Combustion and flue gas treatment system and SOx removal unit

Abstract

The combustion and flue gas treatment system includes a furnace for combusting a fuel with an oxidizer generating a flue gas, ducting for the flue gas connected to a NO.sub.x removal unit and a SO.sub.x removal unit, and a recirculation line for recirculating a part of the flue gas back to the furnace. The SO.sub.x removal unit is located upstream of the NO.sub.x removal unit with reference to the flue gas flow. The recirculation line is connected to the ducting downstream the SO.sub.x removal unit.

Claims

1. A combustion and flue gas treatment system comprising a furnace for combusting a fuel with an oxidizer generating a flue gas, ducting for the flue gas connected to a NO.sub.x removal unit and a SO.sub.X removal unit, a recirculation line for recirculating a part of the flue gas back to the furnace, wherein the SO.sub.x removal unit is located upstream of the NO.sub.x removal unit with reference to the flue gas flow, and in that the recirculation line is connected to the ducting downstream the SO.sub.x removal unit, and wherein the combustion and flue gas treatment system comprises a dust removal unit, the dust removal unit located downstream of the SO.sub.x removal unit and upstream of the NO.sub.x removal unit.

2. The system of claim 1, wherein the dust removal unit is located upstream of a recirculation line connection to the ducting.

3. The system of claim 1, wherein the SO.sub.X removal unit comprises a vessel with an inlet for a flue gas and an outlet for a treated flue gas, and further comprising a pulverized reagent supply for a reagent.

4. The system of claim 3, wherein the pulverized reagent supply comprises a manifold with a plurality of nozzles.

5. The system of claim 3, wherein the pulverized reagent supply comprises a reagent reservoir and a carrier gas supply.

6. The system of claim 1, wherein the SO.sub.X removal unit comprises a vessel with an inlet for a flue gas and an outlet for a treated flue gas, wherein the vessel houses a reagent bed, wherein the inlet and the outlet are located at opposite sides of the vessel with respect to the bed.

7. The system of claim 6, wherein the inlet is at the lower part of the vessel and the outlet is at the upper part of the vessel.

8. The system of claim 1, wherein the furnace is part of a boiler, wherein the system comprises an economizer for heating water supplied to the boiler and a heat exchanger for cooling the flue gas, wherein the SO.sub.x removal unit is located downstream of the economizer and upstream of the heat exchanger.

9. The SO.sub.X removal unit of claim 3, wherein the reagent bed is a fluidized bed.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) Further characteristics and advantages will be more apparent from the description of a preferred but non-exclusive embodiment of the system and device, illustrated by way of non-limiting example in the accompanying drawings, in which:

(2) FIG. 1 shows a combustion and flue gas treatment system of the prior art;

(3) FIGS. 2 and 3 show combustion and flue gas treatment systems in different embodiments of the invention;

(4) FIGS. 4 and 5 show different embodiments of a SO.sub.x removal unit.

DETAILED DESCRIPTION

(5) With reference to the figures, these show a combustion and flue gas treatment system 1 comprising a furnace 2 (for example part of a boiler) for combusting a fuel with an oxidizer generating a flue gas.

(6) The fuel can in different examples be a gas, liquid or solid fuel, but preferably the fuel is a solid fuel such as coal, lignite, etc; the oxidizer can also be any, but preferably it is pure or substantially pure oxygen or air enriched oxygen. The pure or substantially pure oxygen can be pre-heated before being supplied into the furnace 2.

(7) The system 1 further has ducting 15 for conveying the flue gas among the different units that carry out different treatments. In particular, the ducting 15 is connected to the NO.sub.x removal unit 3 and SO.sub.x removal unit 6, with the SO.sub.x removal unit 6 located upstream of the NO.sub.x removal unit 3 with reference to the flue gas flow. For example, the SO.sub.x removal efficiency of the SO.sub.x removal unit 6 is over 60% and preferably over 80%.

(8) The system further comprises the recirculation line 11 for recirculating a part of the flue gas back to the furnace 2; the recirculation line 11 is connected downstream of the SO.sub.x removal unit 6. For example the recirculation line 11 can be connected to the ducting 15 at a position downstream the SO.sub.x removal unit 6 (like in the attached FIGS. 2 and 3) or it is also possible that the recirculation line is connected to the SO.sub.x removal unit at a position downstream thereof or it can be connected to the NO.sub.x removal unit 3 at a position upstream thereof.

