Exxon Research and Engineering Company

Union Carbide Corporation

Accelergy Corporation

Exxonmobil Research and Engineering Company

Chinese Academy of Sciences

Rocco A Fiato

Stuart Leon Soled

Enrique Iglesia

Sabato Miseo

Geoffrey R Say

Stephen M Davis

LeRoy R Clavenna

Gary Wayne Rice

Angelo A Montagna

Edwin L Kugler

Yuhan Sun

Mark Allen

Quanyu Zhao

Gary Brice McVicker

Jack Wayne Johnson

Israel E Wachs

Joseph Ernest Baumgartner

Roy L Pruett

Ronny Bar-Gadda

Loren Leon Ansell

Adeana Richelle Bishop

William Berlin Genetti

Jose Luis Vidal

Claudio C Chersich

David C Long

Gerald B Ansell

Lowell Alan Cosby

Frank Hershkowitz

Michel A Daage

Gabor Kiss

Bal K Kaul

William E Gates

Russell J Koveal

James H Taylor, Jr

Chang J Kim

Stephen C Leviness

Richard Frank Bauman

Alla Jurievna Krylova

Charles W Degeorge

Roger W Cohen

Craig Y Sabottke

Edward Niessen

Hilda Vroman

Frederick J Kaiser, Jr

Jose' L Vidal

Wellington E Walker, Deceased

Benny J Argento

Albert L'Vovoch Lapidus

Sioma Zaczepinski

Gerard C Lahn

Sibylle Pagnucco

Sandra S Unger

Richard F Bauman

Attilio Bisio

An IBTL system having a low GHG footprint for converting biomass to liquid fuels in which a biomass feed is converted to liquids by direct liquefaction and the liquids are upgraded to produce premium fuels. Biomass residues from the direct liquefaction, and optionally additional biomass is pyrolyzed using microwave pyrolysis to produce structured biochar, hydrogen for the liquefaction and upgrading, and COfor conversion to algae, including blue green algae (cyanobacteria) in a photobioreactor (PBR). Produced algae and diazotrophic microorganisms are used to produce a biofertilizer that also contains structured biochar. The structured biochar acts as a nucleation agent for the algae in the PBR, as a absorption agent to absorb inorganics from the biomass feed to direct liquefaction or from the liquids produced thereby, and as a water retention agent in the biofertilizer. The ratio of cyanobacteria to diazotrophic microorganisms in the biofertilizer can be selected so as to achieve desired total chemically active carbon and nitrogen contents in the soil for a given crop.

Processes for producing fuels and biofertilizers from biomass and products produced

An IBTL system having a low GHG footprint for converting biomass to liquid fuels in which a biomass feed is converted to liquids by direct liquefaction and the liquids are upgraded to produce premium fuels. Biomass residues from the direct liquefaction, and optionally additional biomass is pyrolyzed to produce structured biochar, hydrogen for the liquefaction and upgrading, and COfor conversion to algae, including blue green algae (cyanobacteria) in a photobioreactor (PBR). Produced algae and diazotrophic microorganisms are used to produce a biofertilizer that also contains structured biochar. The structured biochar acts as a nucleation agent for the algae in the PBR, as a absorption agent to absorb inorganics from the biomass feed to direct liquefaction or from the liquids produced thereby, and as a water retention agent in the biofertilizer. The ratio of cyanobacteria to diazotrophic microorganisms in the biofertilizer can be selected to optimize the so as to achieve desired total chemically active carbon and nitrogen contents in the soil for a given crop.

Integrated processes for producing fuels and biofertilizers from biomass and products produced

A method for producing synthetic fluids from TGFA's harvested from genetically modified seed crops in which all of the fatty acids in the TGFA's from the seeds of a crop have the same carbon atom chain length, preferably C12 or C14, and the synthetic fluids produced by the method. The TGFA's are hydroprocessed to cleave the fatty acids from the glycol backbone and to hydrodeoxygenate and isomerize the fatty acids to form single carbon chain length isoparaffins having a controlled degree of branching with minimum cracking. Controlled mixtures of hydrocarbon components, in which each hydrocarbon component of the mixture has a different single carbon atom chain length, are produced. The relative ratios of the single carbon atom number hydrocarbons in the mixture are selected to optimize the characteristics of the synthetic fluid product for a given application, if the end product is an SDF, the severity of the hydrotreatment is controlled such that the degree of cracking is minimized and the isomers generated are primarily monomethyl isoparaffins. If the end product is a jet fuel blend stock, the hydrotreatment is somewhat more severe in order to generate multiple branched isomers that have improved aerobic biodegradability and low temperature properties. The degree of hydrotreatment is controlled to limit the degree of branching in order to preserve the required thermal and oxidative stability properties, and to minimize cracking.

