CN103239984B - 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
- Publication number
- CN103239984B CN103239984B CN201310179114.2A CN201310179114A CN103239984B CN 103239984 B CN103239984 B CN 103239984B CN 201310179114 A CN201310179114 A CN 201310179114A CN 103239984 B CN103239984 B CN 103239984B
- Authority
- CN
- China
- Prior art keywords
- flue gas
- desulfurization
- absorber
- limestone calcination
- flue
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
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 boiler desulfurization field, particularly the meticulous continuous desulfurization device of a kind of dry method for CFB boiler and method.
Background technology
Along with the further increasing of environmental protection standard, the requirement of Air Pollutant Emission limit value is more and more stricter.For the desulfurization situation of previous cycle fluid bed unit, the factors such as bed temperature, desulfurizing agent quality are difficult to control to optimum range, only rely on desulfuration in furnace not reach SO
2emission request, therefore need to adopt the method that combines with tail flue gas desulfurization of desulfuration in furnace to reduce SO in flue gas
2content, to meet the pollutant emission requirement of environmental regulations.
At present, the method that flue gas desulfurization is conventional has the multiple methods such as wet desulfurization of flue gas by limestone-gypsum method, semi-dry process flue gas desulphurization and the ammonia process of desulfurization.Wherein semi-dry desulphurization method mainly utilizes containing lime (drier of CaO or the calcium hydroxide (Ca (OH) of drying
2) absorb SO in flue gas
2simultaneously semi-dry desulfurizing process takes up an area less, investment operating cost is low, can obtain again higher even close to the desulfuration efficiency of wet desulphurization level when calcium to sulphur mole ratio is moderate, the old factory transformation being particularly suitable for building place limited adopts, and is an important development direction of desulfur technology from now on.
The drier of lime (CaO) or the calcium hydroxide (Ca (OH) of drying is contained in semi-dry desulphurization technology
2) all need CaO, along with the severization of environmental protection standard, flue gas desulfurization becomes the significant challenge that current coal unit faces, and also more and more receives publicity to built unit Summary of Semi-dry Flue Gas Desulfurization.Therefore how desulphurization in circulating fluidized bed boiler carries out reasonable combination with tail flue gas semi-dry desulphurization, and under ensureing unit safety economical operation prerequisite, the raising utilization rate of desulfurizing agent and the desulfuration efficiency of unit become the hot issue of research worker's research.
Summary of the invention
The object of the invention is to solve above-mentioned the deficiencies in the prior art, a kind of meticulous continuous desulfurization device of the dry method for CFB boiler having desulfurizing agent that in continuous desulfurization technique, semi-dry desulphurization is used and produce is provided;
Another object of the present invention is to provide a kind of meticulous continuous desulfurization method of dry method for CFB boiler.
The present invention is the technical scheme that the above-mentioned technical deficiency of solution adopts: the meticulous continuous desulfurization device of a kind of dry method for 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 is connected with burner hearth (1) through 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 is connected with digester (9) by pulverized coal feed pipe; Limestone calcination device (4) top is connected to through flue and merges pipeline after the flue of being drawn by cyclone separator (2) and be connected to air preheater (5) again, air preheater (5), pre-duster (6), SO
2absorber (7), sack cleaner (12) are connected by flue successively with chimney (13); Pre-duster (6) is through ash conveying pipe and grey storehouse a(10) be connected, sack cleaner (12) is through ash conveying pipe and grey storehouse b(11) be connected; Digester (9) and SO
2absorber (7) connects through calcium hydroxide breast conveyance conduit, SO
2absorber (7) connects to the flow container that circulates (8) through pulverized coal feed pipe, and the flow container that circulates (8) is to SO
2absorber (7) is connected by desulfurizing agent circulating line; Sack cleaner (12) is to grey storehouse b(11) ash conveying pipe through circulating ash pipeline and SO
2absorber (7) connects to the pulverized coal feed pipe of the flow container that circulates (8).
