Catalytic upgrading of FCC effluent

Claim 2

A process for catalytically cracking a petroleum fraction, comprising the following steps in sequence: (a) contacting said petroleum fraction with a cracking catalyst under catalytic cracking conditions to produce a catalytically cracked product; (b) directly passing said catalytically cracked product to means for contacting said catalytically cracked product with a shape-selective crystalline silicate zeolite catalyst, and contacting said cracked product with said shape-selective catalyst under conditions to produce a product comprising a gasoline fraction having a higher octane number and comprising a light distillate oil fraction having a lower pour point than said catalytically cracked product; and (c) fractionating said product of step (b) to produce at least said gasoline fraction with improved octane number and said light distillate oil fraction with improved pour point.

Claim 3

The process of claim 1, wherein step (a) is conducted in a fluid catalytic cracking reactor.

Claim 4

The process of claim 1, wherein said shape-selective zeolite is selected from the group having the structure of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, TMA Offretite and Erionite.

Claim 5

The process of claim 1, wherein said shape-selective zeolite is ZSM-5.

Claim 6

The process of claim 1, wherein said shape-selective zeolite is Zeolite Beta.

Claim 7

The process of claim 1, wherein said catalytically cracked product is contacted with a shape-selective crystalline silicate zeolite at a temperature of 800° to 950° F., a pressure from atmospheric to 100 psig, and a space velocity LHSV of 100 to 4000.

Claim 8

The process of claim 1, wherein said shape-selective crystalline silicate zeolite comprises 65 wt % ZSM-5 and 35 wt % alumina, wherein said ZSM-5 has an alpha value of approximately 23.

Claim 9

The process of claim 1, wherein said shape-selective crystalline silicate zeolite comprises 50 wt % Zeolite Beta and 50 wt % alumina, wherein said Zeolite Beta has an alpha value of about 20.

Claim 10

The process of claim 1, wherein said catalytically cracked product is contacted with said shape-selective crystalline zeolite for a time between 14 and 34 seconds.

Claim 11

The process according to claim 1, wherein the catalytically cracked product is contacted with the shape-selective crystalline silicate zeolite catalyst in the absence of added hydrogen.

Claim 12

A process for simultaneously increasing the octane number of a gasoline fraction and improving the pour point of a light distillate oil fraction produced in a fluid catalytic cracking unit, comprising: (a) contacting a heavy hydrocarbon feed with a cracking catalyst in a fluid catalytic cracking unit under catalytic cracking conditions to produce a catalytically cracked product; (b) directly passing said catalytically cracked product to means for contacting said catalytically cracked product with a shape-selective crystalline silicate zeolite catalyst, and contacting said cracked product with said shape-selective catalyst under conditions to produce a product comprising a gasoline fraction having a higher octane number and comprising a light distillate oil fraction having a lower pour point than said catalytically cracked product; and (c) fractionating said product of step (b) to produce at least said gasoline fraction with improved octane number and said light distillate oil fraction with improved pour point.

Claim 13

A process for simultaneously increasing the octane number of a gasoline fraction and improving the pour point of a light distillate oil fraction produced in a fluid catalytic cracking unit, comprising: (a) contacting a heavy hydrocarbon feed with a cracking catalyst in a fluid catalytic cracking unit under catalytic cracking conditions to produce a catalytically cracked product; (b) directly passing said catalytically cracked product to means for contacting said catalytically cracked product with a shape-selective crystalline silicate zeolite catalyst, and contacting said cracked product with said shape-selective catalyst under conditions to produce a product comprising a gasoline fraction having a higher octane number and comprising a light distillate oil fraction having a lower pour point than said catalytically cracked product; and (c) fractionating said product of step (b) to produce at least said gasoline fraction with improved octane number and said light distillate oil fraction with improved pour point.

Claim 14

The process of claim 11, wherein said shape-selective zeolite is selected from the group having the structure of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, TMA Offretite and Erionite.

Claim 15

The process of claim 11, wherein said shape-selective zeolite is ZSM-5.

Claim 16

The process of claim 11, wherein said shape-selective zeolite is Zeolite Beta.

Claim 17

The process of claim 11, wherein said catalytically cracked product is contacted with a shape-selective crystalline silicate zeolite at a temperature of 800° to 950° F., a pressure from atmospheric to 100 psig, and a space velocity LHSV of 100 to 4000.

Claim 18

The process according to claim 11, wherein the catalytically cracked product is contacted with the shape-selective crystalline silicate zeolite catalyst in the absence of added hydrogen.

