Abstract: Disclosed herein in certain embodiments is a fluid catalyst cracking (FCC) additive composition that includes a first component, a second component, and optionally a third component. The first component includes beta zeolite and a first matrix. The second component includes ZSM-5 zeolite and a second matrix. The third component includes Y zeolite and a third matrix. The components are present in the additive composition in a range that provides for enhanced butylenes to propylene selectivity ratio and total butylenes yield when catalytically cracking a hydrocarbon feed.

Abstract: Disclosed herein is a fluid catalyst cracking (FCC) catalyst composition that includes a first component and a second component. The first component includes zeolite Y and a first matrix that includes a metal passivating constituent. The second component includes beta zeolite and a second matrix. Also disclosed herein are methods of preparing the FCC catalyst composition and method of using the FCC catalyst composition.

Abstract: Disclosed herein is a fluid catalyst cracking (FCC) catalyst composition that includes a first component and a second component. The first component and second component may be separate microspheroidal FCC catalysts or may be incorporated in a common microspheroidal FCC catalyst. The first component includes zeolite Y and a first matrix that includes gamma-alumina. The second component includes beta zeolite and a second matrix. Also disclosed herein are methods of preparing the FCC catalyst composition and method of using the FCC catalyst composition.

Abstract: The present technology provides an adsorbent material that includes a silicate composition, wherein the silicate composition includes a crystalline phase; wherein the silicate composition may have an interconnected porous scaffold having a total mercury (Hg) pore volume of about 0.005 cc/g to about 0.25 cc/g for pores having a diameter of about 20-10,000 ? and a total nitrogen (N) pore volume of about 0.02 cc/g to about 0.1 cc/g for pores having a diameter of about 20-600 ?.

Abstract: A process for mechanical destructuring of cellulosic biomass was developed that makes use of a short application of high compression, impact, and shearing forces. The biomass may be destructured using a specific energy input that is less than 40% of the total combustible energy of the biomass. The destructured biomass, with or without saccharification and/or in-feed glycosyl hydrolase enzymes, may be used in feed applications.

Abstract: Disclosed herein are processes for preparing an ?,?-Cn-diol, wherein n is 5 or greater, from a feedstock comprising a Cn oxygenate. In one embodiment, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising Pt, Cu, Ni, Pd, Pt, Rh, Ir, Ru, or Fe on a WO3 or WOx support. In one embodiment, the process comprises contacting the feedstock with hydrogen in the presence of a catalyst comprising a metal M1 and a metal M2 or an oxide of M2, and optionally a support. In one embodiment, M1 is Pd, Pt, or Ir; and M2 is Mo, W, V, Mn, Re, Zr, Ni, Cu, Zn, Cr, Ge, Sn, Ti, Au, or Co. The Cn oxygenate may be obtained from a biorenewable resource.

Abstract: Disclosed herein are processes for preparing an ?,?-Cn-diol, wherein n is 5 or greater, from a feedstock comprising a Cn oxygenate. In one embodiment, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising Pt, Cu, Ni, Pd, Pt, Rh, Ir, Ru, or Fe on a WO3 or WOx support. In one embodiment, the process comprises contacting the feedstock with hydrogen in the presence of a catalyst comprising a metal M1 and a metal M2 or an oxide of M2, and optionally a support. In one embodiment, M1 is Pd, Pt, or Ir; and M2 is Mo, W, V, Mn, Re, Zr, Ni, Cu, Zn, Cr, Ge, Sn, Ti, Au, or Co. The Cn oxygenate may be obtained from a biorenewable resource.

Abstract: Disclosed herein are processes for preparing an ?,?-Cn-diol, wherein n is 5 or greater, from a feedstock comprising a Cn oxygenate. In one embodiment, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising Pt, Cu, Ni, Pd, Pt, Rh, Ir, Ru, or Fe on a WO3 or WOx support. In one embodiment, the process comprises contacting the feedstock with hydrogen in the presence of a catalyst comprising a metal M1 and a metal M2 or an oxide of M2, and optionally a support. In one embodiment, M1 is Pd, Pt, or Ir; and M2 is Mo, W, V, Mn, Re, Zr, Ni, Cu, Zn, Cr, Ge, Sn, Ti, Au, or Co. The Cn oxygenate may be obtained from a biorenewable resource.

Abstract: A process for mechanical destructuring of cellulosic biomass was developed that makes use of a short application of high compression, impact, and shearing forces. The biomass may be destructured using a specific energy input that is less than 40% of the total combustible energy of the biomass. The destructured biomass, with or without saccharification and/or in-feed glycosyl hydrolase enzymes, may be used in feed applications.

Abstract: Disclosed herein are processes for preparing an ?,?-Cn-diol, wherein n is 5 or greater, from a feedstock comprising a Cn oxygenate. In one embodiment, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising Pt, Cu, Ni, Pd, Pt, Rh, Ir, Ru, or Fe on a WO3 or WOx support. In one embodiment, the process comprises contacting the feedstock with hydrogen in the presence of a catalyst comprising a metal M1 and a metal M2 or an oxide of M2, and optionally a support. In one embodiment, M1 is Pd, Pt, or Ir; and M2 is Mo, W, V, Mn, Re, Zr, Ni, Cu, Zn, Cr, Ge, Sn, Ti, Au, or Co. The Cn oxygenate may be obtained from a biorenewable resource.

Abstract: Disclosed herein are processes for preparing an ?,?-Cn-diol, wherein n is 5 or greater, from a feedstock comprising a Cn oxygenate. In one embodiment, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising Pt, Cu, Ni, Pd, Pt, Rh, Ir, Ru, or Fe on a WO3 or WOx support. In one embodiment, the process comprises contacting the feedstock with hydrogen in the presence of a catalyst comprising a metal M1 and a metal M2 or an oxide of M2, and optionally a support. In one embodiment, M1 is Pd, Pt, or Ir; and M2 is Mo, W, V, Mn, Re, Zr, Ni, Cu, Zn, Cr, Ge, Sn, Ti, Au, or Co. The Cn oxygenate may be obtained from a biorenewable resource.