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 800 DEG C ~ 900 DEG C by temperature, flow is 229m
3/ h ~ 457m
3the flue gas of the CFB boiler furnace (1) of/h blows in limestone calcination device (4) from the lower left quarter of limestone calcination device (4); Again by CaCO
3purity is 70% ~ 90%, and straying quatity is that the agstone of 20t/h ~ 40t/h sprays in limestone calcination device (4) by limestone calcination device (4) upper left quarter, flue gas and agstone particle Homogeneous phase mixing calcining and decomposing in limestone calcination device (4);
(2) output calcining and decomposing gone out be the partial desulfurization agent CaO of 7.84t/h ~ 20.16t/h by the bottom collection of limestone calcination device (4) and the digester (9) delivered in tail flue gas semi-dry desulphurization system, desulfurizing agent CaO and the water added in digester (9) are made calcium hydroxide breast and are sent into SO
2absorber (7) absorbs the SO in flue gas
2;
(3) CO that goes out of calcining and decomposing
2the flue gas of 300 DEG C ~ 400 DEG C of discharging from limestone calcination device (4) top with flue gas, with be arranged in back-end ductwork (3) bottom economizer after, the front flue gas of air preheater (5) mix after more successively through air preheater (5), first enter pre-duster (6) through the flue gas of air preheater (5) and carry out pre-dedusting, in the flyash directly isolating 70% ~ 80%, and deliver to grey storehouse a(10) in, remove the flue gas after most of flyash by SO through pre-duster (6) in tail flue gas semi-dry desulphurization system
2absorber (7) right top enters SO
2in absorber (7), simultaneously from SO
2between the upper right quarter of absorber (7) to flue gas inlet point, add the calcium hydroxide breast in water, digester (9), the loop slurry in circulation flow container (8) successively; Milk of lime squeezes into SO by pump
2in absorber (7), be atomized into the absorbent after droplet by atomising device and mix with flue gas and contact, and with the SO in flue gas
2occur chemical reaction finally generate calcium sulfate, in flue gas by SO
2remove; The moisture that in course of reaction, absorbent is brought into is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner (12) with the particulate form of drying with flue gas and are collected, and flue gas then enters chimney (13) and enters in air after dedusting.
Owing to present invention employs technique scheme, have that the desulfurizing agent reparation technology used of semi-dry desulphurization in continuous desulfurization technique is simple, investment operating cost is low; The desulfurizing agent CaO produced can meet semi-dry desulphurization consumption in continuous processing, can be regulated the output of desulfurizing agent according to demand by the agstone amount controlling to add simultaneously; The continuous desulfurization technique that in stove, dry desulfurization combines with afterbody semi-dry desulphurization, the desulfurizing agent collected not flowing out with flue gas in part sack cleaner gleanings and absorber and desulfurization reaction product together deliver to circulation flow container again pumping forces be delivered to SO
2absorber Inner eycle utilizes, and substantially increases sorbent utilization and desulfuration efficiency, makes enterprise's not only economical operation but also meet environment protection emission requirement.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention;
Detailed description of the invention
Embodiment 1
As shown in Figure 1: the meticulous continuous desulfurization device of a kind of dry method for 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 form; Described CFB boiler furnace 1 is connected to cyclone separator 2 and limestone calcination device 4 respectively by flue; Be connected with burner hearth 1 through feed back pipeline bottom cyclone separator 2, 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, is connected bottom limestone calcination device 4 by pulverized coal feed pipe with digester 9; Limestone calcination device 4 top is connected to through flue and merges pipeline after the flue of being drawn by cyclone separator 2 and be connected to air preheater 5 again, air preheater 5, pre-duster 6, SO
2absorber 7, sack cleaner 12 are connected by flue successively with chimney 13; Pre-duster 6 is connected with grey storehouse a10 through ash conveying pipe, and sack cleaner 12 is connected with grey storehouse b11 through ash conveying pipe; Digester 9 and SO
2absorber 7 connects through calcium hydroxide breast conveyance conduit, SO
2absorber 7 to circulation flow container 8 connects through pulverized coal feed pipe, and flow container 8 to the SO that circulates
2absorber 7 is connected by desulfurizing agent circulating line; Sack cleaner 12 to the ash conveying pipe of grey storehouse b11 through circulating ash pipeline and SO
2the pulverized coal feed pipe of absorber 7 to circulation flow container 8 connects.