(9) With this configuration no heat exchanger like the heat exchanger 4 of the prior art is needed, such that no oxygen slip into the flue gas occurs at the heat exchanger. In addition, since the flue gas is treated at the SO.sub.x removal unit 6 before entering the NO.sub.x removal unit 3, no or a reduced catalyst deactivation occurs at the NO.sub.x removal unit 3. Further, the recirculation between the SO.sub.x removal unit 6 and the NO.sub.x removal unit 3 allows recirculation of the flue gas before its temperature is dropped at the NO.sub.x removal unit 3.

(10) The dust removal unit 5 such as a filter or electrostatic precipitator is located upstream the NO.sub.x removal unit 3; this further helps providing the NO.sub.x removal unit with clean gas, preventing or counteracting a possible catalyst deactivation.

(11) In a first example (FIG. 2), the dust removal unit 5 is located upstream the SO.sub.x removal unit 6. In this example the dust removal unit 5 is located between the furnace 2 and the SO.sub.x removal unit 6. The dust removal unit 5 upstream the SO.sub.x removal unit 6 advantageously allows gathering of fly ash without contamination by the end products at the SO.sub.x removal unit.

(12) In a second example (FIG. 3), the dust removal unit 5 is located downstream the SO.sub.x removal unit 6 and upstream the NO.sub.x removal unit 3. In this example the dust removal unit 5 is located between the SO.sub.x removal unit 6 and NO.sub.x removal unit 3; the connection 16 of the recirculation line 11 to the ducting 15 is preferably located downstream the dust removal unit 5; it is clear that the connection 16 of the recirculation line 11 to the ducting 15 can also be upstream the dust removal unit 5 with reference to the flue gas flow. The dust removal unit 5 downstream the SO.sub.x removal unit 6 advantageously allows gathering of flying ash and CaSO.sub.3 and/or CaSO.sub.4 at the dust removal unit 5 (that can for example include filters).

(13) An economizer (i.e. a heat exchanger that heats the water supplied into the boiler against the flue gas) could also be provided; in this case the SO.sub.x removal unit 6 is preferably located downstream of the economizer. With reference to FIG. 2, in case the economizer is provided, it can for example be located between the furnace 2 and the dust removal unit 5 or between the dust removal unit 5 and the SO.sub.x removal unit 6.

(14) In addition, a heat exchanger 37 can be provided for cooling the flue gas against a cooling medium (for example water or ambient air or other); in this case the SO.sub.x removal unit 6 in preferably provided upstream of the heat exchanger 37.

(15) The SO.sub.x removal unit 6 is a moderate temperature SO.sub.x removal unit able to work up to a temperature of 500 C. and preferably in a temperature range between 250-400 C. preferably 350-400 C.

(16) The SO.sub.x removal unit 6 comprises a vessel 20 with an inlet 21 for a flue gas and an outlet 22 for a treated flue gas.

(17) In addition, the SO.sub.x removal unit 6 comprises a pulverized reagent supply 27 for a reagent.

(18) The pulverized reagent supply 27 comprises a manifold with a plurality of nozzles 29. The manifold 28 is connected to a reservoir 30 and a carrier gas supply 31, such as piping with or without a fan, for recirculating a part of the treated flue gas moving out from the vessel 20 via the outlet 22.

(19) In a different example, the SO.sub.x removal unit 6 comprises a vessel 20 with an inlet 21 for a flue gas and an outlet 22 for a treated flue gas. The vessel 20 further houses a reagent bed 35 and the inlet 21 and the outlet 22 are located at opposite sides of the vessel 20 with respect to the bed 35. The reagent bed 35 is advantageously a fluidized bed (i.e. it is preferably not a fixed bed).

(20) Preferably the inlet 21 is at the lower part of the vessel 20 and the outlet 22 is at the upper part of the vessel 20.

(21) The operation of the system and SO.sub.x removal unit is apparent from that described and illustrated and is substantially the following; in the following reference to the embodiment of FIG. 2 is made, the operation of the embodiment of FIG. 3 is similar.

(22) At the furnace 2 fuel is combusted with an oxidizer; the furnace 2 is preferably an oxy combusted furnace, i.e. fuel such as coal is combusted with pure or substantially pure oxygen or air enriched oxygen.

