Continuous removal of polynuclear aromatics from hydrocarbon recycle oil

Claim 2

A catalytic hydrocracking process comprising: (A) contacting a hydrocarbon feedstock in a hydrocracking zone with added hydrogen and a hydrocracking catalyst at a temperature and pressure sufficient to give a substantial conversion to lower boiling products; and (B) condensing a hydrocarbon effluent from the hydrocracking zone and separating the condensed effluent into (i) a low boiling hydrocarbon product and (ii) an unconverted hydrocarbon oil boiling above about 650° F. and containing one or more aliphatic compounds and one or more fused polynuclear aromatic compounds, the unconverted hydrocarbon oil then being fed as the feed mixture stream into a continuous chromatographic process comprising the steps of (a) simultaneously introducing a feed mixture stream, a desorbing reagent stream, and a regenerator reagent stream proximate the entrance end of an adsorbent bed, the feed stream comprising a mixture of aliphatic compounds and fused polynuclear aromatic compounds, wherein the compounds and fused polynuclear aromatic compounds, wherein the fused polynuclear aromatic compounds have a greater affinity than the aliphatic compounds for the bed, the desorbing stream comprises a liquid capable of removing the fused polynuclear aromatic compounds from the bed, and the regenerator stream comprises a gas capable of regenerating the bed, (b) moving the streams with respect to the bed, and (c) removing a first stream and a substantially separate second stream proximate the exit end of the bed, the first stream having a high concentration of aliphatic compounds with respect to the concentration of fused polynuclear aromatic compounds in the first stream and the second stream having a high concentration of fused polynuclear aromatic compounds with respect to the concentration of aliphatic compounds in the second stream.

Claim 3

The method of claim 1 further comprising the step (D) of recycling the aliphatic compounds exiting the adsorption bed to the hydrocracking zone.

Claim 4

The method of claim 1 further comprising the step (D) of delivering the aliphatic compounds exiting the adsorption bed to a different hydrocracking zone.

Claim 5

The method of claim 1 wherein the feed mixture stream, the desorbing reagent stream, and the regenerator reagent stream are simultaneously introduced at a pressure of at least about 100 psig each.

Claim 6

The method of claim 1 wherein step (b) includes the step of moving the streams with respect to the bed so that (I) substantially all of the bed is sequentially contacted with (i) the feed mixture stream, (ii) the desorbing reagent stream, and (iii) the regenerator reagent stream, and (II) substantially all the polynuclear aromatic compounds are sorbed onto the bed, substantially all the sorbed aromatic compounds then being removed from the bed by the desorbing reagent stream, and substantially all the desorbing reagent stream being removed from the bed by the regenerator reagent stream.

Claim 7

The method of claim 1 wherein step (a) includes the step of simultaneously introducing a purge reagent stream proximate the entrance end of the bed.

Claim 8

The method of claim 6 wherein step (b) includes the step of moving the streams with respect to the bed so that (I) the bed is sequentially contacted with (i) the feed mixture stream, (ii) the purge reagent stream, (iii) the desorbing reagent stream, and (iv) regenerator reagent stream, and (II) substantially all the polynuclear aromatic compounds are sorbed onto the bed, substantially all the sorbed aromatic compounds then being removed from the bed by the desorbing reagent stream, and substantially all the desorbing reagent stream being removed from the bed by the regenerator reagent stream.

Claim 9

The method of claim 7 wherein the purge reagent stream and regenerator reagent stream have substantially the same composition.

Claim 10

The method of claim 7 wherein the purge reagent stream and the regenerator reagent stream are both an inert gas.

Claim 11

The method of claim 1 further comprising the step (d) of recycling the desorbing reagent stream by removing a substantial portion of any polynuclear aromatic compounds in the desorbing reagent stream exiting the bed, thereby forming a recyclable desorbing reagent stream, and introducing the recyclable desorbing reagent stream proximate the entrance end of the bed.