The method of the meticulous continuous desulfurization of a kind of dry method for CFB boiler of the present invention, it comprises the following steps:
(1) be 800 DEG C by temperature, flow is 229m
3the flue gas of the CFB boiler furnace 1 of/h blows in limestone calcination device 4 from the lower left quarter of limestone calcination device 4; Again by CaCO
3purity is 70%, and straying quatity is that the agstone of 20t/h sprays in limestone calcination device 4 by limestone calcination device 4 upper left quarter, flue gas and agstone particle Homogeneous phase mixing calcining and decomposing in limestone calcination device 4;
(2) output calcining and decomposing gone out be the partial desulfurization agent CaO of 7.84t/h by the bottom collection of limestone calcination device 4 and the digester 9 delivered in tail flue gas semi-dry desulphurization system, desulfurizing agent CaO and the water added in digester 9 are made calcium hydroxide breast and are sent into SO
2absorber 7 absorbs the SO in flue gas
2;
(3) CO that goes out of calcining and decomposing
2with the flue gas of 300 DEG C that flue gas is discharged from limestone calcination device 4 top, again successively through air preheater 5 after mixing with the flue gas be arranged in bottom back-end ductwork 3 after economizer, before air preheater 5, first enter pre-duster 6 through the flue gas of air preheater 5 and carry out pre-dedusting, in the flyash directly isolating 70%, and deliver in grey storehouse a10, remove the flue gas after most of flyash by SO through pre-duster 6 in tail flue gas semi-dry desulphurization system
2the right top of absorber 7 enters SO
2in absorber 7, simultaneously from SO
2between the upper right quarter of absorber 7 to flue gas inlet point, add the calcium hydroxide breast in water, digester 9, the loop slurry in circulation flow container 8 successively; Milk of lime squeezes into SO by pump
2in absorber 7, be atomized into the absorbent after droplet by atomising device and mix with flue gas and contact, and with the SO in flue gas
2occur chemical reaction finally generate calcium sulfate, in flue gas by SO
2remove; The moisture that in course of reaction, absorbent is brought into is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner 12 with the particulate form of drying with flue gas and are collected, and flue gas then enters chimney 13 and enters in air after dedusting; For improve sorbent utilization, the desulfurizing agent collected not flowing out with flue gas in part sack cleaner 12 gleanings and absorber and desulfurization reaction product together deliver to circulation flow container 8 again pumping forces be delivered to SO
2absorber 7 Inner eycle utilizes.
Embodiment 2
As shown in Figure 1: the meticulous continuous desulfurization device of a kind of dry method for 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 form; Described CFB boiler furnace 1 is connected to cyclone separator 2 and limestone calcination device 4 respectively by flue; Be connected with burner hearth 1 through feed back pipeline bottom cyclone separator 2, 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, is connected bottom limestone calcination device 4 by pulverized coal feed pipe with digester 9; Limestone calcination device 4 top is connected to through flue and merges pipeline after the flue of being drawn by cyclone separator 2 and be connected to air preheater 5 again, air preheater 5, pre-duster 6, SO
2absorber 7, sack cleaner 12 are connected by flue successively with chimney 13; Pre-duster 6 is connected with grey storehouse a10 through ash conveying pipe, and sack cleaner 12 is connected with grey storehouse b11 through ash conveying pipe; Digester 9 and SO
2absorber 7 connects through calcium hydroxide breast conveyance conduit, SO
2absorber 7 to circulation flow container 8 connects through pulverized coal feed pipe, and flow container 8 to the SO that circulates
2absorber 7 is connected by desulfurizing agent circulating line; Sack cleaner 12 to the ash conveying pipe of grey storehouse b11 through circulating ash pipeline and SO
2the pulverized coal feed pipe of absorber 7 to circulation flow container 8 connects.