Synthetic fluids and methods of manufacture

An integrated coal-to-liquids process is provided to minimize carbon dioxide emissions and efficiently make use of carbon resources, by recovering carbon dioxide emissions from Coal-to-Liquids (CTL) facilities, using the recovered carbon dioxide in at least one carbonylation reaction step for converting ammonia to urea and then converting urea into dimethyl carbonate.

Integrated coal to liquids process and system

A heavy hydrocarbon composition with utility as a heavy hydrocarbon base stock comprising at least 95 wt % paraffin molecules, of which at least 90 wt % are isoparaffin, containing hydrocarbon molecules having consecutive numbers of carbon atoms, is a liquid at 100&#xb0; C., at which temperature its kinematic viscosity, as measured by ASTM D-445, is above 8 cSt, has an initial boiling point of least 850&#xb0; F. (454&#xb0; C.) and an end boiling point of at least 1000&#xb0; F. (538&#xb0; C.), wherein the branching index (BI), as measured by the percentage of methyl hydrogens, and the branching proximity (CH&#x3e;4), as measured by the percentage of recurring methylene carbons which are four or more carbon atoms removed from an end group or branch, of said isoparaffinic hydrocarbon molecules, are such that:

Heavy hydrocarbon composition with utility as a heavy lubricant base stock

A synthetic, isoparaffinic heavy hydrocarbon composition useful as a heavy lubricant base stock contains hydrocarbon molecules having consecutive numbers of carbon atoms, is a liquid at 100&#xb0; C., at which temperature its kinematic viscosity is above 8 cSt and has respective initial and end boiling points of at least 850 and 1000&#xb0; F. (454 and 538&#xb0; C.). The branching index BI and the branching proximity CH&#x3e;4 of the isoparaffinic hydrocarbon molecules, are such that:BI&#x2212;0.5(CH&#x3e;4)&#x3c;15; and&#x2003;&#x2003;(a)BI+0.85(CH&#x3e;4)&#x3c;45;&#x2003;&#x2003;(b)as measured over the hydrocarbon composition as a whole.

Synthetic isoparaffinic premium heavy lubricant base stock

Linear alpha olefins having from four to twenty carbon atoms and low amounts of oxygenates are synthesized, by producing a synthesis gas containing H and CO from natural gas and passing it over a non-shifting cobalt catalyst at reaction conditions of temperature, % CO conversion, and gas feed H :CO mole ratio land water vapor pressure, effective for the mathematical expression 200&minus;0.6T&plus;0.03P &minus;0.6X &minus;8(H :CO) to have a numerical value greater than or equal to 50. This process can be integrated into a conventional Fischer-Tropsch hydrocarbon synthesis process producing fuels and lubricant oils.

Linear alpha olefins from natural gas-derived synthesis gas over a nonshifting cobalt catalyst

A process for the preparation of a catalyst useful for conducting carbon monoxide hydrogenation reactions, especially Fischer-Tropsch reactions. The steps of the process begin with the activation, or reactivation, of a deactivated catalyst, or with the preparation and activation of a fresh catalyst. In accordance with the latter, the steps of the process comprise, first contacting, in one or more steps, a powder or preformed, particulate refractory inorganic support with a liquid, or solution in which there is dispersed or dissolved a compound, or salt of a catalytically active metal, or metals, to impregnate and deposit the metal, or metals, upon the support, or powder. The metal, or metals, impregnated support is calcined following each impregnation step to form oxides of the deposited metal, or metals. The calcined catalyst precursor is then treated with a solution of a chelating compound, preferably a poly- or multidentate chelating compound, sufficient to complex with, extract and remove a portion of the oxides of the metal, or metals. The catalyst is activated by reduction; suitably by contact with hydrogen. In the activation, or reactivation of a deactivated catalyst, the catalyst is first treated with the chelating compound to extract a portion of the oxides of the metal, or metals, and the catalyst is then reduced. In either event, the activated or reactivated catalyst has high activity, or high C,&plus; selectivity, or both high activity and C,&plus; selectivity in conducting carbon monoxide hydrogenation reactions. The productivity of the process is increased.

Process for the preparation of high activity carbon monoxide hydrogenation catalysts; the catalyst compositions, use of the catalysts for conducting such reactions, and the products of such reactions

A process for making a synthesis gas comprising H.sub.2 and CO in the presence of a reforming catalyst comprising a supported non-noble Group VIII metal catalytic component from a feed including a low molecular weight alkane, and preferably methane as in natural gas, O.sub.2, H.sub.2 O and CO.sub.2 without catalyst deactivation is achieved by partially oxidizing and steam reforming the feed in the presence of the catalyst. The feed H.sub.2 O to hydrocarbon carbon mole ratio is less than 2. The mole ratio of the combined feed CO.sub.2 and H.sub.2 O to hydrocarbon carbon ranges from 0.5-2.5 and that of the feed H.sub.2 O to CO.sub.2 ranges from 0.35-6. Synthesis gas having H.sub.2 to CO mole ratios less than 2:1 and even less than 1.5:1 are easily achieved with net CO.sub.2 consumption, which also makes the process environmentally beneficial.

