PROCESS FOR CO-GASIFICATION OF TWO OR MORE CARBONACEOUS FEEDSTOCKS AND APPARATUS THEREOF

• US 20140090298A1
• Filed: 12/29/2011
• Published: 04/03/2014
• Est. Priority Date: 06/10/2011
• Status: Active Grant

• Current Assignee: Bharat Petroleum Corporation Limited (Government of India)
• Original Assignee: Bharat Petroleum Corporation Limited (Government of India)
• Inventors: Rakshit, Pranab Kumar, Voolapalli, Ravi Kumar, Maity, Pintu
• Granted Patent: US 10,174,265 B2
• Time in Patent Office: Days
• US Class Current: 48/101
• CPC Class Codes: C10J 2300/0913 Carbonaceous raw material
• CPC Class Codes: C10J 2300/0916 Biomass
• CPC Class Codes: C10J 2300/093 Coal
• CPC Class Codes: C10J 2300/0943 Coke
• CPC Class Codes: C10J 2300/0969 Carbon dioxide
• CPC Class Codes: C10J 2300/0976 as steam
• CPC Class Codes: C10J 2300/1215 using synthesis gas as fuel
• CPC Class Codes: C10J 2300/1253 by injecting hot gas
• CPC Class Codes: C10J 3/14 using gaseous heat-carriers
• CPC Class Codes: C10J 3/66 by introducing them into the gasification zone
• CPC Class Codes: C10J 3/721 Multistage gasification, e.g. plural parallel or serial gasification stages
• CPC Class Codes: F23G 2202/00 Combustion
• CPC Class Codes: F23G 2203/501 with external recirculation of entrained bed material
• CPC Class Codes: F23G 2203/503 with two or more fluidised beds
• CPC Class Codes: F23G 2900/50001 Combination of two or more furnaces
• CPC Class Codes: F23G 5/027 pyrolising or gasifying stage pyrolisation of sludge C02F11/00; destructive distillation of carbonaceous materials C10B53/00
• CPC Class Codes: F23G 5/30 having a fluidised bed
• CPC Class Codes: Y02P 20/145 the feedstock being materials of biological origin

Abstract

The present invention relates to a process for co-gasification of two or more carbonaceous feedstock, said process comprising combusting a first carbonaceous feedstock having high calorific value with low ash and high hydrogen content, to produce a heated effluent; carrying the heated effluent to second reactor where the heated effluent reacts with a second carbonaceous feedstock, having low calorific value with high ash and low hydrogen content, to produce synthesis gas. The present invention also relates to an apparatus for co-gasification of two or more carbonaceous feedstock, comprising a first reactor (3), having a first feedstock inlet port (1), a oxygen or air inlet port (2), a steam inlet port (9), a ash removal port (7), and a solid recycle port (6); a first cyclone separator (5) connected to the first reactor (3) through a first cyclone separator inlet port (4); a second reactor (16), having a second feedstock inlet port (10), and a ash removal port (15), the second reactor is connected to the first cyclone separator (5) through a gaseous inlet port (8); and a second cyclone separator (12), having a fine particles removal port (13), and an effluent port (14), wherein the second cyclone separator is connected to the second reactor through a second cyclone separator inlet port (11).

Claims

1. A process for co-gasification of two or more carbonaceous feedstock, said process comprising:

combusting a first carbonaceous feedstock having high calorific value with low ash and high hydrogen content, in presence of steam, with an amount of oxygen to produce a heated effluent;

carrying the heated effluent forward so that the heated effluent reacts with a second carbonaceous feedstock, having low calorific value with high ash and low hydrogen content, to produce synthesis gas.

2. A process for co-gasification of two or more carbonaceous feedstock, as claimed in claim 1, said process comprising:

combusting a first carbonaceous feedstock having high calorific value with low ash and high hydrogen content, in a first reactor selected from a fluid bed reactor or an entrained bed reactor, at a temperature in the range of 800 deg C. to 2000 deg C. and pressure in the range of 1 bar to 100 bar in presence of steam with an amount of oxygen to produce a heated effluent;

carrying the heated effluent to a second reactor; and

gasifying a second carbonaceous feedstock having low calorific value, with high ash and low hydrogen content, in the second reactor wherein the heated effluent reacts with the second carbonaceous feedstock to produce synthesis gas.