Abstract: Disclosed are processes for preparing 1,2-cyclohexanediol, and mixtures of 1,2-cyclohexanediol and 1,6-hexanediol, by hydrogenating 1,2,6-hexanetriol.

Abstract: Disclosed are processes for preparing 1,6-hexanediol and synthetic intermediates useful in the production of 1,6-hexanediol from renewable biosources. In one embodiment, a process comprises contacting levoglucosenone with hydrogen in the presence of a first hydrogenation catalyst at a first temperature to form product mixture (I); and heating product mixture (I) in the presence of hydrogen and a second hydrogenation catalyst at a second temperature to form product mixture (II) which comprises 1,6-hexanediol.

Abstract: Disclosed are processes for preparing 1,6-hexanediol from levoglucosenone. In one embodiment, the process comprises contacting levoglucosenone with hydrogen in the presence of a hydrogenation catalyst comprising palladium, platinum/tungsten, nickel/tungsten, rhodium/rhenium, or mixtures thereof at a first temperature between about 50° C. and 100° C. and at a first reaction pressure between about 50 psi and 2000 psi for a first reaction period, and at a second temperature between about 120° C. and 250° C. and at a second pressure between about 500 psi and 2000 psi for a second reaction period to form a product mixture comprising 1,6-hexanediol, wherein the first reaction period is the amount of time in which the levoglucosenone has a conversion of at least about 95%.

Abstract: Disclosed are processes for preparing 1,6-hexanediol from levoglucosenone. In one embodiment, the process comprises contacting levoglucosenone with hydrogen in the presence of a hydrogenation catalyst comprising palladium, platinum/tungsten, nickel/tungsten, rhodium/rhenium, or mixtures thereof at a first temperature between about 50° C. and 100° C. and at a first reaction pressure between about 50 psi and 2000 psi for a first reaction period, and at a second temperature between about 120° C. and 250° C. and at a second pressure between about 500 psi and 2000 psi for a second reaction period to form a product mixture comprising 1,6-hexanediol, wherein the first reaction period is the amount of time in which the levoglucosenone has a conversion of at least about 95%. In one embodiment, the 1,6-hexanediol is converted to 1,6-diaminohexane.

Abstract: Disclosed herein are processes comprising contacting isosorbide with hydrogen in the presence of a first hydrogenation catalyst to form a first product mixture comprising tetrahydrofuran-2,5-dimethanol. The processes can further comprise heating the first product mixture in the presence of hydrogen and a second hydrogenation catalyst to form a second product mixture comprising 1,6-hexanediol. The first and second hydrogenation catalysts can be the same or different.

Abstract: Disclosed are processes comprising contacting an aqueous reaction mixture having an initial pH between about 3 and about 6 and comprising levoglucosenone with a catalyst, and heating the reaction mixture to form a product mixture comprising 5-hydroxymethyl-2-furfural. The processes may further comprise heating the product mixture comprising 5-hydroxymethyl-2-furfural in the presence of hydrogen and a hydrogenation catalyst to form a second product mixture comprising one or more of 2,5-furandimethanol, tetrahydrofuran 2,5-dimethanol, 1,2,6-hexanetriol, 2-hydroxymethyltetrahydropyran, and 1,6-hexanediol.

Abstract: Disclosed are processes for preparing 1,6-hexanediol and synthetic intermediates useful in the production of 1,6-hexanediol from renewable biosources. In one embodiment, a process comprises contacting levoglucosenone with hydrogen in the presence of a first hydrogenation catalyst at a first temperature to form product mixture (I); and heating product mixture (I) in the presence of hydrogen and a second hydrogenation catalyst at a second temperature to form product mixture (II) which comprises 1,6-hexanediol. In one embodiment, the 1,6-hexanediol is converted to 1,6-diaminohexane.

Abstract: Disclosed herein are processes for preparing an ?,?-Cn-diol, wherein n is 5 or greater, from a feedstock comprising a Cn oxygenate. In some embodiments, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising metals M1, M2, and M3 and optionally a support, wherein: M1 is Mn, Cr, V, or Ti; M2 is Ni, Co, or Fe; and M3 is Cu, Ag, Pt, Pd or Au; or M1 is Pt or Rh; M2 is Cu, Ni or Pd; and M3 is Mo, Re or W. The Cn oxygenate may be obtained from a biorenewable resource.

Abstract: Disclosed herein are processes for preparing an ?,?-Cn-diol, wherein n is 5 or greater, from a feedstock comprising a Cn oxygenate. In one embodiment, the process comprises contacting the feedstock with hydrogen gas in the presence of a catalyst comprising a first metal component comprising Ni, Ir, Pt, Rh, Ru, Pd, Fe, Ag, or Au; a heteropoly acid component comprising H3[P(W3O10)4], H4[Si(W3O10)4], H4[P(Mo3O10)4], H4[Si(Mo3O10)4], Cs2.5H0.5[P(W3O10)4]Cs2.5H0.5[Si(W3O10)4], or mixtures thereof; optionally a second metal component comprising Cr, a Cr oxide, Ni, a Ni oxide, Fe, a Fe oxide, Co, a Co oxide, Mn, a Mn oxide, Mo, a Mo oxide, W, a W oxide, Re, a Re oxide, Zn, a Zn oxide, SiO2, or Al2O3; optionally at least one promoter comprising Na, K, Mg, Rb, Cs, Ca, Sr, Ba, Ce, or mixtures thereof; and optionally a support.