CN103239984A - Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler - Google Patents
Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler Download PDFInfo
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- CN103239984A CN103239984A CN2013101791142A CN201310179114A CN103239984A CN 103239984 A CN103239984 A CN 103239984A CN 2013101791142 A CN2013101791142 A CN 2013101791142A CN 201310179114 A CN201310179114 A CN 201310179114A CN 103239984 A CN103239984 A CN 103239984A
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Abstract
The invention relates to a dry-process fine continuous desulfurization device and method for a CFB boiler and belongs to the desulfurization field of boilers. The device consists of a furnace hearth, a cyclone separator, a tail flue path, a lime stone roaster, an air pre-heater, a preliminary dust collector, an SO2 absorber, a circulating liquid tank, a digesting tank, a dust storeroom a, a dust storeroom b, a bag dust collector and a chimney. The method is characterized in that the lime stone roaster and the cyclone separator are arranged in parallel, lime stone powder is sprayed in the roaster from the left upper part, a part of flue gas at the outlet of the furnace hearth is blown in the roaster from the left lower part; CaO decomposed after roasting is collected at the bottom of the roaster and fed to the digesting tank for semi-dry process desulfurization; and decomposed CO2 is exhausted from the top part of the roaster together with the flue gas, and then is mixed with the flue gas in front of the air pre-heater, then passes through the air pre-heater, the preliminary dust collector, the desulfurization absorber, the bag dust collector in sequence and is finally exhausted from the chimney. According to the method, the used desulfurization agent is simple in preparation process, investment and operation cost are low; and the prepared desulfurization agent CaO can satisfy use demand of the semi-dry process desulfurization in the continuous process; meanwhile, the yield of the desulfurization agent can be adjusted by controlling the adding amount of the lime stone powder according to the needs; moreover, the continuous desulfurization process combining the in-furnace dry-process desulfurization and the tail semi-dry process desulfurization can be used for improving the utilization rate and desulfurization efficiency of the desulfurization agent, so that the enterprises can operate economically and the environment-friendly emission requirements can be satisfied.
Description
Technical field
The invention belongs to the boiler desulfurization field, particularly the meticulous continuous desulfurization device and method of a kind of dry method for the CFB boiler.
Background technology
Along with the further increasing of environmental protection standard, the requirement of Air Pollutant Emission limit value is more and more stricter.At the desulfurization situation of current Properties of CFB, factors such as bed temperature, desulfurizing agent quality are difficult to control to optimum range, only rely on desulfuration in furnace can not reach SO
2Emission request, therefore need to adopt SO in the method reduction flue gas that desulfuration in furnace combines with the tail flue gas desulfurization
2Content is to satisfy the pollutant emission requirement of environmental regulations.
At present, flue gas desulfurization method commonly used has several different methods such as limestone-gypsum wet process of FGD, semi-dry process flue gas desulphurization and the ammonia process of desulfurization.Wherein the semi-dry desulphurization method mainly is to utilize to contain lime (drier of CaO or dry calcium hydroxide (Ca (OH)
2) absorb the SO in the flue gas
2The while semi-dry desulfurizing process takes up an area of less, the investment operating cost is low, can obtain higher again under the moderate situation of calcium to sulphur mole ratio even near the desulfuration efficiency of wet desulphurization level, be particularly suitable for building the limited old factory in place and transform and adopt, be an important development direction of desulfur technology from now on.
For the drier that contains lime (CaO) in the semi-dry desulphurization technology or dry calcium hydroxide (Ca (OH)
2) all need CaO, along with the severization of environmental protection standard, flue gas desulfurization becomes the significant challenge that current coal-fired unit faces, and also more and more receives publicity to building unit semi-dry process flue gas desulphurization technology.Therefore how desulphurization in circulating fluidized bed boiler carries out reasonable combination with the tail flue gas semi-dry desulphurization, guarantees under the unit safety economical operation prerequisite, improves the utilization rate of desulfurizing agent and the desulfuration efficiency of unit and becomes the hot issue that the research worker studies.