The method of the meticulous continuous desulfurization of a kind of dry method for CFB boiler of the present invention, it comprises the following steps:
(1) be 900 DEG C by temperature, flow is 457m
3the flue gas of the CFB boiler furnace 1 of/h blows in limestone calcination device 4 from the lower left quarter of limestone calcination device 4; Again by CaCO
3purity is 90%, and straying quatity is that the agstone of 40t/h sprays in limestone calcination device 4 by limestone calcination device 4 upper left quarter, flue gas and agstone particle Homogeneous phase mixing calcining and decomposing in limestone calcination device 4;
(2) output calcining and decomposing gone out be the partial desulfurization agent CaO of 20.16t/h by the bottom collection of limestone calcination device 4 and the digester 9 delivered in tail flue gas semi-dry desulphurization system, desulfurizing agent CaO and the water added in digester 9 are made calcium hydroxide breast and are sent into SO
2absorber 7 absorbs the SO in flue gas
2;
(3) CO that goes out of calcining and decomposing
2with the flue gas of 400 DEG C that flue gas is discharged from limestone calcination device 4 top, again successively through air preheater 5 after mixing with the flue gas be arranged in bottom back-end ductwork 3 after economizer, before air preheater 5, first enter pre-duster 6 through the flue gas of air preheater 5 and carry out pre-dedusting, in the flyash directly isolating 80%, and deliver in grey storehouse a10, remove the flue gas after most of flyash by SO through pre-duster 6 in tail flue gas semi-dry desulphurization system
2the right top of absorber 7 enters SO
2in absorber 7, simultaneously from SO
2between the upper right quarter of absorber 7 to flue gas inlet point, add the calcium hydroxide breast in water, digester 9, the loop slurry in circulation flow container 8 successively; Milk of lime squeezes into SO by pump
2in absorber 7, be atomized into the absorbent after droplet by atomising device and mix with flue gas and contact, and with the SO in flue gas
2occur chemical reaction finally generate calcium sulfate, in flue gas by SO
2remove; The moisture that in course of reaction, absorbent is brought into is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner 12 with the particulate form of drying with flue gas and are collected, and flue gas then enters chimney 13 and enters in air after dedusting; For improve sorbent utilization, the desulfurizing agent collected not flowing out with flue gas in part sack cleaner 12 gleanings and absorber and desulfurization reaction product together deliver to circulation flow container 8 again pumping forces be delivered to SO
2absorber 7 Inner eycle utilizes.
Claims (2)
1. the meticulous continuous desulfurization device of the dry method for 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 is connected with burner hearth (1) through 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 is connected with digester (9) by pulverized coal feed pipe; Limestone calcination device (4) top is connected to through flue and merges pipeline after the flue of being drawn by cyclone separator (2) and be connected to air preheater (5) again, air preheater (5), pre-duster (6), SO
2absorber (7), sack cleaner (12) are connected by flue successively with chimney (13); Pre-duster (6) is through ash conveying pipe and grey storehouse a(10) be connected, sack cleaner (12) is through ash conveying pipe and grey storehouse b(11) be connected; Digester (9) and SO
2absorber (7) connects through calcium hydroxide breast conveyance conduit, SO
2absorber (7) connects to the flow container that circulates (8) through pulverized coal feed pipe, and the flow container that circulates (8) is to SO
2absorber (7) is connected by desulfurizing agent circulating line; Sack cleaner (12) is to grey storehouse b(11) ash conveying pipe through circulating ash pipeline and SO
2absorber (7) connects to the pulverized coal feed pipe of the flow container that circulates (8).