Low hydrogen syngas using CO.sub.2 and a nickel catalyst

Hydrogen containing tail gas from a hydrocarbon synthesis reactor is used as a hydrogen containing catalyst rejuvenating gas. If CO is present, the CO content, is less than 10 mole % of the gas and the H.sub.2 to CO mole ratio is greater than 3:1. At least a portion of the water and liquid hydrocarbons are removed from the tail gas, before it is used to rejuvenate the reversibly deactivated catalyst.

Hydrocarbon synthesis using reactor tail gas for catalyst rejuvenation

The present invention is a database and a method of producing that database which can be used to determine the meaning of scientific or technical documents, such as patents and/or technical or scientific publications and/or abstracts of these patents or publications, and to assign the technical documents to one or more scientific or technical categories within a multidimensional hierarchical model which reflects the business, scientific or technical interests of a business, scientific or technical entity or specialty.

Relational database system containing a multidimensional hierachical

High surface purity heat transfer solids are formed, suitably by washing and treating particulate refractory inorganic solids, notably alumina, which contains as impurities up to about 0.5 wt. % silicon and/or up to about 500 wppm boron, with an acid, or dilute acid solution sufficient to reduce the concentration of silicon and boron in the outer peripheral surface layer of the particles, e.g., as measured inwardly toward the center of a particle to a depth of about 50 .ANG. using X-ray photoelectron spectroscopy, to no greater than about 5 atom percent silicon and boron, preferably about 2 atom percent silicon and boron, based on the total number of cations within said outer peripheral surface layer, thereby reducing the tendency of said particles to sinter and agglomerate in the conversion of said hydrocarbon to hydrogen and carbon monoxide in a fluidized bed synthesis gas operation vis-a-vis particles otherwise similar except that the particles are not treated with the acid. The tendency of the particles to sinter and agglomerate is further reduced by the additional removal of sodium, iron, calcium, and titanium impurities from the outer peripheral surface layer of the particles. Preferably the latter named impurities, or impurities other than silicon and boron, are reduced to a concentration below about 20 atom %, more preferably to a concentration below about 15 atom %, in the outer surface layer of the particles.

High surface purity heat transfer solids for high temperature fluidized

A particulate, precalcined low silica content zirconia, especially one stabilizer with yttria, is useful as a catalyst support or as a heat transfer solids component for conducting chemical reactions at high temperature, in oxidizing, reducing or hydrothermal conditions, especially in syn gas operations. An admixture of precalcined particulate low silica content zirconia, particularly a low silica content yttria-stabilized zirconia, is employed in a preferred embodiment as a heat transfer solid, in concentrations ranging generally from about 10 wt. % to about 99.9 wt. % with a particulate catalyst notably a nickel-on-alumina catalyst, in concentration ranging generally from about 0. 1 wt. % to about 90 wt. %. Such an admixture provides a particularly useful catalytic contact mass in high temperature oxidizing, reducing and hydrothermal environments, notably in conducting synthesis gas generation operations. This type of bed promotes continuous, highly efficient heat and mass transfer within the reacting gas phase. The presence of the heat transfer solid as a bed component maintains excellent bed fluidization characteristics, suppressing the normal tendency of the catalyst to sinter or agglomerate; tendencies which promote defluidization of the bed. Moreover, the heat transfer particles of the bed are highly attrition resistant, and are chemically compatible with the catalyst particles of the admixture.

Particulate solids for catalyst supports and heat transfer materials

The daylight stability, foaming characteristics, color, engine performance test behavior, oxygenates content, and thermal stability of wax isomerate oils and/or hydrocarbon synthesis liquid products are improved by the process of contacting the aforesaid wax isomerate oil and/or hydrocarbon synthesis liquid products with a silica adsorbent, said silica adsorbent being characterized by possessing a pore size of at least about 100 .ANG., preferably at least about 125 .ANG., most preferably at least about 150 .ANG., an alkali/alkaline earth ion concentration, excluding sodium, of greater than about 125 ppm, an iron content of less than about 40 ppm and a zirconium content of less than about 130 ppm.

Performance of contaminated wax isomerate oil and hydrocarbon synthesis

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Basking Ridge, NJ, United States of America

Rocco A Fiato