Reactor apparatus for non-oxidative hydrocarbon conversion to aromatics, methods of using same, and products made using same

Patent metadata

Field	Value
Publication number	US-10836965-B2
Application number	US-201916382755-A
Country	US
Kind code	B2
Filing date	Apr 12, 2019
Priority date	Apr 24, 2018
Publication date	Nov 17, 2020
Grant date	Nov 17, 2020

Abstract

Methods of transforming a hydrocarbon feedstream into an aromatization product in a multi-stage reverse flow reactor (RFR) apparatus are disclosed. The methods include at least two reaction stages in series, at least one being a pyrolysis stage and at least another being a catalytic aromatization stage. Using a highly saturated hydrocarbon feedstream the pyrolysis stage focuses on desaturation, while the catalytic aromatization stage focuses on aromatization. The catalytic aromatization stage contains a aromatization catalyst that can include substantially no magnesium, scandium, yttrium, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, rhenium, iron, ruthenium, cobalt, rhodium, nickel, palladium, platinum, copper, silver, gold, gallium, indium, tin, lanthanides, or actinides, or, in some cases, substantially no added active metals at all. The aromatization product can contain at least 35 mol % aromatic hydrocarbons, based on a total amount of hydrogen and hydrocarbons in the aromatized hydrocarbon product.

First claim

What is claimed is:

1. A hydrocarbon conversion process, comprising:
(a) providing a hydrocarbon feed comprising C 2+ hydrocarbon;
(b) providing an oxidant and a gaseous fuel;
(c) providing tubular flow-through reactor, wherein the tubular flow-through reactor includes
(i) a pre-heated pyrolysis stage and a catalytic aromatization stage, and
(ii) at least one aromatization catalyst located in the catalyst aromatization stage,
(iii) a mixing-distribution stage located between the pyrolysis stage and the aromatization stage,
(iv) a pre-heated first heat transfer stage adjacent to the pyrolysis stage and opposite the mixing-distribution stage, and
(v) a pre-cooled second heat transfer stage adjacent to the catalytic aromatization stage and opposite the mixing distribution stage;

(d) during a second time interval
(i) establishing a forward flow of the hydrocarbon feed to the pyrolysis stage,
(ii) transferring heat from the pyrolysis stage to the hydrocarbon feed to pyrolyse under pyrolysis conditions at least a portion of the hydrocarbon feed's C 2+ hydrocarbon to produce a pyrolysis product comprising (A) C 2+ unsaturated hydrocarbon produced the pyrolysis and (B) unreacted hydrocarbon feed,
(iia) flowing the pyrolysis product to the catalytic aromatization stage;
(iii) aromatizing at least a portion of the C 2+ unsaturated hydrocarbon under aromatization conditions in the presence of the aromatization catalyst in the catalytic aromatization stage to produce an aromatization product comprising benzene,
(iv) depositing coke on or proximate to the aromatization catalyst,
(v) conducting the forward flow of aromatization product from the catalytic aromatization stage and away from the reverse-flow reactor, and
(vi) decreasing the flow of the hydrocarbon feed to the pyrolysis stage; and

(e) during a second time interval,
(i) establishing a reverse flow of the fuel and a reverse flow of the oxidant toward the tubular flow-through reactor, the oxidant flow comprising first and second portions of the oxidant,
(ii) combusting within the catalytic aromatization stage a first portion of the oxidant flow with at least a portion of the deposited coke to produce a reverse flow of a first combustion product,
(iii) combusting in the tubular flow-through reactor a second portion of the oxidant flow with at least a portion of the fuel flow to produce a reverse flow of a second combustion product in the tubular flow-through reactor,
(iv) conducting the reverse flows of the first and second combustion products away from the tubular flow-through reactor, wherein heat is transferred from the first and second combustion products to the tubular flow-through reactor to re-heat at least the pyrolysis stage, and
(v) decreasing the reverse flows of fuel and oxidant.

2. The method of claim 1 , wherein the hydrocarbon feed comprises less than 5 mol % C 1 hydrocarbons and at least 50 mol % C 2 hydrocarbons, based on a total amount of hydrocarbons in the hydrocarbon feedstream.

3. The method of claim 1 , wherein at least one of (i) the hydrocarbon feed, (ii) the oxidant, and (iii) the fuel comprises ≤10% of water, on a molar basis.

4. The method of claim 1 , wherein the aromatization catalyst comprises a porous zeolite containing a 10-ring, an 11-ring, or a 12-ring pore opening.

