Xylene isomerization

Claim 2

An isomerization process for manufacture of xylenes from an initial feed stream comprising C 8 aromatics and containing xylenes which comprises contacting said feed stream with a catalyst containing at least one NZMS which has been either calcined, hydrotreated or chemically treated to remove at least a portion of the template used in the manufacture of the NZMS, or, alternatively, is calcined, hydrotreated or chemically treated in situ prior to carrying out the isomerization process at effective isomerization conditions to provide a selected xylene isomer in a greater concentration than the concentration of said xylene isomer initially in said feed stream wherein said NZMS is characterized in the calcined form by an absorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20° C. and is further characterized after removal of the template by an adsorption of triethylamine less than 5 percent by weight at a pressure of 2.6 torr and a temperature of 22° C.

Claim 3

In a process for conversion of a mixture of aromatic compounds having 8 carbon atoms, said mixture containing ethylbenzene and xylenes, to isomerize xylenes contained in said mixture and convert at least part of said ethylbenzene; the improvement which comprises contacting such mixture with a catalyst containing at least one NZMS catalyst which has been either calcined, hydrotreated or chemically treated to remove at least a portion of the template used in the manufacture of the NZMS, or, alternatively, is calcined, hydrotreated or chemically treated in situ prior to carrying out the isomerization process, in the presence of added hydrogen at effective process conditions to isomerize xylenes containing in said mixture and to convert at least part of said ethylbenzene, wherein said NZMS is characterized in the calcined form by an adsorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20° C. and is further characterized after removal of the template by an adsorption of triethylamine of less than 5 percent by weight at a pressure of 2.6 torr and a temperature of 22° C.

Claim 4

In a process for conversion of a mixture of aromatic compounds having 8 carbon atoms, said mixture containing ethylbenzene and xylenes, to isomerize xylenes contained in said mixture and convert at least part of said ethylbenzene; the improvement which comprises contacting such mixture with a catalyst containing at least one NZMS catalyst which has been either calcined, hydrotreated or chemically treated to remove at least a portion of the template used in the manufacture of the NZMS, or, alternatively, is calcined, hydrotreated or chemically treated in situ prior to carrying out the isomerization process, in the presence of added hydrogen at effective process conditions to isomerize xylenes containing in said mixture and to convert at least part of said ethylbenzene, wherein said NZMS is characterized in the calcined form by an adsorption of isobutane of at least 2 percent by weight at a partial pressure of 500 torr and a temperature of 20° C. and is further characterized after removal of the template by an adsorption of triethylamine of less than 5 percent by weight at a pressure of 2.6 torr and a temperature of 22° C.

Claim 5

The process of claim 1 wherein said NZMS is characterized in the calcined form by an adsorption of isobutane of at least 4 percent by weight at a partial pressure of 500 torr and a temperature of 20° C.

Claim 6

The process of claim 2 wherein said NZMS is further characterized in its calcined form by an adsorption of isobutane of at least 4 percent by weight at a pressure of 500 torr and a temperature of 20° C.

Claim 7

The process of claim 1 or claim 2 wherein said NZMS is characterized in the calcined form by an adsorption of triethylamine of less than 3 percent by weight at a pressure of 2.6 torr and a temperature of 22° C.

Claim 8

The process of claim 1 or claim 2 wherein said catalyst contains an effective amount of at least one crystalline aluminosilicate or crystalline silicate to achieve isomerization or conversion, having activity for the isomerization of xylenes in a weight ratio between about 1:100 and about 100:1 of said zeolitic aluminosilicate to said NZMS molecular sieve and from 0 and about 99 weight percent of at least one inorganic oxide matrix component, based on the total weight of said catalyst.

Claim 9

The process of claim 6 wherein the inorganic oxide component is present in an amount between about 5 and about 95 percent by weight, based on the total weight of said catalyst.

Claim 10

The process of claim 2 wherein said effective process conditions include a temperature between about 500° F. to 1000° F.

Claim 11

The process of claim 8 wherein said effective process conditions include a temperature between about 650° F. and about 950° F.

