Processes for converting glucose to sorbose with tailored selectivity. The processes include contacting glucose with a silica-containing structure that includes a zeolite having a topology of a 10-membered ring or smaller and Lewis acidic M.sup.4+ framework centers, wherein M is Ti, Sn, Zr, or Hf. Contacting the glucose is conducted under reaction conditions sufficient to isomerize the glucose to sorbose.

Processes for converting glucose to sorbose with tailored selectivity. The processes include contacting glucose with a silica-containing structure that includes a zeolite having a topology of a 10-membered ring or smaller and Lewis acidic M.sup.4+ framework centers, wherein M is Ti, Sn, Zr, or Hf. Contacting the glucose is conducted under reaction conditions sufficient to isomerize the glucose to sorbose.

A method including subjecting an ultra-stable Y-type zeolite having a low silica-to-alumina molar ratio (SAR), such as in a range of 3 to 6, to acid treatment and heteroatom incorporation contemporaneously to give a framework-modified ultra-stable Y-type zeolite.

A method including subjecting an ultra-stable Y-type zeolite having a low silica-to-alumina molar ratio (SAR), such as in a range of 3 to 6, to acid treatment and heteroatom incorporation contemporaneously to give a framework-modified ultra-stable Y-type zeolite.

Methods for interconverting olefins in an olefin-rich hydrocarbon stream include contacting the olefin-rich hydrocarbon stream with a catalyst system in an olefin interconversion unit to produce an interconverted effluent comprising ethylene and propylene. The contacting may be conducted at a reaction temperature from 450° C. to 750° C., a reaction pressure from 1 bar to 5 bar, and a residence time from 0.5 seconds to 1000 seconds. The catalyst system includes a framework-substituted beta zeolite. The framework-substituted beta zeolite has a *BEA aluminosilicate framework that has been modified by substituting a portion of framework aluminum atoms of the *BEA aluminosilicate framework with beta-zeolite Al-substitution atoms independently selected from the group consisting of titanium atoms, zirconium atoms, hafnium atoms, and combinations thereof.

Methods for interconverting olefins in an olefin-rich hydrocarbon stream include contacting the olefin-rich hydrocarbon stream with a catalyst system in an olefin interconversion unit to produce an interconverted effluent comprising ethylene and propylene. The contacting may be conducted at a reaction temperature from 450° C. to 750° C., a reaction pressure from 1 bar to 5 bar, and a residence time from 0.5 seconds to 1000 seconds. The catalyst system includes a framework-substituted beta zeolite. The framework-substituted beta zeolite has a *BEA aluminosilicate framework that has been modified by substituting a portion of framework aluminum atoms of the *BEA aluminosilicate framework with beta-zeolite Al-substitution atoms independently selected from the group consisting of titanium atoms, zirconium atoms, hafnium atoms, and combinations thereof.

The present disclosure discloses a method for preparing caprolactam including: (1) contacting cyclohexanone oxime with a catalyst to carry out reaction in the presence of ethanol and under the condition of gas phase Beckmann rearrangement reaction of cyclohexanone oxime; (2) separating the reaction product obtained in step (1) to produce an ethanol solution of crude caprolactam, and then separating the ethanol solution of crude caprolactam to obtain ethanol and crude caprolactam; (3) removing impurities with boiling points lower than that of caprolactam in the crude caprolactam to obtain a light component removal product; (4) mixing the light component removal product with a crystallization solvent to carry out crystallization and solid-liquid separation to obtain a crystalline crystal; (5) subjecting the crystalline crystal to a hydrogenation reaction; wherein the crystallization solvent contains 0.1-2 wt % of ethanol.

An alkali metal ion modified titanium silicalite zeolite TS-1 for gas phase epoxidation of propylene and hydrogen peroxide and a preparation method thereof. The method includes: 1: preparing an alkali metal hydroxide modification solution containing a small amount of TPA.sup.+ ions; 2: conducting a controlled hydrothermal treatment on a TS-1 zeolite matrix by using the alkali metal hydroxide solution containing a small amount of TPA.sup.+ ions; and 3: conducting post-treatment on the hydrothermally modified TS-1 zeolite. In the washing process, the modified TS-1 zeolite wet material is washed with a low concentration alkali metal hydroxide solution; and alkali metal ions are reserved on the silicon hydroxyl of the modified titanium silicalite zeolite. The prepared alkali metal ion modified titanium silicalite zeolite has significantly improved catalytic performance in the gas phase epoxidation of propylene and hydrogen peroxide.

An alkali metal ion modified titanium silicalite zeolite TS-1 for gas phase epoxidation of propylene and hydrogen peroxide and a preparation method thereof. The method includes: 1: preparing an alkali metal hydroxide modification solution containing a small amount of TPA.sup.+ ions; 2: conducting a controlled hydrothermal treatment on a TS-1 zeolite matrix by using the alkali metal hydroxide solution containing a small amount of TPA.sup.+ ions; and 3: conducting post-treatment on the hydrothermally modified TS-1 zeolite. In the washing process, the modified TS-1 zeolite wet material is washed with a low concentration alkali metal hydroxide solution; and alkali metal ions are reserved on the silicon hydroxyl of the modified titanium silicalite zeolite. The prepared alkali metal ion modified titanium silicalite zeolite has significantly improved catalytic performance in the gas phase epoxidation of propylene and hydrogen peroxide.

Provided is a beta zeolite also having exceptional catalytic activity as a catalyst other than an olefin epoxidation catalyst. This beta zeolite is synthesized without using an organic structure-directing agent and has titanium in the structural skeleton thereof, the Ti content being 0.10 mmol/g or higher. This beta zeolite preferably has an Si/Ti molar ratio of 20-200. Also, the Si/Al molar ratio is preferably 100 or higher.