Alkylation/transalkylation in presence of crystalline aluminosilicate catalyst

Claim 2

A process for effecting alkylation of an aromatic hydrocarbon charge selected from the group consisting of aromatic hydrocarbons and aromatic hydrocarbons containing a non-polar substituent which comprises contacting said hydrocarbon charge with an alkylating agent under conditions effective for accomplishing said alkylation including a reactor inlet temperature between about 100° F and about 1200° F, a reactor pressure between atmospheric and about 3000 psig, employing a mole ratio of hydrocarbon charge to alkylating agent in the approximate range of 1:3 to 20:1 and a weight hourly space velocity between about 0.5 and 1000 in the presence of a catalyst comprising a crystalline aluminosilicate zeolite, or a product of heating said zeolite to a temperature of from about 500° F to about 1500° F, characterized by the X-ray diffraction pattern of Table 1 and a formula, expressed in terms of mole ratios of oxides in the anhydrous state, as follows: (0.3-2.5)R.sub.2 O:(0-0.8)M.sub.2 O:Al.sub.2 O.sub.3 : > 8SiO.sub.2 wherein R is an organic nitrogen-containing cation derived from ethylenediamine or pyrrolidine and M is an alkali metal cation, said zeolite being further characterized, after calcination at 600° C, by exhibiting a sorption ratio of n-hexane/2-methylpentane of less than 10 at 90° C.

Claim 3

The process of claim 1 wherein the alkylating agent is an olefin.

Claim 4

The process of claim 2 wherein the reactor inlet temperature is between about 100° F and 950° F and the reactor pressure is between about 25 psig and 800 psig.

Claim 5

The process of claim 2 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is characterized by a SiO 2 :Al 2 O 3 ratio between greater than 8 and about 50.

Claim 6

The process of claim 2 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is combined in an amount between about 1 and about 99 weight percent in a binder therefor.

Claim 7

The process of claim 5 wherein said binder is alumina.

Claim 8

The process of claim 1 wherein the alkylating agent is an alcohol.

Claim 9

The process of claim 7 wherein the reactor inlet temperature is between about 400° F and 1200° F and the reactor pressure is between about 25 psig and 800 psig.

Claim 10

The process of claim 7 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is characterized by a SiO 2 :Al 2 O 3 ratio between greater than 8 and about 50.

Claim 11

The process of claim 7 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is combined in an amount between about 1 and about 99 weight percent in a binder therefor.

Claim 12

The process of claim 10 wherein said binder is alumina.

Claim 13

A process for effecting transalkylation of an aromatic hydrocarbon charge selected from the group consisting of aromatic hydrocarbons and aromatic hydrocarbons containing a non-polar substituent which comprises contacting said hydrocarbon charge with a transalkylating agent under conditions effective for accomplishing said transalkylation including a reactor inlet temperature between about 650° F and about 1100° F, a reactor pressure between atmospheric and about 3000 psig, employing a mole ratio of hydrocarbon charge to transalkylating agent in the approximate range of 1:3 to 20:1 and a weight hourly space velocity between about 0.5 and 1000 in the presence of a catalyst comprising a crystalline aluminosilicate zeolite, or a product of heating said zeolite to a temperature of from about 500° F to about 1500° F, characterized by the X-ray diffraction pattern of Table 1 and a formula, expressed in terms of mole ratios of oxides in the anhydrous state, as follows: (0.3-2.5)R.sub.2 O:(0-0.8)M.sub.2 O:Al.sub.2 O.sub.3 : > 8SiO.sub.2 wherein R is an organic nitrogen-containing cation derived from ethylenediamine or pyrrolidine and M is an alkali metal cation, said zeolite being further characterized, after calcination at 600° C, by exhibiting a sorption ratio of n-hexane/2-methylpentane of less than 10 at 90° C.