Claim 12

The method of claim 1 further comprising the step (d) of recycling the desorbing reagent stream by removing a substantial portion of any polynuclear aromatic compounds in the desorbing reagent stream exiting the bed, thereby forming a recyclable desorbing reagent stream, and introducing the recyclable desorbing reagent stream proximate the entrance end of the bed, wherein the regenerator stream is a heated gas and step (b) includes the step of moving the streams with respect to the bed so that (I) substantially all of the bed is sequentially contacted with (i) the feed mixture stream, (ii) the desorbing reagent stream, and (iii) the regenerator reagent stream, and (II) substantially all the fused polynuclear aromatic compounds are sorbed onto the bed, substantially all the sorbed fused polynuclear aromatic compounds being removed from the bed by the desorbing reagent stream, and substantially all the desorbing reagent stream being removed from the bed by the regenerator reagent stream.

Claim 13

The method of claim 1 further comprising the step (d) of recycling the desorbing reagent stream by removing a substantial portion of any polynuclear aromatic compounds in the desorbing reagent stream exiting the bed, thereby forming a recyclable desorbing reagent stream, and introducing the recyclable desorbing reagent stream proximate the entrance end of the bed, wherein the regenerator stream is a heated gas, step (a) includes the step of simultaneously introducing a purge reagent stream proximate the entrance end of the bed, and step (b) includes the step of moving the streams with respect to the bed so that (I) substantially all of the bed is sequentially contacted with (i) the feed mixture stream, (ii) the purge reagent stream, (iii) the desorbing reagent stream, and (iv) the regenerator reagent stream, and (II) substantially all the fused polynuclear aromatic compounds are sorbed onto the bed, the purge reagent stream substantially preventing contact between the aliphatic compounds and the desorbing reagent stream, substantially all the sorbed fused polynuclear aromatic compounds being removed from the bed by the desorbing reagent stream, and substantially all the desorbing reagent stream being removed from the bed by the regenerator reagent stream.

Claim 14

The method of claim 1 wherein the adsorption bed has a plurality of substantially parallel, transverse ribs separating the bed into a plurality of substantially separate sections.

Claim 15

An oil refining process comprising: (A) forming a liquid capable of solubilizing aromatic compounds having at least about 5 fused aromatic rings; and (B) catalytically hydrocracking a hydrocarbon feedstock by: (i) contacting the feedstock in a hydrocracking zone with added hydrogen and a hydrocracking catalyst at a temperature and pressure sufficient to give a substantial conversion to lower boiling products; and (ii) condensing a hydrocarbon effluent from the hydrocracking zone and separating the condensed effluent into (AA) a low boiling hydrocarbon product and (BB) an unconverted hydrocarbon oil containing one or more fused polynuclear aromatic compounds, the unconverted hydrocarbon oil then being fed as the feed mixture stream into a continuous chromatographic process comprising the steps of (a) simultaneously introducing a feed mixture stream, a desorbing reagent stream, and a regenerator reagent stream proximate the entrance end of an adsorbent bed, the feed stream comprising a mixture of aliphatic compounds and fused polynuclear aromatic compounds, wherein the compounds and fused polynuclear aromatic compounds, wherein the fused polynuclear aromatic compounds have a greater affinity than the aliphatic compounds for the bed, the desorbing stream comprises a liquid capable of removing the fused polynuclear aromatic compounds from the bed, and the regenerator stream comprises a gas capable of regenerating the bed, (b) moving the streams with respect to the bed, and (c) removing a first stream and a substantially separate second stream proximate the exit end of the bed, the first stream having a high concentration of aliphatic compounds with respect to the concentration of fused polynuclear aromatic compounds in the first stream and the second stream having a high concentration of fused polynuclear aromatic compounds with respect to the concentration of aliphatic compounds in the second stream wherein at least a portion of the solvent formed in step (A) is used as the desorbing reagent stream.