Summary of the invention
The objective of the invention is to solve above-mentioned the deficiencies in the prior art, a kind of meticulous continuous desulfurization device of dry method that is used for the CFB boiler that the used desulfurizing agent of semi-dry desulphurization is produced in the continuous desulfurization technology that has is provided;
Another object of the present invention provides the meticulous continuous desulfurization method of a kind of dry method for the CFB boiler.
The present invention for the technical scheme that solves above-mentioned technical deficiency and adopt is: the meticulous continuous desulfurization device of a kind of dry method for the CFB boiler, comprise chimney (13), it is characterized in that it also comprises: CFB boiler furnace (1), cyclone separator (2), back-end ductwork (3), limestone calcination device (4), air preheater (5), pre-duster (6), grey storehouse a(10), tail flue gas semi-dry desulphurization system; Wherein: described tail flue gas semi-dry desulphurization system is by SO
2Absorber (7), circulation flow container (8), digester (9), grey storehouse b(11) sack cleaner (12) composition; Described CFB boiler furnace (1) is connected to cyclone separator (2) and limestone calcination device (4) respectively by flue; Cyclone separator (2) bottom links to each other with burner hearth (1) through the feed back pipeline, and cyclone separator (2) top is connected to back-end ductwork (3) through flue; Agstone is delivered to limestone calcination device (4) through pulverized coal feed pipe, and limestone calcination device (4) bottom links to each other with digester (9) by pulverized coal feed pipe; The merging pipeline is connected to air preheater (5), air preheater (5), pre-duster (6), SO again limestone calcination device (4) top is connected to the flue of being drawn by cyclone separator (2) through flue after
2Absorber (7), sack cleaner (12) and chimney (13) are connected by flue successively; Pre-duster (6) is through ash conveying pipe and grey storehouse a(10) link to each other, sack cleaner (12) is through ash conveying pipe and grey storehouse b(11) link to each other; Digester (9) and SO
2Absorber (7) connects SO through calcium hydroxide breast conveyance conduit
2Absorber (7) to the flow container that circulates (8) connects through pulverized coal feed pipe, and circulation flow container (8) is to SO
2Absorber (7) connects by the desulfurizing agent circulating line; Sack cleaner (12) is to grey storehouse b(11) ash conveying pipe through circulating ash pipeline and SO
2Absorber (7) to the pulverized coal feed pipe of the flow container that circulates (8) connects.
The present invention is used for the method for the meticulous continuous desulfurization of dry method of CFB boiler, and it comprises the following steps:
(1) be that 800 ℃～900 ℃, flow are 229m with temperature
3/ h～457m
3The flue gas of the CFB boiler furnace (1) of/h blows in the limestone calcination device (4) from the lower left quarter of limestone calcination device (4); Again with CaCO
3Purity is 70%～90%, and straying quatity is that the agstone of 20t/h～40t/h is sprayed in the limestone calcination device (4) by limestone calcination device (4) upper left quarter, and flue gas evenly mixes and calcining and decomposing in limestone calcination device (4) with the agstone particle;
(2) output that calcining and decomposing is gone out is that the partial desulfurization agent CaO of 7.84t/h～20.16t/h is collected and delivered to the digester (9) in the tail flue gas semi-dry desulphurization system by the bottom of limestone calcination device (4), desulfurizing agent CaO with add water in the digester (9) and make the calcium hydroxide breast and send into SO
2Absorber (7) absorbs the SO in the flue gas
2
(3) CO that goes out of calcining and decomposing
2300 ℃～400 ℃ the flue gas of discharging from limestone calcination device (4) top with flue gas, with be arranged in back-end ductwork (3) bottom economizer after, the preceding flue gas of air preheater (5) passes through air preheater (5) after mixing again successively, the flue gas of process air preheater (5) at first enters pre-duster (6) and carries out pre-dedusting, in directly isolate 70%～80% flyash, and deliver to grey storehouse a(10) in, the flue gas in the tail flue gas semi-dry desulphurization system after pre-duster (6) is removed most of flyash is by SO
2The right middle and upper part of absorber (7) enters SO
2In the absorber (7), simultaneously from SO
2The upper right quarter of absorber (7) is between the flue gas inlet point, adds water successively, the calcium hydroxide breast in the digester (9), the loop slurry in the circulation flow container (8); Milk of lime is squeezed into SO by pump
2In the absorber (7), be atomized into absorbent behind the droplet by atomising device and mix with flue gas and contact, and with flue gas in SO
2Chemical reaction takes place finally generate calcium sulfate, in the flue gas by SO
2Remove; The moisture that absorbent is brought in the course of reaction is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner (12) with dried granules thing form with flue gas and are collected, and flue gas then enters chimney (13) and enters in the atmosphere after dedusting.
