Integrated fluid catalytic cracking and oxidative propane dehydrogenation process

Patent metadata

Field	Value
Publication number	US-10654773-B2
Application number	US-201816175630-A
Country	US
Kind code	B2
Filing date	Oct 30, 2018
Priority date	Dec 21, 2017
Publication date	May 19, 2020
Grant date	May 19, 2020

Abstract

The present invention is related to an integrated process for enhancing the yields of propylene and other light olefins from Fluid catalytic cracking (FCC) process in combination with Oxidative propane dehydrogenation (OPDH) where in a hydrocarbon stream from Propylene recovery section consisting of propane predominantly, is converted to high value light olefins primarily C 3 and C 2 olefins by catalytic oxidative dehydrogenation using carbon dioxide from FCC flue gas exiting the regenerator. Several process configurations for the conversion of C 3 and C 4 alkanes to their respective alkenes separately or simultaneously by integrating with FCC are provided.

First claim

The invention claimed is:

1. An integrated process for catalytic conversion of alkanes to alkenes, wherein an alkane feed stream from recovery section of fluidized catalytic cracking (FCC) process is converted to respective olefins by catalytic oxidative dehydrogenation (ODH),
wherein dehydrogenation of different alkanes occurs simultaneously in separated ODH reactors connected in series or in same ODH reactor with continuous catalyst regeneration; and
wherein oxygen from flue gas exiting from a regenerator of the FCC process is removed in an oxygen separation unit to obtain an oxygen-free flue gas; and
wherein the oxygen-free flue gas is mixed with the alkane feed stream prior to feeding to ODH reactor.

2. The process as claimed in claim 1 , wherein the process comprises:
a) feeding cracked hydrocarbon products from FCC riser-reactor to a main fractionator column to obtain a product stream comprising of dry gas, LPG, and light naphtha,
b) separating the product stream in a gascon section, into LPG comprising of C 3 and C 4 hydrocarbons, and dry gas comprising of hydrogen, methane, ethane, ethylene, and other non-condensable gases,
c) routing the LPG stream to propylene recovery unit (PRU) to separate and obtain propane, wherein the propane is used as feed stream for ODH process,
d) subjecting the flue gas from FCC regenerator to oxygen (O 2 ) separation to obtain the oxygen-free flue gas,
e) premixing the propane feed stream obtained from step (c) oxygen-free flue gas from step (d) and utilizing the mixture as feed mixture for ODH process to obtain propylene, unreacted propane, ethylene, and other gases, and
f) re-routing the products from step (e) to the gascon section after separation of water.

3. The process as claimed in claim 1 , wherein the process comprises:
a) feeding cracked hydrocarbon products from FCC riser-reactor to a main fractionator column to obtain a product stream comprising of dry gas, LPG, and light naphtha,
b) separating the product stream in a gascon section, into LPG comprising of C 3 and C 4 hydrocarbons, and dry gas comprising hydrogen, methane, ethane, ethylene, and other non-condensable gases,
c) routing the dry gas to ethylene recovery section to separate and obtain ethane, wherein the ethane is used as a feed stream for ODH process,
d) subjecting the flue gas from FCC regenerator to oxygen (O 2 ) separation to obtain the oxygen-free flue gas,
e) premixing the ethane feed stream obtained from step (c) and the oxygen-free flue gas from step (d) and utilizing the mixture as feed mixture for ODH process to obtain ethylene, unreacted ethane, and other gases, and
f) re-routing the products from step (e) to the gascon section after separation of water.

4. The process as claimed in claim 1 , wherein the process comprises:
a) feeding cracked hydrocarbon products from FCC riser-reactor to a main fractionator column to obtain a product stream comprising of dry gas, LPG, and light naphtha,
b) separating the product stream in a gascon section, into LPG comprising of C 3 and C 4 hydrocarbons, and dry gas comprising hydrogen, methane, ethane, ethylene, and other non-condensable gases,
c) routing the LPG stream to propylene recovery unit (PRU) to separate and obtain C 4 hydrocarbon stream from debutanizer section,
d) routing the C 4 hydrocarbon stream to the C 4 -separation section to separate and obtain C 4 alkanes comprising iso-butane and n-butane, wherein the iso-butane or n-butane or their mixture is used as feed stream for the ODH process,
e) subjecting the flue gas from FCC regenerator to oxygen (O 2 ) separation to obtain the oxygen-free flue gas,
f) premixing the C 4 feed stream obtained from step (d) and the oxygen-free flue gas from step (e) and utilizing the mixture as feed mixture for ODH process to obtain butylenes, unreacted butane(s), C 2 , C 3 , and other hydrocarbons,
g) re-routing the products from step (f) to the gascon section after separation of water.