Claim 19

A process for catalytically cracking a petroleum fraction comprising the steps of, contacting said petroleum fraction with a cracking catalyst in a fluid catalytic cracking unit under cracking conditions to produce a catalytically cracked product, fractionating said catalytically cracked product under fractionating conditions, directly passing said cracked product to means for contacting said catalytically cracked product with a shape-selective crystalline silicate zeolite catalyst, prior to said fractionating, and contacting said cracked product with said shape-selective catalyst under conditions comprising a temperature of 800° to 950° F., a pressure for atmospheric to 100 psig, and a space velocity, LHSV of 100 to 4000, to produce a product comprising a gasoline fraction having a higher octane number and comprising a light oil distillate fraction having a lower pour point than comparably boiling gasoline and light oil distillate fractions, respectively, of said catalytically cracked product prior to said contacting with said shape-selective catalyst.

Claim 20

A process for catalytically cracking a petroleum fraction comprising the steps of, contacting said petroleum fraction with a cracking catalyst in a fluid catalytic cracking unit under cracking conditions to produce a catalytically cracked product, fractionating said catalytically cracked product under fractionating conditions, directly passing said cracked product to means for contacting said catalytically cracked product with a shape-selective crystalline silicate zeolite catalyst, prior to said fractionating, and contacting said cracked product with said shape-selective catalyst under conditions comprising a temperature of 800° to 950° F., a pressure for atmospheric to 100 psig, and a space velocity, LHSV of 100 to 4000, to produce a product comprising a gasoline fraction having a higher octane number and comprising a light oil distillate fraction having a lower pour point than comparably boiling gasoline and light oil distillate fractions, respectively, of said catalytically cracked product prior to said contacting with said shape-selective catalyst.

Claim 21

The process of claim 17, wherein said shape-selective zeolite is selected from the group having the structure of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, TMA Offretite and Erionite.

Claim 22

The process of claim 17, wherein said shape-selective zeolite is ZSM-5.

Claim 23

The process of claim 17, wherein said shape-selective zeolite is Zeolite Beta.

Claim 24

The process according to claim 17, wherein the catalytically cracked product is contacted with the shape-selective crystalline silicate zeolite catalyst in the absence of added hydrogen.

Claim 25

A process for catalytically cracking a petroleum fraction, comprising the following steps in sequence: (a) contacting said petroleum fraction with a cracking catalyst under catalytic cracking conditions to produce a catalytically cracked product comprising gasoline boiling range and distillate boiling range hydrocarbons; (b) contacting said gasoline and distillate boiling range hydrocarbons of said catalytically cracked product with a shape-selective crystalline silicate zeolite catalyst under dewaxing conditions to produce a dewaxed product; and (c) fractionating said dewaxed product to produce at least a gasoline fraction with improved octane number and a light distillate oil with improved pour point relative, respectively, to said gasoline boiling range hydrocarbons and a comparably boiling distillate oil fraction of said catalytically cracked product prior to said contacting with shape selective catalyst.

Claim 26

A process for catalytically cracking a petroleum fraction, comprising the following steps in sequence: (a) contacting said petroleum fraction with a cracking catalyst under catalytic cracking conditions to produce a catalytically cracked product comprising gasoline boiling range and distillate boiling range hydrocarbons; (b) contacting said gasoline and distillate boiling range hydrocarbons of said catalytically cracked product with a shape-selective crystalline silicate zeolite catalyst under dewaxing conditions to produce a dewaxed product; and (c) fractionating said dewaxed product to produce at least a gasoline fraction with improved octane number and a light distillate oil with improved pour point relative, respectively, to said gasoline boiling range hydrocarbons and a comparably boiling distillate oil fraction of said catalytically cracked product prior to said contacting with shape selective catalyst.

Claim 27

The process of claim 22, wherein step (a) is conducted in a fluid catalytic cracking reactor.

Claim 28

The process of claim 22, wherein said shape-selective zeolite is selected from the group having the structure of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, TMA Offretite and Erionite.

Claim 29

The process of claim 22, wherein said shape-selective zeolite is ZSM-5.

Claim 30

The process of claim 22, wherein said shape-selective zeolite is Zeolite Beta.

Claim 31

The process of claim 23 wherein said catalytically cracked product is contacted with said shape-selective crystalline silicate zeolite at a temperature of 800° to 950° F., a pressure from atmospheric to 100 psig, and a space velocity, LHSV of 100 to 4000.

Claim 32

The process of claim 27, wherein said shape-selective crystalline silicate zeolite comprises 65 wt % ZSM-5 and 35 wt % alumina, wherein said ZSM-5 has an alpha value of approximately 23.

Claim 33

The process of claim 27, wherein said shape-selective crystalline silicate zeolite comprises 50 wt % Zeolite Beta and 50 wt % alumina, wherein said Zeolite Beta has an alpha value of about 20.

Claim 34

The process of claim 27, wherein said catalytically cracked product is contacted with said shape-selective crystalline zeolite for a time between 14 and 34 seconds.