E.i. Dupont De Nemours and Company

Conocophillips Company

Conoco Inc.

William H Manogue

V N Rao

Hasan Dindi

Steven Henry Swearingen

Leo E Manzer

James L Webster

Jan J Lerou

Swiatoslaw Trofimenko

Douglas W Bruhnke

Elrey L McCann

Allen Capron Sievert

Paul R Resnick

Frank J Weigert

John James Barnes

Cristobal Bonifaz

Mario Joseph Nappa

Norman Herron

Sourav Kumar Sengupta

Theodore Augur Koch

Charles Joseph Noelke

Velliyur Nott Rao

V N Mallikarjuna Rao

James Arthur Trainham

Peter Gideon Gelblum

Tiberiu M Leib

Tianyan Niu

Juan Carlos Figueroa

Vn Mallikarjuna Rao

Thomas R Keane

Rhodium-spinel catalysts with activity for efficiently catalyzing the net partial oxidation of methane at high selectivities for CO and Hproducts are disclosed, along with their method of making. A syngas production process employing such catalysts for the net catalytic partial oxidation of a C-Chydrocarbon (e.g., natural gas or methane) to a product gas mixture comprising CO and His also disclosed. Preferred reaction conditions include maintaining the catalyst at a temperature of about 400-1,200&#xb0; C., superatmospheric pressure, and flow rate sufficient to pass the reactant gas mixture over the catalyst at space velocities of at least about 100,000-25,000,000 hr.

Supported rhodium-spinel catalysts and process for producing synthesis gas

This invention provides a catalyst and a process for the catalytic partial oxidation of a hydrocarbon feedstock by contacting a feed stream including a hydrocarbon feedstock and an oxygen-containing gas with a catalyst in a reaction zone maintained at conversion-promoting conditions effective to produce an effluent stream including carbon monoxide and hydrogen. The process of this invention is characterized by using a porous catalyst containing rhodium, such as rhodium gauze or rhodium felt.

Rhodium cloth catalyst for partial oxidation of hydrocarbons

This invention provides a process for the catalytic partial oxidation of a hydrocarbon feedstock by contacting a feed stream including a hydrocarbon feedstock and an oxygen-containing gas with a catalyst in a reaction zone maintained at conversion-promoting conditions effective to produce an effluent stream including carbon monoxide and hydrogen. The process of this invention is characterized by using an unsupported porous catalyst containing rhodium, such as rhodium foam.

Rhodium foam catalyst for the partial oxidation of hydrocarbons

A process is disclosed for producing the pentfluropropenes of the formula CF CX&boxH;CF , where X is H or Cl. The process involves hydrodehalogenating CF CCl CF with hydrogen at an elevated temperature in the vapor phase over a catalyst comprising an elemental metal, metal oxide, metal halide and/or metal oxyhalide (the metal being copper, nickel, chromium and the halogen of said halides and said oxyhalides being fluorine and/or chlorine. Processes for producing the hydrofluorocarbons CF CH CHF , CF CHFCF and CF CH CF are also disclosed which involve (a) hydrodehalogenating CF CCl CF with the hydrogen as indicated above to produce a product comprising CF CCl&boxH;CF , CF CH&boxH;CF , HCl and HF; and (b) either reacting the CF CCl&boxH;CF and/or CF CH&boxH;CF produced in (a) in the vapor phase with hydrogen to produce CF CH CHF , reacting CF CCl&boxH;CF produced in (a) with HF to produce CF CHFCF , or reacting the CF CH&boxH;CF produced in (a) with HF to produce CF CH CF . Azeotrope compositions of CF CHFCH with HF, and a process for recovering HF from a product mixture comprising HF and CF CHFCF are also disclosed. Also disclosed are compositions and a process for producing compositions comprising (c1) CF CHFCF , CF CH CF or CHF CH CF and (c2) at least one saturated halogenated hydrocarbon and/or ether having the formula: C H Cl F O wherein n is an integer from 1 to 4, a is an integer from 0 to 2n&plus;1, b is an integer from 1 to 2n&plus;2&minus;a, and c is 0 or 1, provided that when c is 1 then n is an integer from 2 to 4, and provided that component (c2) does not include the selected component (c1) compound, wherein the molar ratio of component (c2) to component (c1) is between about 1:99 and a molar ratio of HF to component (c1) in an azeotrope or azeotrope-like composition of component (c1) with HF. The process involves (A) combining (i) the azeotropic composition with (ii) the fluorination precursor to component (c2); and (B) reacting a sufficient amount of the HF from the azeotrope or azeotrope-like composition(i) with precursor component (ii) to provide a composition containing components (c1) and (c2) in the desired ratio. The compositions include at least two (c1) compounds, at least one of which is an ether.