5. The process as claimed in claim 1 , wherein the FCC process is fluid catalytic cracking or Resid fluid catalytic cracking or High severity fluid catalytic cracking or High severity propylene maximizing fluid catalytic cracking process.

6. The process as claimed in claim 1 , wherein the ODH reactor is selected from a fixed bed or fluidized bed or moving bed or combination thereof.

7. The process as claimed in claim 1 , wherein the alkane for dehydrogenation in the ODH process is selected from ethane, propane, and C 4 alkanes or any combination thereof.

8. The process as claimed in claim 1 , wherein the dehydrogenation of ethane, propane and C 4 alkanes is carried out in the ODH process, wherein the C 2 , C 3 and C 4 alkanes are separately introduced at different zones of a fluidized bed riser type of reactor, with continuous catalyst regeneration.

9. The process as claimed in claim 8 , wherein the process comprises:
a) sending the flue gas from the FCC regenerator to O 2 separation to obtain the oxygen-free flue gas,
b) mixing the oxygen-free flue gas with ethane from ethylene recovery section and sending to feed mixture to the fluidized bed riser type of reactor;
c) mixing the oxygen-free flue gas with the propane from PRU and sending feed mixture to the fluidized bed riser type of reactor;
d) mixing the oxygen-free flue gas with C 4 alkanes from C 4 -separation section and sending the feed mixture to the fluidized bed riser type of reactor;
e) introducing the feed mixtures from step (b), (c), and (d) separately at different zones of the fluidized bed riser type of reactor to produce ethylene, propylene, and butylene;
f) continuous circulation of catalyst from the reactor to catalyst regeneration unit;
g) re-circulating the hot catalyst to the reactor;
h) re-routing the products from step (e) to the gascon section after separation of water.

10. The process as claimed in claim 1 , wherein the dehydrogenation of ethane, propane and iso-butane or n-butane occur simultaneously in separate reactors in series on a suitable catalyst which circulates from the former reactor to the latter with subsequent continuous catalyst regeneration.

11. The process as claimed in claim 10 , wherein the process comprises:
a) sending the flue gas from the FCC regenerator to O 2 separation to obtain the oxygen-free flue gas,
b) mixing the oxygen-free flue gas with the ethane from ethylene recovery section and sending the resultant feed mixture to a C 2 alkane dehydrogenation reactor to produce ethylene, wherein the feed mixture is pre-heated by C 2 alkane dehydrogenation reactor effluent stream,
c) mixing the oxygen-free flue gas with the C 3 alkane product from PRU and sending the resultant feed mixture to a propane dehydrogenation (PDH) reactor to produce propylene, wherein the feed mixture is pre-heated by PDH reactor effluent stream, and
d) mixing the oxygen-free flue gas with C 4 alkanes from C 4 -separation section and sending the resultant feed mixture to a butane dehydrogenation (BDH) reactor to produce butylenes, wherein the feed mixture is pre-heated by BDH reactor effluent stream,
e) continuous circulation of catalyst from C 2 alkane dehydrogenation reactor to PDH reactor and then PDH reactor to BDH reactor and then to catalyst regeneration unit;
f) re-circulating the hot catalyst to C 2 alkane dehydrogenation reactor;
g) re-routing the products from steps (b), (c) and (d) to the gascon section after separation of water.

12. The process as claimed in claim 2 , wherein the feed mixtures comprise of at least one of ethane/oxygen-free flue gas, propane/oxygen-free flue gas, iso-butane/oxygen-free flue gas, and n-butane/oxygen-free flue

Assignees

• Indian Oil Corp Ltd

Inventors

• Doosa Hima Bindu
• Thakur Ram Mohan
• Nath Vineeth Venu
• Gupta Kamlesh
• Bhattacharyya Debasis
• Mazumdar Sanjiv Kumar
• RAMAKUMAR Sankara Sri Venkata

Classifications

• C07C7/005

  Processes comprising at least two steps in series · CPC title

• C07C7/09

  by fractional condensation · CPC title

• C07C5/42 Primary

  by dehydrogenation with a hydrogen acceptor · CPC title

• C07C5/48 Primary

  with oxygen as an acceptor · CPC title

• C07C9/08

  Propane · CPC title