A fluid catalytic cracking catalyst for hydrocarbon oil that is a blend of two types of fluid catalytic cracking catalysts each of which has a different hydrogen transfer reaction activity or has a pore distribution within a specific range after being pseudo-equilibrated. One catalyst is a catalyst containing a zeolite and matrix components, and the other catalyst is a catalyst containing a zeolite and matrix components. This catalyst is composed of the one catalyst and the other catalyst blended at a mass ratio within a range of 10:90 to 90:10.

Disclosed herein are modified zeolites and methods for making modified zeolites. In one or more embodiments disclosed herein, a modified zeolite may include a microporous framework including a plurality of micropores having diameters of less than or equal to 2 nm. The microporous framework may include at least silicon atoms and oxygen atoms. The modified zeolite may further include organometallic moieties each bonded to a nitrogen atom of a secondary amine functional group including a nitrogen atom and a hydrogen atom. The organometallic moieties may include a titanium atom that is bonded to the nitrogen atom of the secondary amine functional group. The nitrogen atom of the secondary amine function group may bridge the titanium atom of the organometallic moiety and a silicon atom of the microporous framework.

The present invention features a direct synthesis of light olefins through the hydrogenation of carbon dioxide. In.sub.2O.sub.3 supported on cubic phase yttria-stabilized zirconia is used as a catalyst and is mixed with a molecular sieve to perform the hydrogenation. The cubic crystal structure of the yttria-stabilized zirconium dioxide is an excellent support for indium oxide particles and prevents their deactivation during CO.sub.2 hydrogenation. This direct synthesis route promotes a stable and efficient method for producing light olefins.

A catalytic cracking catalyst contains 10-70 wt % of a cracking active component, 10-60 wt % of a binder and 10-70 wt % of a clay. The cracking active component has 5-100 wt % of a first Y-type molecular sieve and 0-95 wt % of a second molecular sieve. The first Y-type molecular sieve is a modified molecular sieve based on the crystal modification of kaolin and has the sodium oxide content of less than 2 wt %. The process for preparing the catalyst includes the steps of vigorously mixing and stirring a cracking active component comprising a modified molecular sieve based on the crystal modification of kaolin, a binder and a clay with water; spray drying; washing; filtering; and drying. The catalyst is used in the catalytic cracking reaction of heavy oils, and has a good coke selectivity, as well as a higher heavy oil conversion rate.

A process of making an aromatization catalyst comprising: (a) mixing a zeolite, a binder, and water to form a mixture; (b) extruding the mixture to form a green extrudate; (c) drying the green extrudate to form a dried green extrudate; (d) calcining the dried green extrudate to form a support, wherein calcining the dried green extrudate is the only calcination step in the process; (e) washing the support to form a washed support; (f) drying the washed support to form a dried washed support; (g) impregnating the dried washed support with a Group 8-10 transition metal compound and at least one halide-containing compound to form a metalized-halided material; and (h) vacuum drying the metalized-halided material to form a dried metalized-halided material which is the aromatization catalyst.

Disclosed are a catalyst for preparing hydrocarbons from carbon dioxide by one-step hydrogenation and a method for preparing same. The catalyst includes nano-metal oxides and hierarchical zeolites, where the mass fraction of the nano-metal oxides in the catalyst is 10%-90%, and the mass fraction of the hierarchical zeolites in the catalyst is 10%-90%. The catalyst has excellent catalytic performance, good reaction stability and high selectivity for desired products, and in the hydrocarbons, C.sub.2.sup.=-C.sub.4.sup.= reach up to 80%, C.sub.5+ reach up to 80%, and aromatics reach up to 65%.

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 processing paraffinic naphtha include contacting a paraffinic naphtha feedstock with a catalyst system in a dehydrogenation reactor. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite to produce a dehydrogenated product stream. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite. The framework-substituted USY-type zeolite has a modified USY framework. The modified USY framework includes a USY aluminosilicate framework modified by substituting a portion of framework aluminum atoms of the USY aluminosilicate framework with substitution atoms independently selected from the group consisting of titanium atoms, zirconium atoms, hafnium atoms, and combinations thereof. A dehydrogenation catalyst for dehydrogenating a paraffinic naphtha includes the framework-substituted ultra-stable Y (USY)-type zeolite.

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.

A method for producing a hydrocracking catalyst includes preparing a framework substituted Y-type zeolite, preparing a binder, co-mulling the framework substituted Y-type zeolite, the binder, and one or more hydrogenative metal components to form a catalyst precursor, and calcining the catalyst precursor to generate the hydrocracking catalyst. The framework substituted Y-type zeolite is prepared by calcining a Y-type zeolite at 500° C. to 700° C. to form a calcined Y-type zeolite. Further, the framework substituted Y-type zeolite is prepared by forming a suspension containing the calcined Y-type zeolite, the suspension having a liquid to solid mass ratio of 5 to 15, adding acid to adjust the pH of the suspension to less than 2.0, adding and mixing one or more of a zirconium compound, a hafnium compound, or a titanium compound to the suspension, and neutralizing the pH of the suspension to obtain the framework substituted Y-type zeolite.