2., for a method for the meticulous continuous desulfurization of dry method of CFB boiler, it is characterized in that comprising the following steps:
(1) be 800 DEG C ~ 900 DEG C by temperature, flow is 229m
3/ h ~ 457m
3the flue gas of the CFB boiler furnace (1) of/h blows in limestone calcination device (4) from the lower left quarter of limestone calcination device (4); Again by CaCO
3purity is 70% ~ 90%, and straying quatity is that the agstone of 20t/h ~ 40t/h sprays in limestone calcination device (4) by limestone calcination device (4) upper left quarter, flue gas and agstone particle Homogeneous phase mixing calcining and decomposing in limestone calcination device (4);
(2) output calcining and decomposing gone out be the partial desulfurization agent CaO of 7.84t/h ~ 20.16t/h by the bottom collection of limestone calcination device (4) and the digester (9) delivered in tail flue gas semi-dry desulphurization system, desulfurizing agent CaO and the water added in digester (9) are made calcium hydroxide breast and are sent into SO
2absorber (7) absorbs the SO in flue gas
2;
(3) CO that goes out of calcining and decomposing
2the flue gas of 300 DEG C ~ 400 DEG C of discharging from limestone calcination device (4) top with flue gas, with be arranged in back-end ductwork (3) bottom economizer after, the front flue gas of air preheater (5) mix after more successively through air preheater (5), first enter pre-duster (6) through the flue gas of air preheater (5) and carry out pre-dedusting, in the flyash directly isolating 70% ~ 80%, and deliver to grey storehouse a(10) in, remove the flue gas after most of flyash by SO through pre-duster (6) in tail flue gas semi-dry desulphurization system
2absorber (7) right top enters SO
2in absorber (7), simultaneously from SO
2between the upper right quarter of absorber (7) to flue gas inlet point, add the calcium hydroxide breast in water, digester (9), the loop slurry in circulation flow container (8) successively; Milk of lime squeezes into SO by pump
2in absorber (7), be atomized into the absorbent after droplet by atomising device and mix with flue gas and contact, and with the SO in flue gas
2occur chemical reaction finally generate calcium sulfate, in flue gas by SO
2remove; The moisture that in course of reaction, absorbent is brought into is evaporated rapidly, flue-gas temperature reduces, desulfurization reaction product and unemployed absorbent together enter sack cleaner (12) with the particulate form of drying with flue gas and are collected, and flue gas then enters chimney (13) and enters in air after dedusting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310179114.2A CN103239984B (en) | 2013-05-15 | 2013-05-15 | Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310179114.2A CN103239984B (en) | 2013-05-15 | 2013-05-15 | Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103239984A CN103239984A (en) | 2013-08-14 |
| CN103239984B true CN103239984B (en) | 2015-05-06 |
Family
ID=48920072
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310179114.2A Active CN103239984B (en) | 2013-05-15 | 2013-05-15 | Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103239984B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN104896494B (en) * | 2015-06-19 | 2017-07-28 | 山西大学 | A kind of waste-heat recovery device applied to dry desulfurizing process |
| 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 |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1188425A (en) * | 1995-05-16 | 1998-07-22 | 金属股份有限公司 | Process for dry desulphurisation of combustion gas |
| CN1401411A (en) * | 2002-09-17 | 2003-03-12 | 山东大学 | Compound desulfurizing process of circulating fluidized bed boiler |
| CN1442227A (en) * | 2002-03-06 | 2003-09-17 | 国家电站燃烧工程技术研究中心 | Method and system of calcining-circulating fluidized bed desulfur in reaction integration furnace |
| CN202315697U (en) * | 2011-10-28 | 2012-07-11 | 中能东讯新能源科技(大连)有限公司 | Three-segment desulfurizer for boiler of circulating fluidized bed |