Process for the manufacture of 1,1,1,3,3-pentafluoropropene, 2-chloro-pentafluoropropene and compositions comprising saturated derivatives thereof

A process for the production of synthesis gas from light hydrocarbons such as methane includes the net catalytic partial oxidation of a hydrocarbon feedstock by contacting a feed stream comprising the hydrocarbon feedstock and an O -containing gas with a catalyst in a reaction zone maintained at conversion-promoting conditions effective to produce an effluent stream of H and CO in a molar ratio of about 2:1. A preferred catalyst used in the process includes at least one catalytically active metal supported on a catalyst support comprising an aluminum-containing, oxide-dispersion-strengthened, alloy that has been treated to provide a protective oxide layer between the support and the catalytically active metal.

Catalytic partial oxidation processes and catalysts with diffusion barrier coating

A process is disclosed for the separation of a mixture of HF and CF.sub.3 CClFCF.sub.3. The process involves placing the mixture in a separation zone at a temperature of from about -30.degree. C. to about 100.degree. C. and at a pressure sufficient to maintain the mixture in the liquid phase, whereby an organic-enriched phase comprising less than 50 mole percent HF is formed as the bottom layer and an HF-enriched phase comprising more than 90 mole percent HF is formed as the top layer. The organic-enriched phase can be withdrawn from the bottom of the separation zone and subjected to distillation in a distillation column to recover essentially pure CF.sub.3 CClFCF.sub.3. The distillate comprising HF and CF.sub.3 CClFCF.sub.3 can be removed from the top of the distillation column while essentially pure CF.sub.3 CClFCF.sub.3 can be recovered from the bottom of the distillation column. The HF-enriched phase can be withdrawn from the top of the separation zone and subjected to distillation in a distillation column. The distillate comprising HF and CF.sub.3 CClFCF.sub.3 can be removed from the top of the distillation column while essentially pure HF can be recovered from the bottom of the distillation column. If desired, the two distillates can be recycled to the separation zone. Also disclosed are compositions of hydrogen fluoride in combination with an effective amount of CF.sub.3 CClFCF.sub.3 to form an azeotrope or azeotrope-like composition with hydrogen fluoride. Included are compositions containing from about 38.4 to 47.9 mole percent CF.sub.3 CClFCF.sub.3. Also disclosed are processes for producing 1,1,1,2,3,3,3-heptafluoropropane. One process uses a mixture comprising HF and CF.sub.3 CClFCF.sub.3 and is characterized by preparing essentially pure CF.sub.3 CClFCF.sub.3 as indicated above, and reacting the CF.sub.3 CClFCF.sub.3 with hydrogen. Another process uses an azeotropic composition as described above, and reacts the CF.sub.3 CClFCF.sub.3 with hydrogen in the presence of HF. Also disclosed is a process for producing hexafluoropropene. This process is characterized by preparing essentially pure CF.sub.3 CClFCF.sub.3 as indicated above, and dehalogenating the CF.sub.3 CClFCF.sub.3.

Process for the production of fluorocarbons

A process for the production of trifluoroethylene (i.e., CF.sub.2 =CHF or HFC-1123) is disclosed. The process involves contacting (in the vapor phase) at least one halogenated ethane of the formula CF.sub.3 CClFX (where X is H, Cl or F) with hydrogen in the presence of a catalyst including at least one component selected from elemental metals, metal oxides, metal halides and metal oxyhalides. The metal of the component is ruthenium, copper, nickel, and/or chromium and the halogen of the halides and the oxyhalides is fluorine and/or chlorine.

