Desulfurization in a regenerative calcium cycle system
View Patent ↗A method for combustion of a fuel and treatment of the resulting flue gas includes: combusting a fuel to produce a hot flue gas stream containing at least carbon dioxide (CO 2 ) and sulfur dioxide (SO 2 ), bringing the flue gas stream into contact with solid calcium oxide (CaO) in a carbonation reactor operating at a temperature at which CO 2 in the flue gas reacts with CaO to form solid calcium carbonate (CaCO 3 ), heating CaCO 3 in a calcination reactor operating at a temperature at which CaCO 3 is converted to CaO and CO 2 , and recirculating CaO formed in the calcination reactor back to the carbonation reactor. Heating can be at least partially effected by indirect heat exchange with hot flue gas from the combustion. Flue gas used for the indirect heat exchange can be subsequently subjected to dry desulfurization before it is brought into contact with CaO in the carbonation reactor.
1. A method for combustion of a fuel and treatment of the resulting flue gas, said method comprising:
combusting a fuel with air or oxygen to produce a hot flue gas stream containing at least carbon dioxide (CO 2 ) and sulfur dioxide (SO 2 ),
bringing the flue gas stream into contact with solid calcium oxide (CaO) in a carbonation reactor operating at a temperature at which CO 2 in the flue gas reacts with CaO to form solid calcium carbonate (CaCO 3 ),
heating CaCO 3 formed in the carbonation reactor in a calcination reactor operating at a temperature at which CaCO 3 is converted to CaO and CO 2 , whereby said heating is at least partially effected by indirect heat exchange with the hot flue gas stream from the combustion, and
recirculating CaO formed in the calcination reactor back to the carbonation reactor,
wherein the flue gas used for indirect heat exchange in the calcination reactor is subsequently subjected to dry desulfurization before it is brought into contact with CaO in the carbonation reactor.
2. The method according to claim 1 , wherein the desulfurization is performed at a temperature in the range of 200° C. to 700° C.
3. The method according to claim 2 , wherein the desulfurization is performed at a temperature in the range of 200° C. to 400° C.
4. The method according to claim 2 , wherein the desulfurization is performed at a temperature in the range of 500° C. to 700° C.
5. The method according to claim 1 , wherein the desulfurization comprises bringing the flue gas into contact with solid calcium oxide (CaO) at a temperature whereby SO 2 in the flue gas reacts with CaO to form solid calcium sulfate (CaSO 4 ).
6. The method according to claim 1 , further comprising the step of removing dust from the desulfurized flue gas before it is brought into contact with CaO in the carbonation reactor.
7. The method according to claim 5 , wherein the CaO used for desulfurization of the flue gas at least partially comprises CaO recovered from the CO 2 rich flue gas formed in the calcination reactor, from the flue gas stream downstream of the carbonation reactor and/or from CaO formed in the calcination reactor.
8. The method according to claim 1 , wherein the temperature in the carbonation reactor is in the range of 550° C. to 750° C.
9. The method according to claim 1 , wherein the temperature in the calcination reactor is in the range of 800° C. to 1100° C.
10. A system for combustion of a fuel and treatment of the resulting flue gas, said system comprising:
a furnace
a carbonation reactor
a calcination reactor
a dry desulfurizer
wherein the furnace is operative for combusting a fuel with air or oxygen to produce a hot flue gas stream containing at least carbon dioxide (CO 2 ) and sulfur dioxide (SO 2 ),
the carbonation reactor is operative for bringing the flue gas stream into contact with solid calcium oxide (CaO) at a temperature at which CO 2 in the flue gas reacts with CaO to form solid calcium carbonate (CaCO 3 ),
the calcination reactor is operative for heating CaCO 3 formed in the carbonation reactor at a temperature at which CaCO 3 is converted to CaO and CO 2 ,
the calcination reactor comprises means for indirect heating whereby said heating of CaCO 3 is at least partially effected by indirect heat exchange with the hot flue gas stream from the combustion, and
wherein the dry desulfurizer is operative for subjecting the flue gas stream to dry desulfurization before it is brought into contact with CaO in the carbonation reactor.
11. The system according to claim 10 , wherein the dry desulfurizer is configured to operate at a temperature in the range of 200° C. to 700° C.
12. The system according to claim 10 , wherein the dry desulfurizer is operative for bringing the flue gas into contact with solid calcium oxide (CaO) at a temperature whereby SO 2 in the flue gas reacts with CaO to form solid calcium sulfate (CaSO 4 ).
13. The system according to claim 10 , wherein the dry desulfurizer is in fluid connection with and configured to receive CaO recovered from a dust removal unit operative for removing CaO from the CO 2 rich flue gas formed in the calcination reactor.
14. The system according to claim 10 , wherein the dry desulfurizer is in fluid connection with and configured to receive CaO recovered from a dust removal unit operative for removing CaO from the flue gas stream downstream of the carbonation reactor.
15. The system according to claim 10 , wherein the dry desulfurizer is in fluid connection with and configured to receive CaO formed in the calcination reactor.
16. The system according to claim 10 , further comprising a dust removal unit operative for removal of dust from the desulfurized flue gas before it is brought into contact with CaO in the carbonation reactor.
17. The method according to claim 2 , wherein the desulfurization is performed at a temperature in the range of 250° C. to 350° C.
18. The method according to claim 2 , wherein the desulfurization is performed at a temperature in the range of 550° C. to 650° C.
19. The method according to claim 1 , wherein the temperature in the carbonation reactor is about 650° C.
20. The method according to claim 1 , wherein the temperature in the calcination reactor is about 900° C.