Claim 14

A process for effecting transalkylation of an aromatic hydrocarbon charge selected from the group consisting of aromatic hydrocarbons and aromatic hydrocarbons containing a non-polar substituent which comprises contacting said hydrocarbon charge with a transalkylating agent under conditions effective for accomplishing said transalkylation including a reactor inlet temperature between about 650° F and about 1100° F, a reactor pressure between atmospheric and about 3000 psig, employing a mole ratio of hydrocarbon charge to transalkylating agent in the approximate range of 1:3 to 20:1 and a weight hourly space velocity between about 0.5 and 1000 in the presence of a catalyst comprising a crystalline aluminosilicate zeolite, or a product of heating said zeolite to a temperature of from about 500° F to about 1500° F, characterized by the X-ray diffraction pattern of Table 1 and a formula, expressed in terms of mole ratios of oxides in the anhydrous state, as follows: (0.3-2.5)R.sub.2 O:(0-0.8)M.sub.2 O:Al.sub.2 O.sub.3 : > 8SiO.sub.2 wherein R is an organic nitrogen-containing cation derived from ethylenediamine or pyrrolidine and M is an alkali metal cation, said zeolite being further characterized, after calcination at 600° C, by exhibiting a sorption ratio of n-hexane/2-methylpentane of less than 10 at 90° C.

Claim 15

The process of claim 12 wherein the reactor pressure is between about 25 psig and 800 psig.

Claim 16

The process of claim 12 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is characterized by a SiO 2 :Al 2 O 3 ratio between greater than 8 and about 50.

Claim 17

The process of claim 12 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is combined in an amount between about 1 and about 99 weight percent in a binder therefor.

Claim 18

The process of claim 15 wherein said binder is alumina.

Claim 19

The process of claim 12 wherein the aromatic hydrocarbon charge is toluene and the transalkylating agent is trimethylbenzene.

Claim 20

The process of claim 12 wherein the aromatic hydrocarbon charge is toluene and the transalkylating agent is toluene.

Claim 21

A process for effecting alkylation of an aromatic hydrocarbon charge selected from the group consisting of aromatic hydrocarbons and aromatic hydrocarbons containing a non-polar substituent which comprises contacting said hydrocarbon charge with an alkylating agent under conditions effective for accomplishing said alkylation including a reactor inlet temperature between about 100° F and about 1200° F, a reactor pressure between atmospheric and about 3000 psig, employing a mole ratio of hydrocarbon charge to alkylating agent in the approximate range of 1:3 to 20:1 and a weight hourly space velocity between about 0.5 and 1000 in the presence of a catalyst comprising a crystalline aluminosilicate zeolite, or a product of heating said zeolite to a temperature of from about 500° F to about 1500° F, characterized by the X-ray diffraction pattern of Table 2 and a formula, expressed in terms of mole ratios of oxides in the anhydrous state, as follows: (0.3-2.5)R.sub.2 O:(0-0.8)M.sub.2 O:Al.sub.2 O.sub.3 : > 8SiO.sub.2 wherein R is an organic nitrogen-containing cation derived from a 2-(hydroxyalkyl) trialkylammonium compound and M is an alkali metal cation, said zeolite being further characterized, after calcination at 600° C, by exhibiting a sorption ratio of n-hexane/2-methylpentane of less than 10 at 90° C.

Claim 22

A process for effecting alkylation of an aromatic hydrocarbon charge selected from the group consisting of aromatic hydrocarbons and aromatic hydrocarbons containing a non-polar substituent which comprises contacting said hydrocarbon charge with an alkylating agent under conditions effective for accomplishing said alkylation including a reactor inlet temperature between about 100° F and about 1200° F, a reactor pressure between atmospheric and about 3000 psig, employing a mole ratio of hydrocarbon charge to alkylating agent in the approximate range of 1:3 to 20:1 and a weight hourly space velocity between about 0.5 and 1000 in the presence of a catalyst comprising a crystalline aluminosilicate zeolite, or a product of heating said zeolite to a temperature of from about 500° F to about 1500° F, characterized by the X-ray diffraction pattern of Table 2 and a formula, expressed in terms of mole ratios of oxides in the anhydrous state, as follows: (0.3-2.5)R.sub.2 O:(0-0.8)M.sub.2 O:Al.sub.2 O.sub.3 : > 8SiO.sub.2 wherein R is an organic nitrogen-containing cation derived from a 2-(hydroxyalkyl) trialkylammonium compound and M is an alkali metal cation, said zeolite being further characterized, after calcination at 600° C, by exhibiting a sorption ratio of n-hexane/2-methylpentane of less than 10 at 90° C.