Process for the production of trifluoroethylene

Hydrofluorocarbon production using heat carriers in high temperature

Halocarbons such as CCl.sub.2 F.sub.2, CF.sub.3 CFHCl or CF.sub.3 CFCl.sub.2 which contain chlorine and/or bromine are contacted with hydrogen in the presence of silicon carbide and/or a metal selected from aluminum, molybdenum, titanium, nickel, iron or cobalt (or their alloys) at temperatures of 350.degree. to 700.degree. C. and pressures of 0 to 1000 psig to obtain a product wherein at least one chlorine or bromine in the starting material has been replaced by hydrogen.

Halocarbon hydrogenolysis

A process is disclosed for the conversion of halogenated methanes of the formula CCl.sub.y H.sub.2-y F.sub.2 (wherein y is 1 or 2) to a mixture of conversion products. The process involves reacting certain halogenated hydrocarbon feeds and hydrogen (wherein said halogenated methanes are at least one mole percent of the halogenated hydrocarbon feed) in a reaction vessel of alumina, silicon carbide or at least one metal selected from gold, chromium, aluminum, molybdenum, titanium, nickel, iron, cobalt, and their alloys at a temperature of from about 500.degree. C. to 800.degree. C. and a pressure from abut 101 kPa to 7000 kPa to produce a mixture of conversion products of said halogenated methanes which comprises at least 5 mole percent C.sub.2 H.sub.2 F.sub.4, wherein the mole ratio of CH.sub.2 FCF.sub.3 to CHF.sub.2 CHF.sub.2 in said C.sub.2 H.sub.2 F.sub.4 is at least about 1:9.

Process for converting chlorodifluoromethane and/or

Mixtures of halocarbons which contain fluorine and chlorine and/or bromine (e.g. a mixture of CCl.sub.2 FCF.sub.3 with CClF.sub.2 CF.sub.3, CCl.sub.2 F.sub.2, CClF.sub.2 CClF.sub.2 or CHClF.sub.2) are contacted with hydrogen in the presence of silicon carbide and/or a metal selected from aluminum, molybdenum, titanium, nickel, iron or cobalt (or their alloys) at temperatures of 350.degree. to 700.degree. C. and pressures of 0 to 1000 psig to obtain a product mixture which substantially corresponds in terms of the distribution of fluorine substituents on carbon atoms with the mixture of halocarbon starting materials.

Hydrogenolysis of halocarbon mixtures

Gas phase and liquid phase processes are disclosed which use interconversion of CF.sub.3 CHFCl and CF.sub.2 HCF.sub.2 Cl in contact with catalyst consisting essentially of halided aluminum oxide and/or aluminum halide at elevated temperatures to increase the mole ratio of one of said compounds in a composition relative to the other. Also disclosed is use of said interconversion along with hydrogenolysis in processes for producing mixtures of CF.sub.3 CH.sub.2 F and CF.sub.2 HCF.sub.2 H from certain compositions comprising CF.sub.2 HCF.sub.2 Cl such that the mole ratio of CF.sub.3 CH.sub.2 F to CF.sub.2 HCF.sub.2 H in the product mixtures produced from said compositions may be increased or decreased.

Catalytic equilibration to improve the relative yield of selected

Halocarbons such as CCl.sub.2 F, CF.sub.3 CFHCl.sub.2 or CF.sub.3 CFCl.sub.2 which contain chlorine and/or bromine are contacted with hydrogen in the presence of silicon carbide and/or a metal selected from aluminum, molybdenum, titanium, nickel, iron or cobalt (or their alloys) at temperatures of 350.degree. to 700.degree. C. and pressures of 0 to 1000 psig to obtain a product wherein at least one chlorine or bromine in the starting material has been replaced by hydrogen.

Growing community of inventors

Newark, DE, United States of America

William H Manogue