Patents:

During a career of over 30 years at DuPont, Dr. Manzer founded and directed DuPont's Corporate Catalysis Center. Dr. Manzer personally conducted his own research program covering a wide range of topics such as Fischer Tropsch catalysis, enzyme catalysis, heterogenized homogeneous catalysis, fluorocarbon catalysis and recently he has explored the catalytic conversion of biomass to chemicals and fuels. As a result of his research, he has been awarded 120 US patents, with more than 60 pending and over 500 foreign patents have also issued. The US patents are categorized below:

Chemicals and Fuels From Renewable Feedstocks

I. Derivatives of Levulinic Acid

US 7,153,996 (2006) Preparation of levulinic acid esters and formic acid esters from biomass and olefins

     Methylene Lactones

US 7,348,442 (2008) Gas phase synthesis of methylene lactones using catalysts derived from hydrotalcite precursors
US 7,314,942 (2008) Methylenelactone synthesis in supercritical fluids
US 7,205,416 (2007) Liquid phase synthesis of methylene lactones using novel grafted catalyst
US 7,199,254 (2007) Liquid phase synthesis of methylene lactones using novel catalyst
US 7,166,727(B2) (2007) Supercritical fluid phase synthesis of methylene lactones using novel grafted catalyst
US 7,164,033 (2007) Gas phase synthesis of methylene lactones using novel catalyst
US 7,164,032 (2007) Supercritical fluid phase synthesis of methylene lactones using novel catalyst field of invention
US 7,161,014 (2007) Gas phase synthesis of methylene lactones using novel grafted catalyst
US 7,153,981 (2006) Supercritical fluid phase synthesis of methylene lactones using oxynitride catalyst
US 7,151,185 (2006) Gas phase synthesis of methylene lactones using oxnitride catalyst
US 7,141,682 (2006) Liquid phase synthesis of methylene lactones using oxnitride catalyst
US 6,649,776 (2003) Methylenelactone synthesis in supercritical fluids
US 6,313,318 (2001) Process for the preparation of alpha-methylene lactones
US 6,232,474 (2001) Process for the preparation of alpha-methylenelactones and alpha-substituted hydrocarbylidene lactones

     Levulinic Acid Derived Ionic Liquids - Compositions and Catalysis

US 7,314,962 (2008) Alkylation of Aromatic Compounds
US 7,157,588 (2007) Ionic Liquids