Claim 23

A process for effecting transalkylation of an aromatic hydrocarbon charge selected from the group consisting of aromatic hydrocarbons and aromatic hydrocarbons containing a non-polar substituent which comprises contacting said hydrocarbon charge with a transalkylating agent under conditions effective for accomplishing said transalkylation including a reactor inlet temperature between about 650° F and about 1100° F, a reactor pressure between atmospheric and about 3000 psig, employing a mole ratio of hydrocarbon charge to transalkylating agent in the approximate range of 1:3 to 20:1 and a weight hourly space velocity between about 0.5 and 1000 in the presence of a catalyst comprising a crystalline aluminosilicate zeolite, or a product of heating said zeolite to a temperature of from about 500° F to about 1500° F, characterized by the X-ray diffraction pattern of Table 2 and a formula, expressed in terms of mole ratios of oxides in the anhydrous state, as follows: (0.3-2.5)R.sub.2 O:(0-0.8)M.sub.2 O:Al.sub.2 O.sub.3 : > 8SiO.sub.2 wherein R is an organic nitrogen-containing cation derived from a 2-(hydroxyalkyl) trialkylammonium compound and M is an alkali metal cation, said zeolite being further characterized, after calcination at 600° C, by exhibiting a sorption ratio of n-hexane/2-methylpentane of less than 10 at 90° C.

Claim 24

A process for effecting transalkylation of an aromatic hydrocarbon charge selected from the group consisting of aromatic hydrocarbons and aromatic hydrocarbons containing a non-polar substituent which comprises contacting said hydrocarbon charge with a transalkylating agent under conditions effective for accomplishing said transalkylation including a reactor inlet temperature between about 650° F and about 1100° F, a reactor pressure between atmospheric and about 3000 psig, employing a mole ratio of hydrocarbon charge to transalkylating agent in the approximate range of 1:3 to 20:1 and a weight hourly space velocity between about 0.5 and 1000 in the presence of a catalyst comprising a crystalline aluminosilicate zeolite, or a product of heating said zeolite to a temperature of from about 500° F to about 1500° F, characterized by the X-ray diffraction pattern of Table 2 and a formula, expressed in terms of mole ratios of oxides in the anhydrous state, as follows: (0.3-2.5)R.sub.2 O:(0-0.8)M.sub.2 O:Al.sub.2 O.sub.3 : > 8SiO.sub.2 wherein R is an organic nitrogen-containing cation derived from a 2-(hydroxyalkyl) trialkylammonium compound and M is an alkali metal cation, said zeolite being further characterized, after calcination at 600° C, by exhibiting a sorption ratio of n-hexane/2-methylpentane of less than 10 at 90° C.

Claim 25

The process of claim 19 wherein the alkylating agent is an olefin.

Claim 26

The process of claim 21 wherein the reactor inlet temperature is between about 100° F and 950° F and the reactor pressure is between about 25 psig and 800 psig.

Claim 27

The process of claim 21 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is characterized by a SiO 2 :Al 2 O 3 ratio between greater than 8 and about 50.

Claim 28

The process of claim 21 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is combined in an amount between about 1 and about 99 weight percent in a binder therefor.

Claim 29

The process of claim 24 wherein said binder is alumina.

Claim 30

The process of claim 19 wherein the alkylating agent is an alcohol.

Claim 31

The process of claim 26 wherein the reactor inlet temperature is between about 400° F and 1200° F and the reactor pressure is between about 25 psig and 800 psig.

Claim 32

The process of claim 26 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is characterized by a SiO 2 :Al 2 O 3 ratio between greater than 8 and about 50.

Claim 33

The process of claim 26 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is combined in an amount between about 1 and about 99 weight percent in a binder therefor.

Claim 34

The process of claim 29 wherein said binder is alumina.

Claim 35

The process of claim 20 wherein the reactor pressure is between about 25 psig and 800 psig.

Claim 36

The process of claim 20 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is characterized by a SiO 2 :Al 2 O 3 ratio between greater than 8 and about 50.

Claim 37

The process of claim 20 wherein the crystalline aluminosilicate zeolite or the product of heating said zeolite is combined in an amount between about 1 and about 99 weight percent in a binder therefor.

Claim 38

The process of claim 33 wherein said binder is alumina.

Claim 39

The process of claim 20 wherein the aromatic hydrocarbon charge is toluene and the transalkylating agent is trimethylbenzene.

Claim 40

The process of claim 20 wherein the aromatic hydrocarbon charge is toluene and the transalkylating agent is toluene.