(23) Flue gas generated at the furnace 2 is supplied to the dust removal unit 5, where dust is removed, and then to the SO.sub.x removal unit 6.

(24) The flue gas moving out of the furnace 2 can have a temperature of about 250-400 C. preferably 350-400 C.; no sensible temperature drop occurs at the dust removal unit 5 such that at the inlet 21 of the SO.sub.x removal unit 6 the flue gas can have a temperature of about 250-400 C. preferably 350-400 C.

(25) At the SO.sub.x removal unit 6 reagent is supplied and SO.sub.x is removed (as explained in detail in the following); the gas moving out of the SO.sub.x removal unit 6 is thus flue gas deprived of SO.sub.x; no sensible temperature drop occurs at the SO.sub.x removal unit 6, such that the temperature of the flue gas moving out of the SO.sub.x removal unit is about 250-400 C. preferably 350-400 C.

(26) Downstream the SO.sub.x removal unit 6 a part of the flue gas deprived from SO.sub.x is recirculated back to the furnace 2 via the connection 16 and recirculation line 11; since this gas has a temperature of about 250-400 C. preferably 350-400 C. (i.e. about the temperature of the flue gas moving out of the furnace 2) no preheating against the flue gas moving out of the furnace 2 is needed.

(27) The part of the flue gas deprived from SO.sub.x that is not recirculated back into the furnace 2 is forwarded to the NO.sub.x removal unit 3, where it is washed against water and a reagent and made to contact a catalyst, in order to remove NO.sub.x.

(28) The flue gas deprived from SO.sub.x and NO.sub.x is then passed through the condenser 7 for water removal (possibly after cooling in the heat exchanger 37) and is then provided to the GPU 8 where it is compressed and condensed, typically a number of times, in order to separate by condensation carbon dioxide CO.sub.2 from other non-condensable gas. Carbon dioxide is thus forwarded to storage or further treatments or other use via the line 9 and the non-condensable gas (nitrogen, argon, etc.) is discharged to the atmosphere via the stack 10.

(29) With particular reference to the operation of the SO.sub.x removal unit 6, it contacts the flue gas with pulverized and substantially dry reagent at a temperature between 250-400 C. preferably 350-400 C. The reagent can be lime (CaO), hydrate lime (calcium hydroxide, Ca(OH).sub.2), limestone (CaCO.sub.3), or other reagents used in the art.

(30) With reference to the embodiment of FIG. 4 and the use of lime CaO and hydrated lime Ca(OH).sub.2 as the reagent, lime and hydrated lime are supplied together with recirculated flue gas deprived from SO.sub.x into the manifold 28 and injected via the nozzles 29 into the vessel 20.

(31) In the vessel 20 the pulverized lime CaO and hydrated lime Ca(OH).sub.2 contact the flue gas containing SO.sub.x that passes through the vessel 20, causing the reactions
SO.sub.2+CaO.fwdarw.CaSO.sub.3
SO.sub.2+Ca(OH).sub.2.fwdarw.CaSO.sub.3.H.sub.2O+H.sub.2O
SO.sub.3+CaO.fwdarw.CaSO.sub.4
SO.sub.3+Ca(OH).sub.2.fwdarw.CaSO.sub.4+H.sub.2O.

(32) With reference to the embodiment of FIG. 5 and the use of lime CaO and hydrated lime Ca(OH).sub.2 as the reagent, pulverized lime and hydrated lime are contained in the bed 35.

(33) The flue gas entering via the inlet 21 passes through the bed 35 causing the reactions
SO.sub.2+CaO.fwdarw.CaSO.sub.3
SO.sub.2+Ca(OH).sub.2.fwdarw.CaSO.sub.3.H.sub.2O+H.sub.2O
SO.sub.3+CaO.fwdarw.CaSO.sub.4
SO.sub.3+Ca(OH).sub.2.fwdarw.CaSO.sub.4+H.sub.2O.

(34) Also in this embodiment, a pulverized reagent supply 27 is preferably provided, to supplement reagent to the bed 35.

(35) The spent sorbent from the SO.sub.x removal unit 6 can for example be used at the direct contact cooler 7.

(36) Naturally the features described may be independently provided from one another.

(37) In practice the materials used and the dimensions can be chosen at will according to requirements and to the state of the art.