Hydrocarbon pretreatment process for catalytic cracking

Claim 2

A process for pretreating heavy hydrocarbon feedstock for use as a feed in the production of liquid hydrocarbon fuels comprising the steps of: (a) delivering the heavy hydrocarbon feedstock to a tubular thermal-pretreating reactor; (b) delivering hot particulate solids to the tubular thermal-pretreating reactor; (c) vaporizing the heavy hydrocarbon feed-stock at temperature between 1050° F. and 1200° F.; and a residence time of 0.05 to 0.20 seconds.

Claim 3

A process as in claim 1 further comprising the step of heating the particulate solids to a temperature up to 1800° F. by combusting the carbon formed on the particles during the pretreating reaction and delivering the particulate solids to the tubular thermal-pretreating reactor in a weight ratio to the heavy hydrocarbon feed of 3 to 60.

Claim 4

A process as in claim 1 wherein the heavy hydrocarbon is a residual oil.

Claim 5

A process as in claim 1 wherein the reaction products are quenched to a temperature below 850° F.

Claim 6

A process as in claim 1 wherein the reaction conditions comprise a solids to feed ratio by weight between 5 to 30 and the hydrocarbon feed is preheated to between 600° F. to 800° F.

Claim 7

A process as in claim 1 wherein the hydrocarbon feed is Arabian atmospheric tower bottoms and the reaction conditions comprise a temperature of about 1100° F.; a residence time of about 0.02 seconds; a reactor pressure of about 20 psig and a solids to feed ratio by weight of about 8.

Claim 8

A process as in claim 1 further comprising the step of immediately delivering the separated cracking gas from the thermal pretreating reactor to a catalytic cracker.

Claim 9

A process as in claim 7 wherein the process conditions in the catalytic cracker comprise a reactor outlet temperature of about 970° F.

Claim 10

A process as in claim 8 wherein the process conditions in the catalytic cracker comprise a reactor pressure of about 20 psig; the catalytic solids are at a temperature of 1530° F. when introduced to the catalytic reactor; the gas from the thermal pretreating reactor is at about 1100° F.; the ratio by weight of catalytic solids to the thermally pretreated gas feed to the catalytic reactor is about 1 and water is introduced to the catalytic reactor to maintain the catalytic cracking temperature at about 970° F.

Claim 11

A process as in claim 9 wherein the heavy hydrocarbon feed is a residual oil.

Claim 12

A process as in claim 1 wherein the hydrocarbon feed and hot particulate solids are delivered to the tubular cracking reactor through a reactor feeder having vertical passages communicating with the tubular cracking reactor and the solids in a hot solids vessel, means for providing localized fluidization to the solids above the vertical passages and means for delivering the heavy hydrocarbon to the tubular reactor at an angle to the path of the particulate solids entering the tubular reactor.

Claim 13

A process as in claim 1, wherein the particulate solids and the pretreated product gases are separated in a separator wherein the particulate solids pretreated product gases enter the separator through a separator inlet and change direction ninety degrees; the pretreated product gases change direction another ninety degrees to effect a one hundred and eighty degree reversal in direction from the entry direction; the particulate solids continue in the path oriented ninety degrees from the particulate solids-pretreated product gas separator inlet and thereafter, the path of the particulate solids is directed downwardly.

Claim 14

A process as in claim 1, wherein the particulate solids and pretreated product gases are separated in a separator comprising a chamber for rapidly disengaging about 80% of the particulate solids from the incoming mixed phase stream, said chamber having approximately rectilinear longitudinal side walls to form a flow path of height H and width W approximately rectangular in cross section, said chamber also having a mixed phase inlet of inside width D i , a gas outlet, and a solids outlet, said inlet being at one end of the chamber and disposed normal to the flow path the height H of which is equal to at least D i or 4 inches, whichever is greater, and the width W of which is no less than 0.75 D i but no more than 1.25 D i , said solids outlet being at the opposite end of the chamber and being suitably arranged for the downflow of discharged solids by gravity, and said gas outlet being therebetween at a distance no greater than 4 D i from the inlet as measured between respective centerlines and oriented to effect a 180° change in direction of the gas whereby resultant centrifugal forces direct the solid particles in the incoming stream toward a wall of the chamber opposite to the inlet forming thereat and maintaining an essentially static bed of solids, the surface of the bed defining a curvilinear path of an arc of approximately 90° of a circle for the outflow of solids to the solids outlet.

Claim 15

A process for pretreating heavy hydrocarbon feedstock for use as a feed in the production of liquid hydrocarbon fuels comprising the steps of: (a) delivering the heavy hydrocarbon feedstock to a tubular thermal pretreating reactor; (b) delivering hot particulate solids to the tubular thermal pretreating reactor; (c) pretreating the heavy hydrocarbon feedstock at a temperature between 1050° F. and 1200° F.; and a residence time of 0.20 to 0.50 seconds wherein the heavy hydrocarbon feedstock is vaporized thereby forming a pretreated gas. (d) separating the pretreated gas from the particulate solids; (e) immediately delivering the separated pretreated gas from the thermal pretreating reactor to a catalytic reactor; and (f) catalytically cracking the pretreated effluent from the thermal cracking reactor.

Claim 16

A process for pretreating heavy hydrocarbon feedstock for use as a feed in the production of liquid hydrocarbon fuels comprising the steps of: (a) delivering the heavy hydrocarbon feedstock to a tubular thermal pretreating reactor; (b) delivering hot particulate solids to the tubular thermal pretreating reactor; (c) pretreating the heavy hydrocarbon feedstock at a temperature between 1050° F. and 1200° F.; and a residence time of 0.20 to 0.50 seconds wherein the heavy hydrocarbon feedstock is vaporized thereby forming a pretreated gas. (d) separating the pretreated gas from the particulate solids; (e) immediately delivering the separated pretreated gas from the thermal pretreating reactor to a catalytic reactor; and (f) catalytically cracking the pretreated effluent from the thermal cracking reactor.

Claim 17

A process as in claim 14 wherein the catalytic cracking conditions comprise a reactor outlet temperature of 950° F. to 1150° F.

Claim 18

A process as in claim 15 wherein the process conditions in the catalytic cracker comprise a reactor pressure of 0 to 350 psig; the catalyst solids delivered to the reactor are at a temperature of 1000° F. to 1700° F.; the ratio of catalytic solids to the thermally pretreated gas feed to the catalytic cracker is 0.1 to 20.

Claim 19

A process as in claim 14 wherein the catalytic cracking conditions comprise a catalytic reactor outlet temperature of about 970° F.; a reactor pressure of about 20 psig; the catalyst to solids are at a temperature of about 1530° F. when introduced to the catalytic reactor; the gas from the thermal pretreating reactor is about 1100° F.; the ratio by weight of catalytic solids to the thermally pretreated gas feed to the catalytic reactor is about 1 and water is introduced to the catalytic reactor to maintain the catalyst cracking temperature at about 970° F.