Because the present invention adopted technique scheme, have that the used desulfurizing agent reparation technology of semi-dry desulphurization in the continuous desulfurization technology is simple, the investment operating cost is low; The desulfurizing agent CaO that produces can satisfy semi-dry desulphurization consumption in the continuous processing, simultaneously the output that can regulate desulfurizing agent by the agstone amount of control adding according to demand; The continuous desulfurization technology that dry desulfurization combines with the afterbody semi-dry desulphurization in the stove, with the desulfurizing agent do not collected with the flue gas outflow in part sack cleaner gleanings and the absorber and desulfurization reaction product together deliver to the circulation flow container again pump power be delivered to SO
2Recycling in the absorber, improved sorbent utilization and desulfuration efficiency greatly, make not only economical operation but also satisfy the environment protection emission requirement of enterprise.
Description of drawings
Fig. 1 is structural representation of the present invention;
The specific embodiment
Embodiment 1
As shown in Figure 1: the meticulous continuous desulfurization device of a kind of dry method for the CFB boiler in the present embodiment, comprise chimney 13, other also comprises: CFB boiler furnace 1, cyclone separator 2, back-end ductwork 3, limestone calcination device 4, air preheater 5, pre-duster 6, grey storehouse a10, tail flue gas semi-dry desulphurization system; Wherein: described tail flue gas semi-dry desulphurization system is by SO
2Absorber 7, circulation flow container 8, digester 9, grey storehouse b11 sack cleaner 12 are formed; Described CFB boiler furnace 1 is connected to cyclone separator 2 and limestone calcination device 4 respectively by flue; Cyclone separator 2 bottoms link to each other with burner hearth 1 through the feed back pipeline, and cyclone separator 2 tops are connected to back-end ductwork 3 through flue; Agstone is delivered to limestone calcination device 4 through pulverized coal feed pipe, and limestone calcination device 4 bottoms link to each other with digester 9 by pulverized coal feed pipe; The merging pipeline is connected to air preheater 5, air preheater 5, pre-duster 6, SO again limestone calcination device 4 tops are connected to the flue of being drawn by cyclone separator 2 through flue after
2Absorber 7, sack cleaner 12 and chimney 13 are connected by flue successively; Pre-duster 6 links to each other with grey storehouse a10 through ash conveying pipe, and sack cleaner 12 links to each other with grey storehouse b11 through ash conveying pipe; Digester 9 and SO
2Absorber 7 connects SO through calcium hydroxide breast conveyance conduit
2Absorber 7 to circulation flow container 8 connects through pulverized coal feed pipe, and circulation flow container 8 is to SO
2Absorber 7 connects by the desulfurizing agent circulating line; Sack cleaner 12 to the ash conveying pipe of grey storehouse b11 through circulating ash pipeline and SO
2Absorber 7 to the pulverized coal feed pipe of circulation flow container 8 connects.
