Cracking catalyst and manufacture thereof

Claim 2

A process for producing an attrition-resistant zeolitic cracking catalyst which comprises providing a finely divided mixture comprising particles of sodium zeolite Y, sodium zeolite B and amorphous silica-alumina, mixing said mixture of particles with a solution of sodium silicate to form a slurry without milling, washing or drying said mixture prior to or subsequent to addition of sodium silicate, spray drying said slurry to form microspheres, forming an acidic slurry containing said microspheres and then subjecting the microspheres to ion-exchange treatment to reduce the sodium content thereof without an intermediate drying step.

Claim 3

The process of claim 1 wherein said mixture comprises about 20-40% sodium zeolite Y, about 20-40% sodium zeolite B and the balance being amorphous silica-alumina.

Claim 4

The process of claim 2 wherein said mixture is obtained as a by-product in the manufacture of a fluid cracking catalyst from microspheres of calcined clay and sodium hydroxide solution.

Claim 5

The process of claim 3 wherein said sodium silicate is sodium disilicate obtained as a by-product in the manufacture of fluid cracking catalyst.

Claim 6

The process of claim 1 wherein sufficient sodium silicate is present in the microspheres produced by spray dryer to result in the incorporation of about 10% to 35% SiO 2 by weight in the ion exchanged microspheres, said weight being based on the dry weight of said microspheres.

Claim 7

A fluid cracking catalyst produced by the process of claim 1.

Claim 8

The catalyst of claim 6 which has a surface area in the range of 225 to 325 m 2 /g; and a pore structure characterized by less than 0.15 cc/g porosity in the 20 to 100A diameter range; and an Engelhard Attrition Index below 2.

Claim 9

A process for producing a family of fluid cracking catalysts, members of said family differing in overall composition and performance when used in catalytic cracking, said process comprising: (a) mixing microspheres of kaolin clay calcined to undergo the exotherm with a sodium hydroxide solution, metakaolin being optionally present, (b) heating the mixture until crystals of sodium zeolite Y form in the microspheres and silica is leached therefrom, resulting in the formation of a sodium disilicate aqueous mother liquor, ultrafine solids comprising sodiyn zeolite Y, and microspheres containing sodium zeolite Y and also the silica-depleted residue of calcined kaolin clay; (c) separating said microspheres containing zeolite Y from step (b) from said sodium disilicate aqueous mother liquor under conditions such that said ultrafine crystals of zeolite Y and other ultrafine solids remain in the aqueous effluent, whereby zeolite Y is present in both the microspheres separated in step (c) and the aqueous effluent from step (c) (d) recovering said ultrafine crystals of sodium zeolite Y and the other ultrafine solids from the aqueous effluent in step (c); (e) mixing the recovered ultrafine solids from step (d) with sodium silicate to form a slurry, (f) spray drying said slurry from step (e) to form microspheres comprising ultrafine solids recovered in step (d) and including crystals of sodium zeolite Y; (g) separately acidifying at least a portion of the zeolite Y-containing microspheres obtained in and recovered in step (c) step (b) and at least a portion of the zeolite Y containing microspheres from step (f), and ion-exchanging the microspheres in the slurries thus-acidified to replace sodium with more desirable cations; (h) and recovering as separate products the two different types of ion exchanged microspheres, both types of microspheres comprising zeolite Y, the microsphere resulting from the separation in step (c) having an overall SiO 2 /Al 2 O 3 molar ratio appreciably less than 1.5/1 and the microspheres resulting from the separation of ultrafine solids in step (c) and recovery in step (d) followed by spray drying in step (f) having an overall SiO 2 /Al 2 O 3 ratio greater than 1.8/1.

Claim 10

A process for producing a family of fluid cracking catalysts, members of said family differing in overall composition and performance when used in catalytic cracking, said process comprising: (a) mixing microspheres of kaolin clay calcined to undergo the exotherm with a sodium hydroxide solution, metakaolin being optionally present, (b) heating the mixture until crystals of sodium zeolite Y form in the microspheres and silica is leached therefrom, resulting in the formation of a sodium disilicate aqueous mother liquor, ultrafine solids comprising sodiyn zeolite Y, and microspheres containing sodium zeolite Y and also the silica-depleted residue of calcined kaolin clay; (c) separating said microspheres containing zeolite Y from step (b) from said sodium disilicate aqueous mother liquor under conditions such that said ultrafine crystals of zeolite Y and other ultrafine solids remain in the aqueous effluent, whereby zeolite Y is present in both the microspheres separated in step (c) and the aqueous effluent from step (c) (d) recovering said ultrafine crystals of sodium zeolite Y and the other ultrafine solids from the aqueous effluent in step (c); (e) mixing the recovered ultrafine solids from step (d) with sodium silicate to form a slurry, (f) spray drying said slurry from step (e) to form microspheres comprising ultrafine solids recovered in step (d) and including crystals of sodium zeolite Y; (g) separately acidifying at least a portion of the zeolite Y-containing microspheres obtained in and recovered in step (c) step (b) and at least a portion of the zeolite Y containing microspheres from step (f), and ion-exchanging the microspheres in the slurries thus-acidified to replace sodium with more desirable cations; (h) and recovering as separate products the two different types of ion exchanged microspheres, both types of microspheres comprising zeolite Y, the microsphere resulting from the separation in step (c) having an overall SiO 2 /Al 2 O 3 molar ratio appreciably less than 1.5/1 and the microspheres resulting from the separation of ultrafine solids in step (c) and recovery in step (d) followed by spray drying in step (f) having an overall SiO 2 /Al 2 O 3 ratio greater than 1.8/1.

Claim 11

The process of claim 8 wherein the sodium silicate used in step (e) is sodium disilicate.

Claim 12

The process of claim 8 wherein the sodium silicate used in step (e) is obtained from sodium disilicate formed in step (b) and separated as mother liquor in step (c).

Claim 13

The process of claim 8 wherein substantially all of the solids recovered in step (d) are finer than about 20 microns equivalent spherical diameter.

Claim 14

The process of claim 8 wherein the material recovered in step (d) comprises about 20 to 40% sodium zeolite Y and about 20 to 40% sodium zeolite B.

Claim 15

The process of claim 8 wherein the material recovered in step (d) is saturated with sodium disilicate.

Claim 16

The process of claim 8 wherein the microspheres from step (f) are ion-exchange with an ammonium salt to reduce the sodium content and then ion-exchanged with a rare earth salt without an intermediate drying step.

Claim 17

The process of claim 14 wherein said ultrafine solids are not successively ion-exchanged with an ammonium salt until the Na 2 O content is below about 0.5.

Claim 18

The process of claim 8 wherein sufficient sodium silicate is added in step (e) to result in a product containing about 10% to 35% by weight SiO 2 derived from sodium silicate.

Claim 19

The process of claim 8 wherein the product contains about 20% by weight SiO 2 derived from sodium silicate.