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Christopher D DiGiulio

Charles P Luebke

Jaime G Moscoso

Andrea G Bozzano

Gregory A Funk

Clayton Colin Sadler

Mark Paul Lapinski

Wolfgang A Spieker

Bryan James Egolf

Louis A Lattanzio

Raul Zavala

Nicholas J Schoenfeldt

Thulasidas Chellppannair

John Joseph Senetar

Stuart R Miller

Manuela Serban

David James Shecterle

Rajeswar R Gattupalli

Phillip F Daly

James W Harris

Steven A Bradley

William Yanez

Michael Van De Cotte

Ka Leung Lok

Krishna Mani

Sujay R Krishnamurthy

Hari S Bajpai

Jeffrey R Grott

Hosoo Lim

Lin Jin

William T Kender

Parag Jain

Michael W Penninger

Matthew R Zuraski

Paul Adams

Falaah Falih

Zudtky Wisecraver

Priyank Tiwari

Michael J Grapenthien

Kristen E Allaire

Joseph Peterson

Haibo Yu

Elie J Fayad

Gaurav Srivastava

Shubhra J Bhadra

A flow battery system with a cathode cell including a first electrode, an anode cell includes a second electrode, and a membrane between the two cells. A first electrolyte tank includes a catholyte. A second electrolyte tank includes an anolyte. The system includes two rebalancing cells. A first rebalancing cell is in fluid communication between the cathode cell and the first electrolyte tank and is configured to reduce active species from the catholyte. The second rebalancing cell is in fluid communication with the first electrolyte tank and the second electrolyte tank such that the first electrolyte tank and the second electrolyte tank are in direct fluid communication. The second rebalancing cell is configured to reduce active species from the catholyte and the reduced catholyte may be combined directly with the anolyte. The second rebalancing cell may be a chemical reactor, a catalytic reactor, or an electrochemical reactor.

Ferric ion reduction system to enable electrolyte rebalance within an iron flow battery

A process is provided for purification of biogas to produce biomethane. The biogas is treated in a pressure swing adsorption unit to remove carbon dioxide and water. Other impurities including oxygen, hydrogen and carbon monoxide may be removed by an additional adsorption bed. The adsorption beds may be single stage or two-stage VPSA or PSA adsorption beds.

Treatment of biogas by pressure swing adsorption

Processes and apparatus for reforming hydrocarbons to reduce the impact of contaminants created by non-catalyst coking. The reaction zone receives sulfur to inhibit the impact, and a control index is used to control the determine conditions with generally lower pressures. Additionally, a compression zone, pressure control zone and combustion zone operation are provided for the operation of the reaction zone at the generally lower pressures.

Processes and apparatuses for operating a hydrocarbon conversion zone

A process and system for monitoring and controlling the operation of a dehydrogenation reactor is provided. Samples of hydrocarbon streams are taken at sampling locations to be analyzed at a single gas chromatograph or other analytical equipment. Actions can be taken to modify the operation of the dehydrogenation reactor as necessary to maintain its operation within predetermined parameters. In particular, actions may be taken when a hydrocarbon stream exhibits an amount of cracking that is outside parameters. It is usually intended that actions will be taken on a gradual basis once or twice per day to reduce the cost of the process while still providing the necessary changes to operations.

System for optimizing fired-heater operation through monitoring of high temperature dehydrogenation processes

An alkylation process including an upfront isomerization zone is described. 100% n-butane or field butanes can be converted into a blend of approximately 60 wt % isobutane and 40 wt % n-butane in the isomerization zone. This blend can be used as the feed to all types of alkylation zones. It stabilizes the feed composition so that the dehydrogenation zone and alkylation zone always operate with the same feed.

Isomerization zone in alkylate complex

Processes for producing a gasoline blend in which Chydrocarbons are separated from a naphtha feed. The Chydrocarbons are isomerized and dehydrogenated to increase the octane value of the components therein. In order to avoid conversion of methylcyclohexane to toluene in the dehydrogenation reactor, the various processes provide flow schemes in which the methylcyclohexane bypasses the Cdehydrogenation reaction zone.

Processes for increasing an octane value of a gasoline component

Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500&#xb0;-645&#xb0; C.

Dehydrogenation process at reduced hydrogen to hydrocarbon ratios

The present invention relates to the integration of an alkylation unit for use in a hydrocarbon conversion process. More specifically, the present invention relates to the integration of a dehydrogenation unit and an alkylation unit and the placement of different isomerization units located off the deisobutanizer and the debutanizer.

Integration of a dehydrogenation unit and an alkylation unit

Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500&#xb0;-645&#xb0; C. The process uses a low coke catalyst.

Processes for co-production of methyl tertiary-butyl ether (MTBE) and alkylate is disclosed. The process includes comprising passing a hydrocarbon feed stream comprising Chydrocarbons to a dehydrogenation unit to generate a dehydrogenation effluent comprising Colefins. The dehydrogenation effluent is passed to a MTBE unit to provide a mixed stream comprising Colefins and MTBE. The mixed stream is separated to provide an MTBE product stream and a fractionator overhead stream comprising olefins. The fractionator overhead stream is passed to an alkylation unit to produce an alkylation product stream comprising an alkylate.

Co-production of MTBE and alkylate

A process is presented for the production of light olefins. The process utilizes a SAPO-18 catalyst and is operated at an elevated pressure. The process generates higher concentrations of heavier olefins which can then be processed to generate light olefins. The processing of the heavier olefins can include metathesis reactions and olefin cracking processes.

MTO process for enhanced production of propylene and high value products

An integrated process for production of gasoline has been described. The process includes a C-Cisomerization zone, two Cisomerization zones separate by a deisoheptanizer, and a reforming zone. The use of two Cisomerization zones eliminates the need for the large recycle stream from the deisoheptanizer. The low temperature in first Cisomerization zone favors the formation of multi-branched Cparaffins and cyclohexanes and maximizes Cyield. The separation between paraffin and cycloalkane in deisoheptanizer becomes easier due to conversion of cycloalkanes to cyclohexanes in the first Cisomerization zone. Further, the high temperature in second Cisomerization zone favors the formation of higher octane cyclopentanes over cyclohexanes. An aromatic-containing stream can be introduced to second Cisomerization zone. The saturation of the aromatics in the second Cisomerization zone provides heat that increases the reactor outlet temperature in the isomerization reactors to favor cyclopentanes.

Integrated process for production of gasoline

A process for the production of butadiene is presented. The process combines the separation of butenes and butadienes extracted from a non-oxidated dehydrogenation process with the separation of butenes and butadienes from an oxidative dehydrogenation process to increase the butadiene yields and reduce the equipment for the recovery of a butadiene product.

Integration of N-C4/N-C4=/BD separation system for on-purpose butadiene synthesis

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Chicago, IL, United States of America

Christopher D DiGiulio