5. The method of claim 1 , wherein the aromatization catalyst comprises one or more of ZSM-5, ZSM-11, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-50, ZSM-57, MCM-68, MCM-22, PSH-3, SSZ-25, ERB-1, ITQ-1, ITQ-2, MCM-36, MCM-56, and UZM-8.

6. The method of claim 1 , wherein the aromatization catalyst comprises substantially no magnesium, scandium, yttrium, titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, rhenium, iron, ruthenium, cobalt, rhodium, nickel, palladium, platinum, copper, silver, gold, gallium, indium, tin, lanthanides, or actinides deposited on or in pores of the aromatization catalyst.

7. The method of claim 1 , wherein the aromatization catalyst is a dehydrocyclization catalyst which comprises substantially no added active metals.

8. The method of claim 1 , wherein the aromatization catalyst comprises from about 0.05 wt. % to about 3 wt. % zinc, based on a total weight of the aromatization catalyst.

9. The method of claim 1 , wherein the pyrolysis conditions include (i) a temperature in the range of from 700° C. to 1100° C. and (ii) a pressure in the range of 7 psig to 150 psig.

10. The method of claim 1 , wherein the pyrolysis product comprises at least 45 mol % ethylene, based on a total amount of hydrogen and hydrocarbons in the thermal pyrolysis product.

11. The method of claim 1 , wherein the aromatization includes converting to aromatic hydrocarbon at least 70% of the pyrolysis product's C 2+ unsaturated hydrocarbon, and wherein the aromatization product further comprises one or more of toluene, o-xylene, m-xylene, p-xylene, ethylbenzene, styrene, a-methylstyrene, mesitylene, 1,2,3-trimethylbenzene, 1,2,4-trimethylbenzene, cumene, naphthalene, and methylnaphthalene.

12. The method of claim 1 , wherein the aromatization includes converting to aromatic hydrocarbon at least a portion of any C 1 -C 10 saturated hydrocarbon in the pyrolysis product.

13. The method of claim 1 , further comprising carrying out a purge mode after step (d) and before step (e).

14. The method of claim 1 , further comprising repeating steps (d) and (e).

15. The method of claim 1 , wherein the first interval is in the range of from 0.05 second to 120 seconds, and the ratio of the first interval to the second interval is in the range of from 1:10 to 50:1.

16. The method of claim 1 , wherein the tubular flow-through reactor is a reverse-flow reactor.

17. The method of claim 16 , wherein the reverse-flow reactor is a regenerative thermal reverse-flow reactor (“RTRFR”).

18. The method of claim 1 , further comprising (i) during the first time interval transferring heat from the first heat transfer stage to the hydrocarbon feed and transferring heat from the aromatization product to the second heat transfer stage and (ii) during the second time interval, (A) transferring heat from the second heat transfer stage to the first portion of the oxidant and/or the second portion of the oxidant, (B) transferring heat from at least the second combustion product to the first heat transfer stage, and (C) combusting >90 wt. % of the fuel flow downstream of the catalytic aromatization stage.

19. The method of claim 18 , wherein the aromatization conditions include a temperature ≤750° C.; a pressure ≥10 psia (68.9 kPa absolute); and a space velocity (GHSV) ≥500 hr −1 .

20. The method of claim 18 , wherein during the second time interval at least a portion of any heat generated by the combustion of deposited coke is transferred to the catalytic aromatization stage, and during the first time interval transferring to the aromatization reaction at least a portion of the heat transferred to the catalytic aromatization stage during the second time interval.

21. The method of claim 1 , further comprising separating from the aromatization product one or more of ethylene, acetylene, propylene, 1,3-butadiene, benzene, toluene, o-xylene, p-xylene, and naphthalene.

22. The method of claim 1 , further comprising separating from the aromatization product and recycling to step (d) one or more of methane, ethane, propane, butanes, and hexanes.

23. The method of clai

Assignees

• Exxonmobil Chemical Patents Inc

Inventors

• Shekhar Mayank
• Lattner James R
• Barrai Federico
• Weiss Brian M
• Bhandari Dhaval A
• Allen Joshua W

Classifications

• B01F23/19

  Mixing systems, i.e. flow charts or diagrams; Arrangements, e.g. comprising controlling means · CPC title

• B01J8/067

  Heating or cooling the reactor (B01J8/062 takes precedence) · CPC title

• C10G35/24

  Controlling or regulating of reforming operations · CPC title

• C10G2400/30

  Aromatics · CPC title

• B01J2208/0053

  Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling · CPC title