3. The process as claimed in claim 1, further comprising:

separating carbon particles from the heated effluent; and

recycling the separated carbon particles to the first reactor.

4. The process as claimed in claim 3, wherein the separation is by means of a cyclone separator.

5. The process as claimed in claim 1, wherein the first carbonaceous feedstock having high calorific value with low ash and high hydrogen content is selected from the group consisting of Petcoke, low ash Coal, Natural gas, Liquefied petroleum gas, synthesis gas, coal and oil emulsions or mixtures thereof.

6. The process as claimed in claim 1, wherein the second carbonaceous feedstock having low calorific value with high ash and low hydrogen content is selected from the group consisting of Indian Coal, high ash coal and Biomass or mixtures thereof.

7. The process as claimed in claim 1, wherein the amount of oxygen used in the combustion of first carbonaceous feedstock having high calorific value with low ash and high hydrogen content, is stoichiometric oxygen or ±

5 to ±

20% by weight than the stoichiometric oxygen.

8. The process as claimed in claim 1, wherein the oxygen is preheated at a temperature in the range of 200 deg C. to 400 deg C.

9. The process as claimed in claim 1, wherein the combustion of first carbonaceous feedstock having high calorific value with low ash and high hydrogen content is carried out at a temperature in the range of 900 deg C. to 1800 deg C.

10. The process as claimed in claim 1, wherein the combustion of first carbonaceous feedstock having high calorific value with low ash and high hydrogen content is carried out at a pressure in the range of 1 bar to 90 bar.

11. The process as claimed in claim 1, wherein the heated effluent comprises heat, super heated steam and hot gases.

12. The process as claimed in claim 2, wherein the second reactor is selected from a moving bed reactor or a fluid bed reactor.

13. The process as claimed in claim 12, wherein the heated effluent is introduced radially into the moving bed reactor.

14. The process as claimed in claim 12, wherein the moving bed reactor is selected from up-draft moving bed reactor, or down-draft moving bed reactor.

15. A process for gasification of carbonaceous feedstock, said process comprising:

combusting petcoke in a fluid bed reactor at a temperature in the range of 800 deg C. to 1700 deg C. and pressure in the range of 1 bar to 100 bar, in presence of steam with an amount of oxygen, thereby producing a heated effluent;

separating carbon particles from the heated effluent;

sending the separated carbon particles to the fluid bed reactor;

carrying the heated effluent to a moving bed reactor; and

gasifying Indian coal in the moving bed reactor wherein the heated effluent reacts with the Indian coal to produce synthesis gas.

16. An apparatus for co-gasification of two or more carbonaceous feedstock, said apparatus comprising:

a first reactor, having a first feedstock inlet port, an oxygen or air inlet port, a steam inlet port, an ash removal port, and a solid recycle port;

a first cyclone separator-connected to the first reactor through a first cyclone separator inlet port;

a second reactor, having a second feedstock inlet port, and an ash removal port, wherein the second reactor is connected to the first cyclone separator through a gaseous inlet port; and

a second cyclone separator, having a fine particles removal port, and an effluent port, wherein the second cyclone separator is connected to the second reactor through a second cyclone separator inlet port.

17. The apparatus as claimed in claim 16, wherein the first reactor is selected from a fluid bed reactor or an entrained bed reactor.

18. The apparatus as claimed in claim 16, wherein the first reactor is a fluid bed reactor.

19. The apparatus as claimed in claim 16, wherein the second reactor is selected from a moving bed reactor or a fluid bed reactor.

20. The apparatus as claimed in claim 19, wherein the second reactor is selected from a group consisting of up-draft moving bed reactor, and down-draft moving bed reactor.

21. The apparatus as claimed in claim 19, wherein the second reactor is a moving bed reactor in which the heated effluent is introduced radially.

22. The apparatus as claimed in claim 21, wherein the moving bed reactor comprises:

a feed stock inlet port;

a distributor;

an effluent port; and

an ash removal port.

23. The apparatus as claimed in claim 22, wherein the moving bed reactor is connected to the first reactor through an inlet port.