# US 8,772,563 B2 · Process for the conversion of ethane to aromatic hydrocarbons

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- Number: US 8,772,563 B2
- Document ID: US8772563B2
- Status: Granted
- Kind: B2
- Application number: 12/371,803
- Filed: 2009-02-16
- Published: 2009-08-20
- Granted: 2014-07-08
- Earliest claimed: 2008-02-18
- Assignees: Shell Oil Company
- Applicants: Ann Marie Lauritzen; Ajay Madhav Madgavkar
- Inventors: Ann Marie Lauritzen; Ajay Madhav Madgavkar
- Web page: https://patentgrep.com/patent/US8772563B2

## CPC

- B01J 29/44: Noble metals
- B01J 29/061: {containing metallic elements added to the zeolite}
- B01J 29/068: Noble metals
- B01J 29/405: {containing rare earth elements, titanium, zirconium, hafnium, zinc, cadmium, mercury, gallium, indium, thallium, tin or lead}
- C07C 2/76: by condensation of hydrocarbons with partial elimination of hydrogen
- C10G 45/70: with catalysts containing platinum group metals or compounds thereof
- B01J 37/0009: {Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst}
- B01J 2229/20: to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
- B01J 2229/42: Addition of matrix or binder particles
- C07C 2529/068: Noble metals
- C07C 2529/44: Noble metals
- C07C 2529/67: Noble metals
- C07C 2529/74: Noble metals
- Y02P 20/50: Improvements relating to the production of bulk chemicals
- Y02P 20/52: using catalysts, e.g. selective catalysts
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS

## Abstract

A process for producing aromatic hydrocarbons which comprises (a) contacting ethane with a dehyroaromatization aromatic catalyst which is comprised of about 0.005 to about 0.1 wt % platinum, an amount of gallium which is equal to or greater than the amount of the platinum, from about 10 to about 99.9 wt % of an aluminosilicate, and a binder, and (b) separating methane, hydrogen, and C2-5 hydrocarbons from the reaction products of step (a) to produce aromatic reaction products including benzene.

## Claims

### Claim 1

A process for producing aromatic hydrocarbons which comprises:
(a) contacting ethane with a dehydroaromatization catalyst which comprises:
(1) 0.01 to 0.05 wt % platinum, based on the total weight of the catalyst calculated as metal,
(2) an amount of gallium equal to or greater, by weight, than the amount of the platinum, basis the metal, and no more than about 1 wt %, based on the total weight of the catalyst calculated as metal;
(3) about 10 to about 99.9 wt % of an aluminosilicate, and
(4) a binder;
(b) collecting the products from (a) and separating and recovering C6+ aromatic hydrocarbons,
(c) optionally recovering methane and hydrogen; and
(d) optionally recycling C2-5 hydrocarbons to (a).

### Claim 2 (depends on 1)

The process of claim 1 wherein the reactor comprises a bed of catalyst particles and the ethane flows through the bed.

### Claim 3 (depends on 2)

The process of claim 2 wherein the reactor is selected from fixed bed, moving bed, and fluidized bed reactors.

### Claim 4 (depends on 1)

The process of claim 1 wherein the ethane contact time is from about 0.1 seconds to about 1 minute.

### Claim 5 (depends on 1)

The process of claim 1 wherein the reaction is carried out at from about 550 to about 730° C. and from about 0.01 to about 1.0 MPa.

### Claim 6 (depends on 1)

The process of claim 1 wherein the amount of platinum is from about 0.02 to about 0.05 wt %, based on the total weight of the catalyst calculated as metal.

### Claim 7 (depends on 1)

The process of claim 1 wherein the catalyst comprises no more than about 0.5 wt % of gallium, calculated as metal.

### Claim 8 (depends on 1)

The process of claim 1 wherein the amount of the aluminosilicate is from about 30 to about 99.9 wt % based on the total weight of the catalyst.

### Claim 9 (depends on 1)

The process of claim 1 wherein the aluminosilicate has a silicon dioxide:aluminum trioxide molar ratio of from about 20 to about 80.

### Claim 10 (depends on 1)

The process of claim 1 wherein the aluminosilicate is a zeolite.

### Claim 11 (depends on 10)

The process of claim 10 wherein the zeolite is selected from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-23, and ZSM-35.

### Claim 12 (depends on 10)

The process of claim 10 wherein the zeolite is converted to the H+ form.

### Claim 13 (depends on 1)

The process of claim 1 wherein the binder is selected from silica, alumina and mixtures thereof.

### Claim 14

A process for producing aromatic hydrocarbons which comprises:
(a) contacting ethane with a dehydroaromatization catalyst which comprises:
(1) 0.005 to 0.05 wt % platinum, based on the total weight of the catalyst calculated as metal,
(2) an amount of gallium equal to or greater, by weight, than the amount of the platinum, basis the metal, and no more than about 1 wt %, based on the total weight of the catalyst calculated as metal;
(3) about 10 to about 99.9 wt % of an aluminosilicate, and
(4) a binder;
(b) collecting the products from (a) and separating and recovering C6+aromatic hydrocarbons,
(c) optionally recovering methane and hydrogen; and
(d) optionally recycling C2-5 hydrocarbons to (a).

### Claim 15 (depends on 14)

The process of claim 14 wherein the reactor is selected from fixed bed, moving bed, and fluidized bed reactors.

### Claim 16 (depends on 14)

The process of claim 14 wherein the ethane contact time is from about 0.1 seconds to about 1 minute.

### Claim 17 (depends on 14)

The process of claim 14 wherein the reaction is carried out at from about 550 to about 730° C. and from about 0.01 to about 1.0 MPa.

### Claim 18 (depends on 14)

The process of claim 14 wherein the catalyst comprises no more than about 0.5 wt % of gallium, calculated as metal.

### Claim 19 (depends on 14)

The process of claim 14 wherein the amount of the aluminosilicate is from about 30 to about 99.9 wt % based on the total weight of the catalyst.