| CN202555128U (en) * | 2012-04-13 | 2012-11-28 | 蓝天环保设备工程股份有限公司 | Equipment for desulfurizing in boiler by using semidry process desulfurization ash |
| CN203281221U (en) * | 2013-05-15 | 2013-11-13 | 山西平朔煤矸石发电有限责任公司 | Dry fine continuous desulfurization device for CFB (Circulating fluid bed) boiler |
-
2013
- 2013-05-15 CN CN201310179114.2A patent/CN103239984B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1188425A (en) * | 1995-05-16 | 1998-07-22 | 金属股份有限公司 | Process for dry desulphurisation of combustion gas |
| CN1442227A (en) * | 2002-03-06 | 2003-09-17 | 国家电站燃烧工程技术研究中心 | Method and system of calcining-circulating fluidized bed desulfur in reaction integration furnace |
| CN1401411A (en) * | 2002-09-17 | 2003-03-12 | 山东大学 | Compound desulfurizing process of circulating fluidized bed boiler |
| CN202315697U (en) * | 2011-10-28 | 2012-07-11 | 中能东讯新能源科技(大连)有限公司 | Three-segment desulfurizer for boiler of circulating fluidized bed |
| CN202555128U (en) * | 2012-04-13 | 2012-11-28 | 蓝天环保设备工程股份有限公司 | Equipment for desulfurizing in boiler by using semidry process desulfurization ash |
| CN203281221U (en) * | 2013-05-15 | 2013-11-13 | 山西平朔煤矸石发电有限责任公司 | Dry fine continuous desulfurization device for CFB (Circulating fluid bed) boiler |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103239984A (en) | 2013-08-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104759203B (en) | A kind of fluidized-bed process of directly trapping mineralising carbon dioxide in flue gas and system | |
| CN102179161B (en) | Slurry for desulfuration and denitration of recirculating fluidized bed boiler | |
| CN103453538B (en) | A kind of minimum discharge CFBB with three grades of desulphurization systems | |
| CN204865475U (en) | Coal -fired power plant boiler flue gas desulphurization device | |
| CN203549871U (en) | Novel ultra-low emission circulating fluidized bed boiler | |
| CN108163816B (en) | A kind of charcoal heat-also Primordial Qi coupling reduction SO2The device and method for preparing sulphur | |
| CN101342459A (en) | Exhuast gas desulfurization, recycle and treatment method and apparatus | |
| CN104822433A (en) | Dry processes, apparatuses, compositions and systems for reducing sulfur oxides and HCI | |
| CN108273375A (en) | The hot carbonizer flue gas desulfurization device and technique in vulcanized sodium production | |
| CN205886588U (en) | System for again, utilize desulfurization again with semi -dry desulfurization ash | |
| CN109718660A (en) | Circulating fluidized bed boiler and sulfur method | |
| CN101703886B (en) | Desulfuration method by directly utilizing magnesium slags in circulating fluidized bed boiler | |
| CN105561753A (en) | Novel dry process cement kiln flue gas online desulfurization device and technology | |
| CN103239984B (en) | Dry-process fine continuous desulfurization device and method for CFB (Circulating Fluidized Bed) boiler | |
| CN201427021Y (en) | Flue gas desulfurization device for digestive and circulating fluidized bed | |
| CN103706246B (en) | Flue gas circulating fluidized bed combined desulfurization mercury removal device and method | |
| CN107252624A (en) | The semi-dry desulphurization system and technique of a kind of utilization flyash | |
| CN104941435A (en) | Normal temperature semi-dry method circulating fluidized bed flue gas desulphurization system and method | |
| CN204352726U (en) | Water coal-pulp smoke cleaning system | |
| CN203281221U (en) | Dry fine continuous desulfurization device for CFB (Circulating fluid bed) boiler | |
| CN206295800U (en) | A kind of semi-dry flue gas desulfurization device | |
| CN103446875A (en) | Reinforced desulphurization method and reinforced desulphurization system of desulphurizer for combustion system of circulating fluidized bed | |
| CN105477963A (en) | Coal-fired boiler flue gas environmentally-friendly deep treatment method and apparatus | |
| CN102350211B (en) | Three-stage desulfurization device for circulating fluidized bed boiler | |
| CN202315697U (en) | Three-segment desulfurizer for boiler of circulating fluidized bed |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |