Process and a system for enhancing liquid yield of heavy hydrocarbon feedstock

Patent metadata

Field	Value
Publication number	US-2016281002-A1
Application number	US-201415036051-A
Country	US
Kind code	A1
Filing date	Jan 6, 2014
Priority date	Nov 18, 2013
Publication date	Sep 29, 2016
Grant date	—

Abstract

The present invention provides a process and a system for coking and simultaneous upgrading of a heavy hydrocarbon feedstock. More particularly the present invention relates to a process of cracking heavy hydrocarbon feedstock employing high heat carrier, incorporated with weak acid sites for improving the liquid yield and reducing coke yield. The feedstock is vaporized and brought in contact with a heat carrier material to produce a product stream and separating the product stream from the particulate heat carrier, regeneration of the particulate heat carrier to the extent of 10-30% and collecting a gaseous and liquid product from the product stream.

First claim

1 . A process for coking and simultaneous upgrading of a heavy hydrocarbon feedstock, comprising:
a. providing a heated particulate material to a reactor chamber; b. dispensing preheated heavy hydrocarbon feedstock in the reactor chamber such that the same conies in contact with the particulate material at a temperature in the range of 480° C. to 620° C. c. allowing said heavy hydrocarbon feedstock to stay in contact with the particulate material for a predetermined time period to form a product mixture and a coke laden particulate material; and d. withdrawing the product mixture from the reactor chamber; characterized in that:
the preheated heavy hydrocarbon feedstock is dispensed as an atomized spray in the reactor chamber;
the predetermined time period is such that the product comprises about 70 wt % to about 80 wt % of hydrocarbons having boiling point in the range of about 40 to 600° C.

2 . The process as claimed in claim 1 , wherein the particulate material has specific area in the range of 100 to 200 m 2 /gm; Heat capacity in the range of 0.9 to 1.0 KJ/Kg ° C.; acidity of more than mass equivalent per gram and apparent bulk density of 0.7 to 1.0 gm/cc.

3 . The process as claimed in claim 1 , wherein the particulate material comprises a modified clay component, a binder component and optionally a diluent material, wherein the binder has less than 0.1 wt % of soda.

4 . The process as claimed in claim 3 , Wherein the modified clay is selected from modified kaolinite, modified bentonite, modified illite, modified vermiculite, modified smectite, modified montmorillonite, modified sepiolite, modified hectorite and mixtures thereof.

5 . The process as claimed in claim 3 , wherein the binder is selected from the group comprising of alumina and the alumina is selected from alumina gel, psedobohemite, aluminium trihydrate, eta, theta and gamma.

6 . The process as claimed in claim 3 , wherein the diluent material is selected from non-modified clay, silica and aluminium trihydrate.

7 . The process as claimed in claim 1 , wherein the predetermined time period is in excess of about 60 seconds.

8 . The process as claimed in claim 1 , wherein the predetermined time period is maintained in the range of about 60 to about 900 seconds.

9 . The process as claimed in claim 1 , wherein the predetermined time period is maintained in the range of about 60 to about 600 seconds.

10 . The process as claimed in claim 1 , wherein the predetermined time period is maintained in the range of about 60 to about 300 seconds.

11 . The process as claimed in claim 1 , wherein a temperature during the predetermined period is maintained in the range of about 480° C. to 590° C.

12 . The process as claimed in claim 1 , wherein an amount of preheated heavy hydrocarbon feedstock provided to the reactor chamber is such that a loading ratio of said heated particulate material to said preheated heavy hydrocarbon feedstock is in the range of 4:1 to 20:1.

13 . The process as claimed in claim 1 , wherein the heavy hydrocarbon feedstock has a CCR content in excess of about 20 wt %.

14 . The process as claimed in claim 1 , wherein the heavy hydrocarbon feedstock is selected from the group comprising of heavy oil, bitumen or mixtures thereof.

15 . The process as claimed in claim 1 , further comprising separating the product mixture to obtain a light fraction and a heavy fraction and optionally recirculating at least a part of the heavy fraction to the reactor chamber.