Claim 12

The process of claim 1 or claim 2 wherein said NZMS has at least part of its cations as hydrogen or hydrogen-forming species.

Claim 13

The process of claim 10 wherein said hydrogen-forming species is NH 4 + .

Claim 14

The process of claim 2 wherein ethylbenzene is converted to a xylene.

Claim 15

The process of 7 wherein said inorganic oxide matrix component is selected from the group consisting of clays, silicas, aluminas, and mixtures thereof.

Claim 16

The process of 7 wherein said inorganic oxide matrix component is selected from the group consisting of clays, silicas, aluminas, and mixtures thereof.

Claim 17

The process of claim 1 or claim 2 wherein said NZMS is a SAPO.

Claim 18

The process of claim 1 or claim 2 wherein said NZMS is selected from the group consisting of CoAPSOs, FeAPSOs, MgAPSOs, MnAPSOs, TiAPSOs, ZnAPSOs, CoMgAPSOs, CoMnMgAPSOs, MeAPOs, TAPOs, FAPOs and mixture thereof.

Claim 19

The process of claim 1 or claim 2 wherein said NZMS is selected from the group consisting of CoAPSOs, FeAPSOs, MgAPSOs, MnAPSOs, TiAPSOs, ZnAPSOs, CoMgAPSOs, CoMnMgAPSOs and mixtures thereof.

Claim 20

The process of claim 1 or claim 2 wherein said NZMS is selected from the group consisting of ELAPSO-11, ELAPSO-31, ELAPSO-41, and mixtures thereof.

Claim 21

The process of claim 17 wherein said NZMS is selected from the group consisting of CoAPSO-11, CoAPSO-31, CoAPSO-41, FeAPSO-11, FeAPSO-31, FeAPSO-41, MgAPSO-11, MgAPSO-31, MgAPSO-41, MnAPSO-11, MnAPSO-31, MnAPSO-41, SAPO-11, SAPO-31, SAPO-41, TiAPSO-11, TiAPSO 31, TiAPSO-41, ZnAPSO-11, ZnAPSO-31, ZnAPSO-41, CoMgAPSO-11, CoMgAPSO-31, CoMgAPSO-41, CoMnMgAPSO-11, CoMnMgAPSO-31, CoMnMgAPSO-41 and mixtures thereof.

Claim 22

The process of claim 1 or claim 2 wherein said NZMS is selected from the group consisting of MeAPO-11, MeAPO-31, MeAPO-41, TAPO-11, TAPO-31, TAPO-41, FAPO-11, FAPO-31, FAPO-41 and mixtures thereof.

Claim 23

The process of claim 19 wherein "Me" is selected from the group consisting of cobalt magnesium, manganese and mixtures thereof.

Claim 24

The process of claim 19 wherein "Me" is selected from the group consisting of magnesium, manganese and mixtures thereof.

Claim 25

The process of claim 6 wherein said zeolitic aluminosilicate is selected from the group consisting of ferrierite, silicalite, ZSM-type zeolites and mixtures thereof.

Claim 26

The process of claim 2 wherein an effective amount of hydrogen is present and said catalyst contains an effective amount of at least one dehydrogenation catalyst to isomerized xylenes contained in said mixture and to convert at least part of said ethylbenzene.

Claim 27

The process of claim 23 wherein the hydrogenation component is selected from the group consisting of Pd, Pt, Ni and mixtures thereof.

Claim 28

The process of claim 24 wherein said hydrogenation component is present in an effective amount between 0.05 and about 3.0 wt. percent of at least one of Pd and Pt.

Claim 29

The process of claim 24 wherein the hydrogenation component is Ni and is present in an effective amount between about 0.05 and about 5.0 weight percent.

Claim 30

The process of claim 1 wherein said initial feed stream comprises m-xylene and said product contains a greater concentration of para-xylene than said initial feedstream.

Claim 31

The process of claim 1 wherein said product contains a greater concentration of o-xylene than said initial feed stream.

Claim 32

The process of claim 1 wherein said product contains a greater concentration of m-xylene than said initial feed stream.

Claim 33

The process of claim 1 wherein said initial feed stream contains ethylbenzene.