Honeywell International Inc.

Airmyne, Inc.

University of California

Bp Chemicals Limited

Sudip Mukhopadhyay

Hsueh Sung Tung

Haridasan K Nair

Michael Van Der Puy

Rajesh K Dubey

Daniel C Merkel

Jing Ji Ma

HsuehSung Tung

Cheryl L Bortz

Mark Patrick Cyffka

Barbara A Light

Steven D Phillips

Bart Ludo Scherpbier

Haiyou Wang

Robert C Johnson

Kim M Fleming

Le-Xuan Diec

Flynn Corrigan Michael Legg

Ngoc The Pham

Rajiv R Singh

Desaraju Varaprasad

Yamini Pandey

Jun Seon Hong

Derek Chase Popple

Joana Cabrera

Aryan Johari

John Glenn Sunley

Joseph T Kennedy

George A Shia

Alexis T Bell

Songyuan Xie

Sander Gaemers

Jingji Ma

Carlos Guillermo Ramirez

Cyndia Aiyun Cao

Mark Zerella

Dominick Yaate Quaye

Lea Dankers

Rajesh Dubey

Glen Aaron Sanders

David Nalewajek

Awdhoot V Kerkar

Andrew Richard Lucy

Boris Korolev

Jelena Sepa

Cheryl Cantlon

Brian Ellis

Alan Scott

Philip Howard

Hugh Podmore

Michael James Muskett

Kim Do

Richard Udy

Aryaman Bhartia

Arun Suresh Kamath

Susan A Ferguson

Hai Bien

Amanuel H Gebrehrhan

Valerie Ann Wilson

Sophia Elaine Chandler Sperman

Robert Johnson

Susan Ferguson

Steven Phillips

George Honeywell International Inc Shia

Tung Hsuehsung

Ma Jingji

George Shia

Cheryl L Cantlon

In a general aspect, interfacial surface structures for removing carbon dioxide from a gaseous feed are presented. In some cases, a method of removing carbon dioxide gas from a gaseous feed includes wetting surfaces of an interfacial surface structure in a gas-liquid contactor with an alkaline capture solution. The gaseous feed containing the COgas is passed across the wetted surfaces of the interfacial surface structure to dissolve the COgas in the alkaline capture solution. A CO-rich alkaline capture solution is collected from the gas-liquid contactor. The CO-rich alkaline capture solution includes dissolved COgas from the gaseous feed.

Interfacial surface structures for carbon dioxide removal systems

In a general aspect, a carbon dioxide (CO) removal system uses geothermal energy. In some implementations, a method to remove COgas from a gaseous feed includes directing a gaseous feed to interact with an alkaline capture solution in a first gas-liquid contactor. A first portion of COfrom the gaseous feed dissolves into the alkaline capture solution to form a CO-rich alkaline capture solution. Steam is generated using heat from a geothermal heat source, and the steam heats the CO-rich alkaline capture solution in a second gas-liquid contactor. A second portion of the COis separated from the CO-rich alkaline capture solution in the second gas-liquid contactor to form a CO-lean alkaline capture solution. The CO-lean alkaline capture solution is directed to the first gas-liquid contactor.

Carbon dioxide removal systems using a geothermal heat source

In a general aspect, a carbon dioxide removal system is presented. In some cases, a gas-liquid contactor is wetted with an alkaline capture solution. A first flow from a first gaseous feed including COfrom a first source is directed to interact with the alkaline capture solution in the gas-liquid contactor, which forms a first CO-rich alkaline capture solution. A second flow from a second gaseous feed including COfrom a second, distinct source is directed to interact with the first CO-rich alkaline capture solution, which forms a second CO-rich alkaline capture solution. In some cases, the second flow is independent of the first gaseous feed, and a concentration of COin the second CO-rich alkaline capture solution is higher than a concentration of COin the first CO-rich alkaline capture solution. COcan be separated from the second CO-rich alkaline capture solution.

Hybrid carbon dioxide removal systems

An apparatus includes a captured carbon dioxide input. The captured carbon dioxide input is coupled to receive captured carbon dioxide from a direct air capture system. The apparatus uses the captured carbon dioxide as a low global warming refrigerant to provide cooling functionality in automotive, commercial, and industrial applications, or other operations involving low global warming refrigerants. In various embodiments, the apparatus is a refrigeration apparatus or a heat pump apparatus. Low global warming carbon dioxide refrigerant is natural, non-toxic, non-flammable, and abundant when obtained from a direct air capture system. Moreover, carbon dioxide refrigerant has a high heat transfer coefficient and has a global warming potential (GWP) of one. Carbon dioxide refrigerant is a more sustainable and efficient coolant option than common refrigerants, such as R22, R152, R404a, and R1234yf refrigerants.

Using carbon dioxide from a direct air capture system as a low global warming car and industrial refrigerant

An efficient low-energy carbon dioxide removal system comprises an automated air mover equipped with sensing devices to measure flow rate, volume, level, pressure, temperature and concentration. Packing materials and air-liquid distributors are used in a multi-stage catalytic reactor. The multi-stage catalytic reactor processes ambient air and generates pure carbon dioxide gas and generates exhausted gas released to ambient air. In operation, air contacts the base solution in the presence of a catalyst via the air mover, distributor, and packing materials. The air reacts with the base solution thereby generating a base solution having carbon dioxide and generating exhaust (absorption reaction). Next, the exhaust is released from the reactor. Next, a catalyst is added, heat is applied to the base solution having carbon dioxide thereby generating carbon dioxide and generating a base solution without carbon dioxide (desorption reaction).