     5-Methyl-N-Alkyl and Aryl Pyrrolidones

US 7,465,813 (2008) Process for making 5-methyl-N-alkyl-2-pyrrolidone from alkyl amine(s) and levulinic acid
US 7,030,249 (2006) Process for converting alpha-angelica lactone to 5-methyl-N-alkyl- 2-pyrrolidone using alkyl amines
US 7,129,362 (2006) Production of 5-methyl-N-aryl-2-pyrrolidone and 5-methyl-N-alkyl-2- pyrrolidone by reductive of levulinic acid esters with aryl and alkyl amines
US 7,030,249 (2006) Process for converting alpha-angelica lactone to 5-methyl-N-alkyl- 2-pyrrolidone using alkyl amines
US 7,030,074 (2006) Production of 5-methyl-N-(methyl aryl)-2-pyrrolidone, 5-methyl-N- (methyl cycloalkyl)-2-pyrrolidone and 5-methyl-N-alkyl-2-pyrrolidone by reductive amination of levulinic acid esters with cyano compounds
US 7,025,819(B2) (2006) Production of 5-methyl-n-(methylaryl)-2-pyrrolidone, 5-methyl-n-(methylcycloalkyl)-2-pyrrolidonea and 5-methyl-n-alkyl-2-pyrrolidone by reductive amination of levulinic acid esters with cyano compounds
US 7,014,697(B2) (2006) Production of 5-methyl-n-(methyl aryl)-2-pyrrolidone, 5-methyl-n-(methyl cycloalkyl) -2-pyrrolidone and 5-methyl-n-alkyl-2-pyrrolidone by reductive amination of levulinic acid esters with cyano compounds
US 7,002,024 (B2) (2006) Production of N-aryl-2-lactam and N-alkyl-2-lactam by reductive amination of lactones with aryl amines
US 6,995,275(B2) (2006) Production of N-aryl-2-lactam and N-alkyl-2-lactam by reductive amination of lactones with aryl and alkyl nitro compounds
US 6,992,195(B2) (2006) Production of N-aryl-2-lactam and N-cycloalkyl-2-lactam by reductive amination of lactones with arylamines
US 6,991,744 (B2) (2006) Refrigerant Compositions Containing a Compatibilizer
US 6,987,192 (B2) (2006) Production of N-aryl-2-lactam and N-alkyl-2-lactam by reductive amination of lactones with aryl and alkyl nitro compounds
US 6,984,736 (B2) (2006) Production of N-aryl-2-lactam and N-alkyl-2-lactam by reductive amination of lactones with aryl and alkyl nitro compounds
US 6,982,339 (2006) Production of N-aryl-2-lactam and N-cycloalkyl-2-lactam by reductive amination of lactones with aryl amines
US 6,930,126 (2005) Production of 5-Methyl-N-(Methylaryl)-2-Pyrrolidone, 5-Methyl-N-(Methylcycloalkyl)-2-Pyrrolidone and 5-Methyl-N-Alkyl-2-Pyrrolidone by Reductive Amination of Levulinic Acid Esters with Cyano Compounds
US 6,916,842 (2005) Production of 5-Methyl-N-(Methylaryl)-2-Pyrrolidone, 5-Methyl-N-(Methylcycloalkyl)-2-Pyrrolidone and 5-Methyl-N-Alkyl-2-Pyrrolidone by Reductive Amination of Levulinic Acid Esters with Cyano Compounds
US 6,906,201 (2005) Production of N-(methyl aryl)-2-lactam, N-(methyl cycloalkyl)-2-lactam and N-alkyl-2-lactam by reductive amination of lactones with aryl and alkyl cyano compounds
US 6,903,222 (2005) Production of 5-methyl-N-aryl-2-pyrrolidone and 5-methyl-N- cycloalkyl-2-pyrrolidone by reductive amination of levulinic acid with aryl amines
US 6,900,337 (2005) Production of 5-methyl-1-hydrocarbyl-2-pyrrolidone by reductive amination of levulinic acid
US 6,863,722 (2005) Production of 5-methyl-n-aryl-2-pyrrolidone and 5-methyl-n-alkyl-2- pyrrolidone by reductive amination of levulinic acid with nitro compounds
US 6,855,731 (2005) Production of 5-methyl-N-aryl-2-pyrrolidone and 5-methyl-N-alkyl-2- pyrrolidone by reductive amination of levulinic acid esters with nitro compounds
US 6,841,520 (2005) Production of 5-methyl-N-aryl-2-pyrrolidone and 5-methyl-N-cycloalkyl-2- pyrrolidone by reductive amination of levulinic acid with cyano compounds
US 6,828,278 (2004) Production of N-aryl-2-lactam and N-cycloalkyl-2-lactam by reductive amination of lactones with aryl amines
US 6,828,277 (2004) Production of N-aryl-2-Lactam and N-Alkyl-2-Lacatam by reductive amination of lactones with aryl and alkyl nitro compounds
US 6,818,593 (2004) Production of 5-methylene-N-aryl-2-pyrrolidone and 5-methyl-N-alkyl-2-pyrrolidone by reductive amination of levulinic acid with nitro compounds
US 6,743,819 (2004) Production of 5-methyl-N-aryl-2-pyrrolidone and 5-methyl-N-cycloalkyl-2- pyrrolidone by reductive amination of levulinic acid with aryl amines