16 . The process as claimed in claim 15 , wherein the step of separating the product mixture to obtain a light fraction and a heavy fraction is performed in a condenser.

17 . The process as claimed in claim 1 , further comprising regenerating at least a part of the coke laden particulate material and recirculating the regenerated particulate material to the reactor chamber.

18 . The process as claimed in claim 1 , further comprising controlling a velocity of the coke laden particulate material and/or controlling a velocity of regenerated particulate material.

19 . The process as claimed in claim 18 , wherein the velocity of the coke laden particulate material is reduced using a first cyclone device and the velocity of the regenerated particulate material is reduced using a second cyclone device.

20 . The process as claimed in claim 19 , wherein the first and the second cyclone device are the same.

21 . The process as claimed in claim 17 , wherein 10 to 30 wt % of the coke laden particulate material is regenerated and recirculated to the reactor chamber.

22 . The process as claimed in claim 1 , wherein the reactor chamber is in the form of an upflow reactor.

23 . The process as claimed in claim 1 , wherein the step of providing a particulate material to the reactor chamber comprises maintaining the particulate material in form of a fluidized bed in the reactor chamber.

24 . The process as claimed in claim 23 , wherein maintaining the particulate material in form of a fluidized bed in the reactor chamber comprises feeding a fluidizing medium via at least one inlet located at a first elevation of the reactor chamber and feeding the particulate material via at least one inlet located at a second elevation of the reactor chamber.

25 . The process as claimed in claim 1 , Wherein the step of dispensing preheated heavy hydrocarbon feedstock in the reactor chamber comprises dispensing the heavy hydrocarbon feedstock as an atomized spray from at least a top end of the reactor chamber.

26 . The process as claimed in claim 1 , wherein the step of dispensing preheated heavy hydrocarbon feedstock in the reactor chamber comprises dispensing the heavy hydrocarbon feedstock as an atomized spray from a plurality of elevations within the reactor chamber.

27 . The process as claimed in claim 1 , wherein the step of allowing said heavy hydrocarbon feedstock to contact with the particulate material to form a product mixture and a coke laden particulate material comprises maintaining the heavy hydrocarbon feedstock and the particulate material in a conversion zone of the reactor chamber.

28 . A system for coking and simultaneous upgrading of a heavy hydrocarbon feedstock, comprising:
a reactor defining a chamber; a particulate material supply means for supplying heated particulate material to the reactor chamber; a hydrocarbon feedstock supply means for dispensing pre-heated heavy hydrocarbon feed stock to the reactor chamber such that the same comes in contact with the particulate material; a product withdrawal means for withdrawing the product thus formed in the reactor chamber, characterized in that: the hydrocarbon feed stock supply means dispenses the preheated heavy hydrocarbon feed stock as an atomized spray in the reactor chamber; and the reactor chamber allows the heated heavy hydrocarbon feedstock to stay in contact with the particulate material for a predetermined amount of time period such that the product comprises about 70 wt % to about 80 wt % of hydrocarbon having boiling point in the range of 40 to 600° C.

29 . The system as claimed in claim 28 , further comprising a velocity controlling means for controlling a velocity of the coke laden particulate material and/or controlling a velocity of the regenerated particulate material.

30 . The system as claimed

Assignees

• Indian Oil Corp Ltd

Inventors

• Kasliwal Pankaj Kumar
• Prabhu Kuvettu Mohan
• Karthikeyani Arumugam Velayutham
• Hariprasadgupta Bandaru Venkata
• Swamy Balaiah
• Sarkar Biswanath
• Kumar Brijesh
• Rajagopal Santanam
• Malhotra Ravinder Kumar

Classifications

• C10G9/26

  with discontinuously preheated non-moving solid material, e.g. blast and run · CPC title

• C10G9/005 Primary

  Coking (in order to produce liquid products mainly) · CPC title

• C10G9/32

  according to the "fluidised-bed" technique · CPC title