Optimized reactor configuration for optimal performance of the aromax catalyst for aromatics synthesis

Patent metadata

Field	Value
Publication number	US-11634648-B2
Application number	US-202217948718-A
Country	US
Kind code	B2
Filing date	Sep 20, 2022
Priority date	Jan 4, 2018
Publication date	Apr 25, 2023
Grant date	Apr 25, 2023

Abstract

A naphtha reforming reactor system comprising a first reactor comprising a first inlet and a first outlet, wherein the first reactor is configured to operate as an adiabatic reactor, and wherein the first reactor comprises a first naphtha reforming catalyst; and a second reactor comprising a second inlet and a second outlet, wherein the second inlet is in fluid communication with the first outlet of the first reactor, wherein the second reactor is configured to operate as an isothermal reactor, and wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, a heat source configured to heat the interior of the reactor furnace; and a second naphtha reforming catalyst disposed within the plurality of tubes, wherein the first naphtha reforming catalyst and the second naphtha reforming catalyst are the same or different.

First claim

We claim:

1. A method comprising:
introducing a hydrocarbon feed stream to a first reactor operating under adiabatic naphtha reforming conditions, wherein the first reactor comprises a radial flow reactor comprises a first naphtha reforming catalyst, and wherein the hydrocarbon feed stream comprises a convertible hydrocarbon;
converting at least a portion of the convertible hydrocarbon in the hydrocarbon feed stream to an aromatic hydrocarbon in the first reactor to form a first reactor effluent;
passing the first reactor effluent from the first reactor to a second reactor operating under isothermal naphtha reforming conditions, wherein the second reactor comprises a plurality of tubes disposed within a reactor furnace, and a second naphtha reforming catalyst disposed within the plurality of tubes, and wherein the plurality of tubes are arranged in parallel between an inlet and an outlet of the reactor furnace;
passing the first reactor effluent through the plurality of tubes within the second reactor;
converting at least an additional portion of the convertible hydrocarbon in the first reactor effluent to an additional amount of the aromatic hydrocarbon in the second reactor to form a second reactor effluent, wherein the plurality of tubes is heated within the reactor furnace during the converting; and
recovering the second reactor effluent from the second reactor.

2. The method of claim 1 , further comprising:
heating the first reactor effluent within the reactor furnace, wherein heating the first reactor effluent within the second reactor occurs during the converting.

3. The method of claim 1 , further comprising:
heating the first reactor effluent in a second furnace prior to passing the first reactor effluent into the second reactor.

4. The method of claim 3 , wherein heating the first reactor effluent comprises heating the first reactor effluent while cooling the second reactor effluent by heat exchange in a feed effluent heat exchanger to produce a feed effluent heat exchanger effluent.

5. The method of claim 1 , wherein the first reactor comprises an adiabatic radial flow reactor comprising a first catalyst bed.

6. The method of claim 1 , wherein an amount of the first naphtha reforming catalyst in the first reactor is less than an amount of the second naphtha reforming catalyst in the second reactor.

7. The method of claim 1 , wherein the hydrocarbon feed stream comprising C 6 to C 8 hydrocarbons containing up to about 15 wt. % of C 5 and lighter hydrocarbons (C 5 − ).

8. The method of claim 7 , wherein the hydrocarbon feed stream further contains up to about 10 wt. % of C 9 and heavier hydrocarbons (C 9 + ).

9. The method of claim 1 , wherein the hydrocarbon feed stream is processed in a preliminary reactor prior to introducing the hydrocarbon feed stream to the first reactor.

10. The method of claim 9 , wherein the preliminary reactor comprises a reactor bed with a sulfur adsorbing material.

11. The method of claim 1 , wherein the second reactor is disposed within a reactor furnace, wherein the reactor furnace comprises a radiant zone and a convection zone, and wherein heating the first reactor effluent comprises heating the first reactor effluent within tubes disposed within the convection zone.

12. The method of claim 1 , wherein the plurality of tubes does not contain a metal protective layer comprising stannide.

Assignees

• Chevron Phillips Chemical Co Lp

Inventors

• Mcgahee Vincent D
• Hasenberg Daniel M

Classifications

• C10G59/02

  plural serial stages only · CPC title

• C10G2300/1044

  Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C · CPC title

• C10G35/04 Primary

  Catalytic reforming · CPC title

• C10G59/00

  Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha · CPC title

• C10G59/06

  plural parallel stages only · CPC title