Claim 16

An oil refining process comprising: (A) forming a liquid capable of solubilizing aromatic compounds having at least about 5 fused aromatic rings; and (B) catalytically hydrocracking a hydrocarbon feedstock by: (i) contacting the feedstock in a hydrocracking zone with added hydrogen and a hydrocracking catalyst at a temperature and pressure sufficient to give a substantial conversion to lower boiling products; and (ii) condensing a hydrocarbon effluent from the hydrocracking zone and separating the condensed effluent into (AA) a low boiling hydrocarbon product and (BB) an unconverted hydrocarbon oil containing one or more fused polynuclear aromatic compounds, the unconverted hydrocarbon oil then being fed as the feed mixture stream into a continuous chromatographic process comprising the steps of (a) simultaneously introducing a feed mixture stream, a desorbing reagent stream, and a regenerator reagent stream proximate the entrance end of an adsorbent bed, the feed stream comprising a mixture of aliphatic compounds and fused polynuclear aromatic compounds, wherein the compounds and fused polynuclear aromatic compounds, wherein the fused polynuclear aromatic compounds have a greater affinity than the aliphatic compounds for the bed, the desorbing stream comprises a liquid capable of removing the fused polynuclear aromatic compounds from the bed, and the regenerator stream comprises a gas capable of regenerating the bed, (b) moving the streams with respect to the bed, and (c) removing a first stream and a substantially separate second stream proximate the exit end of the bed, the first stream having a high concentration of aliphatic compounds with respect to the concentration of fused polynuclear aromatic compounds in the first stream and the second stream having a high concentration of fused polynuclear aromatic compounds with respect to the concentration of aliphatic compounds in the second stream wherein at least a portion of the solvent formed in step (A) is used as the desorbing reagent stream.

Claim 17

A catalytic hydrocracking process comprising: (A) contacting a hydrocarbon feedstock in a hydrocracking zone with added hydrogen and a hydrocracking catalyst at a temperature and pressure sufficient to give a substantial conversion to lower boiling products; (B) condensing a hydrocarbon effluent from the hydrocracking zone and separating the condensed effluent into (i) a low boiling hydrocarbon product and (ii) an unconverted hydrocarbon oil boiling above about 650° F. and containing one or more aliphatic compounds and one or more fused polynuclear aromatic compounds; (C) simultaneously introducing the unconverted hydrocarbon oil, a desorbing reagent stream, and a regenerator reagent stream proximate the entrance end of an adsorbent bed, wherein the fused polynuclear aromatic compounds in the unconverted hydrocarbon oil have a greater affinity than the aliphatic compounds in the unconverted hydrocarbon oil for the bed, the desorbing stream comprises a liquid capable of removing the fused polynuclear aromatic compounds from the bed, and the regenerator stream comprises a gas capable of regenerating the bed; (D) moving the streams with respect to the bed; and (E) removing, proximate the exit end of the bed, a first stream having a high molar ratio of the aliphatic compounds to the fused polynuclear aromatic compounds and a second stream having a high molar ratio of the fused polynuclear aromatic compounds to the aliphatic compounds.

Claim 18

A catalytic hydrocracking process comprising: (A) contacting a hydrocarbon feedstock in a hydrocracking zone with added hydrogen and a hydrocracking catalyst at a temperature and pressure sufficient to give a substantial conversion to lower boiling products; (B) condensing a hydrocarbon effluent from the hydrocracking zone and separating the condensed effluent into (i) a low boiling hydrocarbon product and (ii) an unconverted hydrocarbon oil boiling above about 650° F. and containing one or more aliphatic compounds and one or more fused polynuclear aromatic compounds; (C) simultaneously introducing the unconverted hydrocarbon oil, a desorbing reagent stream, and a regenerator reagent stream proximate the entrance end of an adsorbent bed, wherein the fused polynuclear aromatic compounds in the unconverted hydrocarbon oil have a greater affinity than the aliphatic compounds in the unconverted hydrocarbon oil for the bed, the desorbing stream comprises a liquid capable of removing the fused polynuclear aromatic compounds from the bed, and the regenerator stream comprises a gas capable of regenerating the bed; (D) moving the streams with respect to the bed; and (E) removing, proximate the exit end of the bed, a first stream having a high molar ratio of the aliphatic compounds to the fused polynuclear aromatic compounds and a second stream having a high molar ratio of the fused polynuclear aromatic compounds to the aliphatic compounds.

Claim 19

The method of claim 15 wherein the first stream is substantially devoid of the fused polynuclear aromatic compounds.

Claim 20

The method of claim 15 wherein the second stream is substantially devoid of the aliphatic compounds.

Claim 21

The method of claim 15 wherein the first stream is substantially devoid of the fused polynuclear aromatic compounds, and the second stream is substantially devoid of the aliphatic compounds.