Efficient and fully automated catalytic direct carbon dioxide capture from air system

A carbon processing system comprises an air mover and a multi-stage reactor. The multi-stage reactor processes ambient air and generates carbon dioxide and generates exhausted gas released to ambient air. In operation, air contacts the base solution via the air mover. The air reacts with the base solution thereby generating a base solution having carbon dioxide and generating exhaust (absorption reaction). Next, the exhaust is released from the reactor. Next, heat is applied to the base solution having carbon dioxide thereby generating carbon dioxide and generating a base solution without carbon dioxide (desorption reaction). The base solution without carbon dioxide generated after applying heat is reusable in processing new air. The absorption reaction and desorption reaction are reversible reactions resulting in regeneration of the base solution into its form prior to contact with the air yielding high scalability and less processing volume as required by many conventional carbon processing techniques.

Fully automated direct air capture carbon dioxide processing system

A system for detecting trace-gas includes an optical sensor mounted on a vehicle and processing circuitry. The optical sensor includes a plurality of interferometers configured to collect samples. The processing circuitry is configured to generate a digitized signal based on the samples, apply a forward Fourier-transform on the digitized signal to generate spectrum information for the plurality of interferometers, and determine a gas species has been detected using one or more intensity of absorption features of the spectrum information corresponding to the gas species from the spectrum information.

Optical sensor for trace-gas measurement

A crosslinkable composition includes a first silicon-containing resin comprising alkyl groups and alkyl groups and a second silicon-containing resin comprising alkyl groups. The first silicon-containing resin has a weight average molecular weight from 1000 AMU to 10,000 AMU. The second silicon-containing resin has a weight average molecular weight from 900 AMU to 5000 AMU. The composition further includes at least one solvent and at least one heat-activated catalyst.

Polysiloxane formulations and coatings for optoelectronic applications

Disclosed are processes for producing halogenated olefins, and preferably tetrafluorinated propene(s), from one or more alkanes having both fluorine substituents and non-fluorine substituents, preferably with a high degree of conversion and selectivity. Preferably the process comprises the use of a catalyzed reaction in which the catalyst is selected from the group consisting of activated carbons halogenated mono- and di-valent metal oxides, mono- and di-valent Lewis acid metal halides, zero-valent metals, and combinations of these.

Processes for selective dehydrohalogenation of halogenated alkanes

Disclosed are processes for the production of fluorinated olefins, preferably adapted to commercialization of CFCF&#x2550;CH(1234yf). Three steps may be used in preferred embodiments in which a feedstock such as CCl&#x2550;CClCHCl (which may be purchased or synthesized from 1,2,3-trichloropropane) is fluorinated (preferably with HF in gas-phase in the presence of a catalyst) to synthesize a compound such as CFCCl&#x2550;CH, preferably in a 80-96% selectivity. The CFCCl&#x2550;CHis preferably converted to CFCFClCH(244-isomer) using a SbClas the catalyst which is then transformed selectively to 1234yf, preferably in a gas-phase catalytic reaction using activated carbon as the catalyst. For the first step, a mixture of CrOand FeCl/C is preferably used as the catalyst to achieve high selectivity to CFCCl&#x2550;CH(96%). In the second step, SbCl/C is preferably used as the selective catalyst for transforming 1233xf to 244-isomer, CFCFClCH. The intermediates are preferably isolated and purified by distillation and used in the next step without further purification, preferably to a purity level of greater than about 95%.

Method for producing fluorinated organic compounds

Disclosed are processes for producing halogenated olefins, and preferably tetrafluorinated propene(s), from one or more alkanes having both fluorine substituents and non-fluorine substituents, preferably with a high degree of conversion and selectivity. Preferably the process comprises the use of a catalyzed reaction in which the catalyst is selected from the group consisting of activated carbons, halogentated mono- and di-valent metal oxides, mono- and di-valent Lewis acid metal halides, zero-valent metals, and combinations of these.

Disclosed is a process for producing fluorinated organic compounds, including hydrofluoropropenes, which preferably comprises converting at least one compound of Formula (I):C(X)CFC(X)&#x2003;&#x2003;(I)to at least one compound of Formula (II)CFCF&#x2550;CHZ&#x2003;&#x2003;(II)where each X and Z is independently H, F, Cl, I or Br, said process preferably not including any substantial amount of oxygen-containing catalyst in certain embodiments. Preferably Z is H.

Disclosed is a process for the synthesis of fluorinated olefins, and in particularly preferred embodiments tetrafluorinated olefins having F on an unsaturated, non-terminal carbon, such as 2,3,3,3-tetrafluoropropene. The preferred processes of the present invention in accordance with one embodiment generally comprise:

Process for synthesis of fluorinated olefins

Disclosed is a method for producing fluorinated organic compounds, including reacting CF&#x2550;CFCl with CHFCl under conditions effective to produce a product composition including CFCClFCHCl. The present invention also relates to the production of hydrofluoropropenes, which preferably comprises converting at least one compound of formula (I):CFCFCHX&#x2003;&#x2003;(I)to at least one compound of formula (II)CFCZCHZ&#x2003;&#x2003;(II).where each X is independently Cl, F, I or Br; each Z is independently H or F; n is 1 or 2; m is 1, 2 or 3, provided that when n is 1, m is 1 or 2; a is 2 or 3, and a&#x2212;m&#x2267;0. Certain embodiments include the step of reacting fluorinated C2 olefin, such as tetrafluoroethylene, with a C1 addition agent under conditions effective to produce a compound of formula (I).

Growing community of inventors

Berkeley, CA, United States of America

Sudip Mukhopadhyay