     Gamma-Valerolactone and It's Derivatives

US 6,946,563 (2005) Production of 5-methyl-dihydro-furan-2-one from levulinic acid in supercritical media
US 6,756,501 (2004) Manufacture of 3-MethylTetrahydrofuran from alpha-Methylene-Gamma-Butyrolactone in a Single Step Process
US 6,673,946 (2004) Manufacture of 3-methyl-tetrahydrofuran from 2-methyl-butyrolactone
US 6,664,402 (2003) Manufacture of 3-methyl-tetrahydrofuran from alpha-methylene-gamma-butyrolactone in a two step process
US 6,617,464 (2003) Production of 5-methylbutyrolactone from levulinic acid

     Nylon Intermediates

US 6,835,849 (2004) Synthesis of alkenoate esters from lactones and alcohols

II. 1,3-Propanediol Derivatives

US 7,074,968 (2006) Continuous process for the preparation of polytrimethylene ether glycol
US 6,977,291 (2005) Production of Polytrimethylene Ether Glycol and Copolymers Thereof
US 6,720,459 (2004) Continuous process for the preparation of polytrimethyleneether glycol
US 7,402,711 (2008) Preparation of poly(tetramethylene) glycol
US 7,405,330 (2008) Preparation of polytrimethylene ether glycol and copolymers thereof

III. Catmint Oil Derived Insecticides

US 7,067,677B2 (2006) Production of dihydronepetalactone by hydrogenation of nepetalactone

IV. Erythritol Hydrogenation to Tetrahydrofuran

US 7,019,155(B2) (2006) Hydrogenation of Tetrahydroxybutane to Tetrahydrofuran
US 6,593,481 (2003) Hydrogenation of 3,4-tetrahydrofurandiol to tetrahydrofuran

V. Enzyme Catalysis

US 6,670,158 (2003) Method for producing methacrylic acid and acrylic acid with a combination of enzyme catalysts
US 6,582,943 (2002) Method for producing 2-hydroxyisobutyric acid and methacrylic acid from acetone cyanohydrin

VI.Gas to Liquids (Fischer Tropsch)

US 6,759,439 (2004) Fischer-Tropsch processes and catalysts with promoters
US 6,727,289 (2004) Boron promoted catalysts and Fischer Tropsch processes
US 6,602,921 (2003) Process for the preparation of hydrocarbons
US 6,489,371 (2002) Fischer-Tropsch processes and catalysts with promoters
US 6,476,085 (2002) Fischer-Tropsch processes using catalysts on mesoporous supports
US 6,368,997 (2002) Fischer-Tropsch processes and catalysts using fluorided supports
US 6,365,544 (2002) Fischer-Tropsch processes and catalysts using fluorided alumina supports
US 6,353,035 (2002) Fischer-Tropsch processes using xerogel and aerogel catalysts by destabilizing aqueous colloids
US 6,333,294 (2001) Fischer-Tropsch processes and catalysts with promoters
US 6,319,872 (2001) Fischer-Tropsch processes using catalysts on mesoporous supports
US 6,235,677 (2001) Fischer-Tropsch processes using xerogel and aerogel catalysts by destabilizing aqueous colloids

VII. Hydrocarbon Routes to p-Xylene

US 7,071,371 (2006) Gel catalysts and methods for their use in catalytic dehydrogenation processes
US 7,067,708(B2) (2006) Process for the preparation of p-xylene
US 6,696,388 (2004) Gel catalysts and process for preparing thereof
US 6,686,310 (2004) High Surface Area Metal Oxide Catalysts Incorporating Metals and Metal Ions
US 6,600,081 (2003) Process for the preparation of p-xylene
US 6,475,950 (2002) Catalytic dehydrogenation processes and chromium catalysts for use therein

VIII. Environmentally Safer Phosgene Catalysts

US 6,054,612 (2000) Phosgene manufacturing process
US 6,054,107 (2000) Phosgene manufacturing process
US 6,022,993 (2000) Phosgene manufacturing process
US 5,879,652 (1999) Process for producing oxochlorides of sulfur
US 5,759,508 (1998) Process for producing oxochlorides of sulfur

