquid distributor and a demister. Half modules comprise downcomers against the shell of the vessel for transporting liquid to the subjacent stage.

Vapor-liquid contacting apparatus and process with offset contacting modules

A contacting device and method are presented for the collection, contacting, and distribution of fluids between particulate beds of a downflow vessel, which may operate in co-current flow. By one approach, the contacting device includes a liquid collection tray, a mixing channel in fluid communication with the liquid collection tray, and a liquid distribution zone.

Methods and apparatus for fluid contacting in a downflow vessel

Processes for controlling the rate and temperature of cooling fluid through a heat exchange zone in, for example, an alkylation reactor using an ionic liquid catalyst. A cooling fluid system may be used to provide the cooling fluid which includes a chiller and a reservoir. The cooling fluid may pass from the reservoir through the heat exchange zone. A bypass line may be used to pass a portion of the cooling fluid around the heat exchange zone. The amount of cooling fluid may be adjusted, with a valve, based upon the temperature of the cooled process fluid flowing out of the heat exchange zone. Some of the cooling fluid from the chiller may be circulated back to the chiller in a chiller loop.

Processes and systems for controlling cooling fluid in an ionic liquid reactor system with a heat exchanger

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Inverness, IL, United States of America

Zhanping Xu