The method of a kind of meticulous continuous desulfurization of dry method for the CFB boiler of the present invention, it comprises the following steps:
(1) be that 800 ℃, flow are 229m with temperature
3The flue gas of the CFB boiler furnace 1 of/h blows in the limestone calcination device 4 from the lower left quarter of limestone calcination device 4; Again with CaCO
3Purity is 70%, and straying quatity is that the agstone of 20t/h is sprayed in the limestone calcination device 4 by limestone calcination device 4 upper left quarters, and flue gas evenly mixes and calcining and decomposing in limestone calcination device 4 with the agstone particle;
(2) output that calcining and decomposing is gone out is that the partial desulfurization agent CaO of 7.84t/h is collected and delivered to the digester 9 in the tail flue gas semi-dry desulphurization system by the bottom of limestone calcination device 4, desulfurizing agent CaO with add water in the digester 9 and make the calcium hydroxide breast and send into SO
2The SO that absorber 7 absorbs in the flue gas
2
(3) CO that goes out of calcining and decomposing
2300 ℃ the flue gas of discharging from limestone calcination device 4 tops with flue gas, with be arranged in back-end ductwork 3 bottom economizers after, flue gas before the air preheater 5 passes through air preheater 5 after mixing again successively, the flue gas of process air preheater 5 at first enters pre-duster 6 and carries out pre-dedusting, in directly isolate 70% flyash, and deliver among the grey storehouse a10, the flue gas in the tail flue gas semi-dry desulphurization system after pre-duster 6 is removed most of flyash is by SO
2Absorber 7 right middle and upper parts enter SO
2In the absorber 7, simultaneously from SO
2The upper right quarter of absorber 7 is between the flue gas inlet point, adds water successively, the calcium hydroxide breast in the digester 9, the loop slurry in the circulation flow container 8; Milk of lime is squeezed into SO by pump
2In the absorber 7, be atomized into absorbent behind the droplet by atomising device and mix with flue gas and contact, and with flue gas in SO
2Chemical reaction takes place finally generate calcium sulfate, in the flue gas by SO
2Remove; The moisture that absorbent is brought in the course of reaction is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner 12 with dried granules thing form with flue gas and are collected, and flue gas then enters chimney 13 and enters in the atmosphere after dedusting; Be to improve sorbent utilization, with the desulfurizing agent do not collected with the flue gas outflow in part sack cleaner 12 gleanings and the absorber and desulfurization reaction product together deliver to circulation flow container 8 again pump power be delivered to SO
2Recycling in the absorber 7.
As shown in Figure 1: the meticulous continuous desulfurization device of a kind of dry method for the CFB boiler in the present embodiment, comprise chimney 13, other also comprises: CFB boiler furnace 1, cyclone separator 2, back-end ductwork 3, limestone calcination device 4, air preheater 5, pre-duster 6, grey storehouse a10, tail flue gas semi-dry desulphurization system; Wherein: described tail flue gas semi-dry desulphurization system is by SO
2Absorber 7, circulation flow container 8, digester 9, grey storehouse b11 sack cleaner 12 are formed; Described CFB boiler furnace 1 is connected to cyclone separator 2 and limestone calcination device 4 respectively by flue; Cyclone separator 2 bottoms link to each other with burner hearth 1 through the feed back pipeline, and cyclone separator 2 tops are connected to back-end ductwork 3 through flue; Agstone is delivered to limestone calcination device 4 through pulverized coal feed pipe, and limestone calcination device 4 bottoms link to each other with digester 9 by pulverized coal feed pipe; The merging pipeline is connected to air preheater 5, air preheater 5, pre-duster 6, SO again limestone calcination device 4 tops are connected to the flue of being drawn by cyclone separator 2 through flue after
2Absorber 7, sack cleaner 12 and chimney 13 are connected by flue successively; Pre-duster 6 links to each other with grey storehouse a10 through ash conveying pipe, and sack cleaner 12 links to each other with grey storehouse b11 through ash conveying pipe; Digester 9 and SO
2Absorber 7 connects SO through calcium hydroxide breast conveyance conduit
2Absorber 7 to circulation flow container 8 connects through pulverized coal feed pipe, and circulation flow container 8 is to SO
2Absorber 7 connects by the desulfurizing agent circulating line; Sack cleaner 12 to the ash conveying pipe of grey storehouse b11 through circulating ash pipeline and SO
2Absorber 7 to the pulverized coal feed pipe of circulation flow container 8 connects.