IX. Fluoromonomer Catalysis

US 6,706,935 (2004) Catalytic equilibration to increase the relative mole fraction of CF3CHFCl, CF3CHCl2 or CF3CF2H in a composition
US 6,624,337 (2003) Process for the manufacture of fluoroolefins
US 5,286,824 (1993) Process for the preparation of halogenated 2,2-bis(trifluoromethyl)-1,3-dioxolanes
US 5,068,472 (1991) Multistep synthesis of hexafluoropropylene
US 5,057,634 (1991) Multistep synthesis of hexafluoropropylene
US 5,043,491 (1991) Multistep synthesis of hexafluoropropylene

X. Chlorofluorocarbon Replacements

US 6,762,333 (2004) Process for Reducing the Fluorine Content of Hydrofluorocarbons and Hydrohalofluorocarbons
US 6,281,396 (2001) Fluorocarbon purification process
US 5,763,698 (1998) Process for reducing the fluorine content of hydrofluorocarbons and hydrohalofluorocarbons
US 5,523,498 (1996) Process for reducing the fluorine content of hydrofluorocarbons and hydrohalofluorocarbons
US 5,461,177 (1995) Fluorocarbon purification process
US 5,345,016 (1994) Manufacture of 1,1,1,2-tetrafluoroethane
US 5,302,765 (1994) Catalytic process for producing CF3CHClF
US 5,261,948 (1993) Carbon molecular sieve for the kinetic separation of acid gases and fluorocarbons
US 5,243,106 (1993) Processes using aluminum fluoride catalyst compositions for preparing 1,1-dichloro-1,2,2,2-tetrafluoroethane
US 5,220,083 (1993) Synthesis of perfluoropropane
US 5,243,108 (1993) Aluminum fluoride catalyst compositions and use thereof in a chlorofluorination process for preparing 1,1-dichloro-1,2,2,2-tetrafluoroethane
US 5,185,482 (1993) Manufacture of 1,1,1,2-tetrafluoroethane
US 5,177,224 (1993) Process for the preparation of halogenated 2,2-bis(trifluoromethyl)-1,3-dioxolanes
US 5,120,883 (1992) Catalytic process for producing CCl3CF3
US 5,094,773 (1992) Azeotropes of HF and process for the separation of HF via azeotropic distillation
US 5,051,537 (1991) Gas-phase fluorination
US 5,026,930 (1991) Gas-phase fluorination process
US 5,008,476 (1991) Process for the preparation of 1,1,1,2-tetrafluoroethane
US 5,008,475 (1991) Gas-phase fluorination process
US 4,944,846 (1990) Process for the separation of HF via Azeotropic distillation
US 4,935,558 (1990) Reductive dechlorination of 1,1,1,2-tetrafluoro-2-chloroethane
US 4,922,037 (1990) Gas-phase fluorination process
US 4,911,792 (1990) Process for the separation of HF via phase separation and distillation
US 4,902,838 (1990) Isomerization of saturated fluorohydrocarbons
US 4,843,181 (1989) Process for the manufacture of 1,1,1-trifluorodichloroethane and 1,1,1,2-tetrafluorochloroethane
US 4,766,260 (1988) Gas-phase fluorination process
US 4,766,259 (1988) Gas-phase fluorination process

XI. Homogeneous Catalysis

US 6,369,257 (2002) Hydroformylation of olefins using supported bis(phosphorus) ligands
US 6,288,253 (2001) Supported dendrimer catalyst
US 6,284,927 (2001) Hydroperoxide decomposition process
US 6,229,052 (2001) Hydroformylation of olefins using supported bis(phosphorus) ligands
US 4,057,565 (1977) 2-Dialkylaminobenzyl and 2-dialkylaminomethylphenyl derivatives of selected transition metals
US 4,042,610 (1977) Process for preparing hydrocarbyl and silahydrocarbyl transition metal dihydrocarbylamides