Inherently safe ODH operation

Patent metadata

Field	Value
Publication number	US-9630893-B2
Application number	US-201615370572-A
Country	US
Kind code	B2
Filing date	Dec 6, 2016
Priority date	Nov 21, 2013
Publication date	Apr 25, 2017
Grant date	Apr 25, 2017

Abstract

In the operation of an oxidative dehydrogenation (ODH) process, it is desirable to remove oxygen in the product stream for a number of reasons, including to reduce oxidation of the product. This may be achieved by having several pre-reactors upstream of the main reactor having a catalyst system containing labile oxygen. The feed passes through one or more reactors saturated with labile oxygen. When the labile oxygen is consumed through a valve system, the pre-reactor accepts product from the main reactor and complexes reactive oxygen in the product stream until the catalyst system is saturated with labile oxygen. Then the reactor becomes a pre-reactor and another pre-reactor becomes a scavenger.

First claim

What is claimed is:

1. A process for the catalytic oxidative dehydrogenation of one or more C 2-4 alkanes comprising at least three pre-reactors and one or more downstream main oxidative dehydrogenation reactors comprising:
i) passing a feed stream comprising said one or more C 2-4 alkanes through a first pre-reactor containing a dehydration catalyst that is saturated with reactive oxygen;
ii) reacting the feed stream with the dehydration catalyst that is saturated with reactive oxygen at a temperature from about 300° C. to about 500° C. and a pressure from about 0.5 to about 100 psig to produce a partially dehydrogenated stream comprising unreacted C 2-4 alkanes;
iii) passing the partially dehydrogenated stream together with additional oxygen feed to one or more downstream main oxidative dehydrogenation reactors;
iv) oxidatively dehydrogenating the partially dehydrogenated stream at a temperature from about 300° C. to about 500° C. and a pressure from about 0.5 to about 100 psig to produce a product stream;
v) removing the product stream from said one or more downstream main oxidative dehydrogenation reactors comprising corresponding C 2-4 alkenes, unreacted C 2-4 alkanes, unreacted oxygen and water vapor;
vi) passing the product stream through a series of two or more pre-reactor comprising a lead and a guard dehydrogenation reactor having secondary dehydrogenation catalyst that are depleted of reactive oxygen the lead dehydrogenation reactor having a secondary dehydrogenation catalyst that is less depleted of reactive oxygen than the dehydrogenation catalyst in the guard dehydrogenation reactor;
vii) reacting the product stream with the dehydrogenation catalyst of the lead dehydrogenation reactor depleted of reactive oxygen at a temperature from about 50° C. to about 270° C. and a pressure from about 0.5 to about 100 psig to complex the oxygen depleting oxygen from the product stream and regenerating oxidative dehydrogenation catalyst by increasing the saturation with reactive oxygen; and
viii) reacting the product stream from the lead dehydrogenation reactor with the reactive oxygen depleted catalyst of the guard oxygen dehydrogenation reactor at a temperature from about 50° C. to about 270° C. and a pressure from about 0.5 to about 100 psig to complex the oxygen depleting oxygen from the product stream and partially regenerating oxidative dehydrogenation catalyst by increasing the saturation with reactive oxygen; and
ix) recovering a product stream depleted of oxygen;
recovering a product stream depleted of oxygen;
x) continuing step (i) to (ix) until either:
a) the pre-reactor comprising the first dehydrogenation catalyst and through which the feed stream is being passed is depleted of reactive oxygen or is more depleted or reactive oxygen than another pre-reactor; or
b) the pre-reactor comprising the second oxidative dehydrogenation catalyst through which the product stream is being passed is substantially saturated with reactive oxygen;

xi) when condition (a) is achieved the feed stream is diverted from the first pre-reactor to lead dehydrogenation reactor that is more saturated with reactive oxygen the product stream from the main dehydrogenation reactors is diverted to the guard dehydrogenation reactor and the product stream from the guard dehydrogenation reactor is diverted to the primary dehydrogenation reactor in which the dehydrogenation catalyst is depleted of reactive oxygen and the process continues from step (i) on.

2. The process according to claim 1 , wherein the oxidative dehydrogenation catalyst in any reactor is independently selected from:
i) catalysts of the formula
V x Mo y Nb z Te m Me n O p

wherein Me is a metal selected from Ta, Ti, W, Hf, Zr, Sb and mixtures thereof; and
x is from about 0.1 to about 3 provided that when Me is absent x is greater than 0.5;
y is from about 0.5 to about 1.5;
z is from about 0.001 to about 3;
m is from about 0.001 to about 5;
n is from 0 to about 2; and
p is a number to satisfy the valence state of the mixed oxide catalyst; and
ii) catalysts of the formula
Mo a V b Nb c Te e O d

wherein:
a is from about 0.75 to about 1.25;
b is from about 0.1 to about 0.5;
c is from about 0.1 to about 0.5;
e is from about 0.1 to about 0.3; and
d is a number to satisfy the valence state of the mixed oxide catalyst.

3. The process according to claim 2 , wherein said one or more downstream main oxidative dehydrogenation reactors are operated at a gas hourly space velocity (GHSV) from about 500 to about 30000 h −1 .

4. The process according to claim 3 , wherein the catalyst in the main reactor is supported on an inert metal oxide support having a surface area of less than about 5 m 2 /g.

5. The process according to claim 4 , wherein the pre-reactors are fixed bed reactors and the oxidative dehydrogenation catalyst is supported on an inert metal oxide support having a surface area of not less than about 100 m 2 /g.

6. The process according to claim 5 , wherein said one or more downstream main oxidative dehydrogenation reactors are selected from fixed bed reactors, fluidized or ebullated bed reactors, and ceramic membrane reactors.

7. The process according to claim 6 , having a selectivity for said one or more C 2-4 alkenes of greater than about 85%.

8. The process according to claim 7 , wherein said one or more C 2-4 alkanes is ethane.

9. The process according to claim 8 , wherein the catalyst in said pre-reactors is of formula (ii) and wherein:
a is from about 0.90 to about 1.10;
b is from about 0.25 to about 0.3;
c is from about 0.1 to about 0.3;
e is from about 0.1 to about 0.2; and
d is a number to satisfy the valence state of the mixed oxide catalyst.

10. The process according to claim 1 , wherein in step (vi) the product stream from said downstream main oxidative dehydrogenation reactors is passed sequentially through two or more pre-reactors in which the first of these sequential pre-reactors has a higher amount of reactive oxygen in the oxidative dehydrogenation catalyst than in the subsequent pre-reactors.

11. The process according to claim 1 , further comprising a third pre-reactor comprising an oxidative dehydrogenation catalyst that can accept the feed stream when enriched with oxygen or accept the product stream when substantially depleted of oxygen.

Assignees

• Nova Chemicals International Sa

Inventors

• Simanzhenkov Vasily
• Gao Xiaoliang
• Foy Edward Christopher
• Kustov Leonid Modestovich
• Kucherov Aleksey Victorovich
• Finashina Elena Dmitrievna

Classifications

• B01J2208/00716

  Means for reactor start-up · CPC title

• B01J19/242

  in series · CPC title

• B01J2208/00628

  Controlling the composition of the reactive mixture · CPC title

• B01J2208/00637

  Means for stopping or slowing down the reaction · CPC title

• B01J19/2475

  Membrane reactors · CPC title