The method of a kind of meticulous continuous desulfurization of dry method for the CFB boiler of the present invention, it comprises the following steps:
(1) be that 900 ℃, flow are 457m with temperature
3The flue gas of the CFB boiler furnace 1 of/h blows in the limestone calcination device 4 from the lower left quarter of limestone calcination device 4; Again with CaCO
3Purity is 90%, and straying quatity is that the agstone of 40t/h is sprayed in the limestone calcination device 4 by limestone calcination device 4 upper left quarters, and flue gas evenly mixes and calcining and decomposing in limestone calcination device 4 with the agstone particle;
(2) output that calcining and decomposing is gone out is that the partial desulfurization agent CaO of 20.16t/h is collected and delivered to the digester 9 in the tail flue gas semi-dry desulphurization system by the bottom of limestone calcination device 4, desulfurizing agent CaO with add water in the digester 9 and make the calcium hydroxide breast and send into SO
2The SO that absorber 7 absorbs in the flue gas
2
(3) CO that goes out of calcining and decomposing
2400 ℃ the flue gas of discharging from limestone calcination device 4 tops with flue gas, with be arranged in back-end ductwork 3 bottom economizers after, flue gas before the air preheater 5 passes through air preheater 5 after mixing again successively, the flue gas of process air preheater 5 at first enters pre-duster 6 and carries out pre-dedusting, in directly isolate 80% flyash, and deliver among the grey storehouse a10, the flue gas in the tail flue gas semi-dry desulphurization system after pre-duster 6 is removed most of flyash is by SO
2Absorber 7 right middle and upper parts enter SO
2In the absorber 7, simultaneously from SO
2The upper right quarter of absorber 7 is between the flue gas inlet point, adds water successively, the calcium hydroxide breast in the digester 9, the loop slurry in the circulation flow container 8; Milk of lime is squeezed into SO by pump
2In the absorber 7, be atomized into absorbent behind the droplet by atomising device and mix with flue gas and contact, and with flue gas in SO
2Chemical reaction takes place finally generate calcium sulfate, in the flue gas by SO
2Remove; The moisture that absorbent is brought in the course of reaction is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner 12 with dried granules thing form with flue gas and are collected, and flue gas then enters chimney 13 and enters in the atmosphere after dedusting; Be to improve sorbent utilization, with the desulfurizing agent do not collected with the flue gas outflow in part sack cleaner 12 gleanings and the absorber and desulfurization reaction product together deliver to circulation flow container 8 again pump power be delivered to SO
2Recycling in the absorber 7.
Claims (2)
1. meticulous continuous desulfurization device of dry method that is used for the CFB boiler, comprise chimney (13), it is characterized in that it also comprises: CFB boiler furnace (1), cyclone separator (2), back-end ductwork (3), limestone calcination device (4), air preheater (5), pre-duster (6), grey storehouse a(10), tail flue gas semi-dry desulphurization system; Wherein: described tail flue gas semi-dry desulphurization system is by SO
2Absorber (7), circulation flow container (8), digester (9), grey storehouse b(11) sack cleaner (12) composition; Described CFB boiler furnace (1) is connected to cyclone separator (2) and limestone calcination device (4) respectively by flue; Cyclone separator (2) bottom links to each other with burner hearth (1) through the feed back pipeline, and cyclone separator (2) top is connected to back-end ductwork (3) through flue; Agstone is delivered to limestone calcination device (4) through pulverized coal feed pipe, and limestone calcination device (4) bottom links to each other with digester (9) by pulverized coal feed pipe; The merging pipeline is connected to air preheater (5), air preheater (5), pre-duster (6), SO again limestone calcination device (4) top is connected to the flue of being drawn by cyclone separator (2) through flue after
2Absorber (7), sack cleaner (12) and chimney (13) are connected by flue successively; Pre-duster (6) is through ash conveying pipe and grey storehouse a(10) link to each other, sack cleaner (12) is through ash conveying pipe and grey storehouse b(11) link to each other; Digester (9) and SO
2Absorber (7) connects SO through calcium hydroxide breast conveyance conduit
2Absorber (7) to the flow container that circulates (8) connects through pulverized coal feed pipe, and circulation flow container (8) is to SO
2Absorber (7) connects by the desulfurizing agent circulating line; Sack cleaner (12) is to grey storehouse b(11) ash conveying pipe through circulating ash pipeline and SO
2Absorber (7) to the pulverized coal feed pipe of the flow container that circulates (8) connects.
2. a method that is used for the meticulous continuous desulfurization of dry method of CFB boiler is characterized in that comprising the following steps:
(1) be that 800 ℃～900 ℃, flow are 229m with temperature
3/ h～457m
3The flue gas of the CFB boiler furnace (1) of/h blows in the limestone calcination device (4) from the lower left quarter of limestone calcination device (4); Again with CaCO
3Purity is 70%～90%, and straying quatity is that the agstone of 20t/h～40t/h is sprayed in the limestone calcination device (4) by limestone calcination device (4) upper left quarter, and flue gas evenly mixes and calcining and decomposing in limestone calcination device (4) with the agstone particle;
(2) output that calcining and decomposing is gone out is that the partial desulfurization agent CaO of 7.84t/h～20.16t/h is collected and delivered to the digester (9) in the tail flue gas semi-dry desulphurization system by the bottom of limestone calcination device (4), desulfurizing agent CaO with add water in the digester (9) and make the calcium hydroxide breast and send into SO
2Absorber (7) absorbs the SO in the flue gas
2
(3) CO that goes out of calcining and decomposing
2300 ℃～400 ℃ the flue gas of discharging from limestone calcination device (4) top with flue gas, with be arranged in back-end ductwork (3) bottom economizer after, the preceding flue gas of air preheater (5) passes through air preheater (5) after mixing again successively, the flue gas of process air preheater (5) at first enters pre-duster (6) and carries out pre-dedusting, in directly isolate 70%～80% flyash, and deliver to grey storehouse a(10) in, the flue gas in the tail flue gas semi-dry desulphurization system after pre-duster (6) is removed most of flyash is by SO
2The right middle and upper part of absorber (7) enters SO
2In the absorber (7), simultaneously from SO
2The upper right quarter of absorber (7) is between the flue gas inlet point, adds water successively, the calcium hydroxide breast in the digester (9), the loop slurry in the circulation flow container (8); Milk of lime is squeezed into SO by pump
2In the absorber (7), be atomized into absorbent behind the droplet by atomising device and mix with flue gas and contact, and with flue gas in SO
2Chemical reaction takes place finally generate calcium sulfate, in the flue gas by SO
2Remove; The moisture that absorbent is brought in the course of reaction is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner (12) with dried granules thing form with flue gas and are collected, and flue gas then enters chimney (13) and enters in the atmosphere after dedusting.
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| CN103816794A (en) * | 2014-03-05 | 2014-05-28 | 青岛新天地固体废物综合处置有限公司 | Stack gas treatment device through adopting semi-dry method and treatment method of device |
| CN104896494A (en) * | 2015-06-19 | 2015-09-09 | 山西大学 | Afterheat recovery device applied to dry desulfurization technology |
| CN115364655A (en) * | 2022-08-16 | 2022-11-22 | 中冶南方都市环保工程技术股份有限公司 | System and method for purifying electric furnace flue gas by multiple pollutants |
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| CN104896494A (en) * | 2015-06-19 | 2015-09-09 | 山西大学 | Afterheat recovery device applied to dry desulfurization technology |
| CN115364655A (en) * | 2022-08-16 | 2022-11-22 | 中冶南方都市环保工程技术股份有限公司 | System and method for purifying electric furnace flue gas by multiple pollutants |
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