CN105570880A - Bed temperature uniformity improving and ultralow emitting system of circulating fluidized bed boiler - Google Patents
Bed temperature uniformity improving and ultralow emitting system of circulating fluidized bed boiler Download PDFInfo
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- CN105570880A CN105570880A CN201511020882.9A CN201511020882A CN105570880A CN 105570880 A CN105570880 A CN 105570880A CN 201511020882 A CN201511020882 A CN 201511020882A CN 105570880 A CN105570880 A CN 105570880A
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- Prior art keywords
- separator
- central tube
- standard
- upper shell
- inlet flue
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/24—Devices for removal of material from the bed
- F23C10/26—Devices for removal of material from the bed combined with devices for partial reintroduction of material into the bed, e.g. after separation of agglomerated parts
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2206/00—Fluidised bed combustion
- F23C2206/10—Circulating fluidised bed
Abstract
A bed temperature uniformity improving and ultralow emitting system of a circulating fluidized bed boiler is provided with a hearth, standard separator inlet flue ducts, large-flow separator inlet flue ducts, acceleration flow guide bosses, standard center barrels, a large-flow center barrel and a vertical pipe. The resistance matching manner of three separators is adjusted through the above components, the flow deviation and the efficiency deviation among the separators are reduced, the total number of materials separated by the middle separator is increased, the material concentration of the center area of the hearth is increased, and the middle bed temperature is lowered. By means of the system, the original formation concentration of SO2 and NOx can be lowered, the consumption amount of limestone and a denitration reducing agent can be reduced, and low-cost ultralow emitting can be achieved. Meanwhile, the carbon content of ash can be reduced, and the running environmental protection property and economical efficiency of the circulating fluidized bed boiler are improved. The system is suitable for energy conservation and environment protection upgrading and rebuilding of newly-built units and in-service units.
Description
Technical field
The invention belongs to Sector of Cfb Boilers, be specifically related to a kind of Circulating Fluidized Bed Temperature uniformity and improve and minimum discharge system.
Background technology
Separator is one of critical component of CFBB, and its Main Function is separated from air-flow by a large amount of high-temp solid material, sends burner hearth back to, runs with the fast fluidization maintaining burner hearth.Separator type selecting and design are always the important component parts of Circulating fluidized bed boiler design.The CFBB of below 150MW capacitance grade generally arranges 2 separators, and the large circulating fluidized bed boiler of 200MW and 300MW capacitance grade generally arranges 3 separators, as shown in Figure 1.
Large quantity research shows: the asymmetric arrangement of 3 separators can bring the difference of separative efficiency, and then causes ring ash quantity inequality and run difference.The practical operation situation of observer nation's internal circulating fluidized-bed boiler is not difficult to find, comparatively 2 separator circulation fluidized-bed combustion boilers are poor for the operation characteristic of 3 separator circulation fluidized-bed combustion boilers, be embodied in: 1) boiler operatiopn bed temperature is higher, bed temperature deviation large (general middle part bed temperature exceeds both sides bed temperature 30-50 DEG C); 2) ash content carbon is high; 3) a large amount of dust stratification of separator inlet flue ubiquity; 4) NOx and SO
2original discharge concentration high; 5) lime stone and denitrification reducing agent consumption large.
Along with the increasingly stringent of national environmental standard, separator optimization is carried out to large circulating fluidized bed boiler, improve bed temperature uniformity, reduce CFBB SO to greatest extent
2and NO
xoriginal generation concentration, reduces lime stone and denitrification reducing agent consumption, and final stablizing realizes minimum discharge, and raising CFBB being run to the feature of environmental protection and economy is most important.
Summary of the invention
In order to overcome above-mentioned prior art Problems existing, a kind of Circulating Fluidized Bed Temperature uniformity is the object of the present invention is to provide to improve and minimum discharge system, reduce the flow deviation between separator and efficiency variation, increase the material total amount that intermediate separator is separated, improve burner hearth central area material concentration, reduce middle part bed temperature.SO can be reduced by the present invention
2and NO
xoriginal generation concentration, reduce lime stone and denitrification reducing agent consumption, realize the minimum discharge of low cost, can also ash content carbon be reduced simultaneously, improve the feature of environmental protection and the economy of CFBB operation, method is applicable to new-built unit and in-service unit energy-conserving and environment-protective upgrading.
In order to achieve the above object, the present invention adopts following technical scheme:
A kind of Circulating Fluidized Bed Temperature uniformity is improved and minimum discharge system, comprises and is arranged on left side separator A, intermediate separator B on burner hearth 1 and right side separator C;
Described left side separator A comprises left side separator upper shell 5A, the left standard separator inlet flue 2A be communicated with burner hearth 1, flow guiding dummy club 3A is accelerated in the left side being arranged in left standard separator inlet flue 2A and side, separator upper shell 5A boundary, left side, insert the left standard central tube 4A in the separator upper shell 5A of left side, be arranged in the left side separator cone 6A of separator upper shell 5A lower end, left side, be arranged in the left side separator lower shell 7A of separator cone 6A lower end, left side;
Described intermediate separator B comprises intermediate separator upper shell 5B, the large discharge separator inlet flue 2B be communicated with burner hearth 1, be arranged in the middle acceleration flow guiding dummy club 3B of large discharge separator inlet flue 2B and side, intermediate separator upper shell 5B boundary, insert the large discharge central tube 4B in intermediate separator upper shell 5B, be arranged in the intermediate separator cone 6B of intermediate separator upper shell 5B lower end, be arranged in the intermediate separator lower shell 7B of intermediate separator cone 6B lower end;
Described right side separator C comprises right side separator upper shell 5C, the right standard separator inlet flue 2C be communicated with burner hearth 1, flow guiding dummy club 3C is accelerated on the right side being arranged in right standard separator inlet flue 2C and side, separator upper shell 5C boundary, right side, insert the right standard central tube 4C in the separator upper shell 5C of right side, be arranged in the right side separator cone 6C of separator upper shell 5C lower end, right side, be arranged in the right side separator lower shell 7C of separator cone 6C lower end, right side;
The sectional area of described left standard separator inlet flue 2A and right standard separator inlet flue 2C is less than the sectional area of large discharge separator inlet flue 2B, the sectional area that left side accelerates flow guiding dummy club 3A and right side to accelerate flow guiding dummy club 3C is greater than the middle sectional area accelerating flow guiding dummy club 3B, and the velocity of flue gas of left standard separator inlet flue 2A and right standard separator inlet flue 2C is lower than the velocity of flue gas of large discharge separator inlet flue 2B;
The diameter of described left standard central tube 4A and right standard central tube 4C is less than the diameter of large discharge central tube 4B, the insertion depth of left standard central tube 4A and right standard central tube 4C is longer than large discharge central tube 4B, and the velocity of flue gas in left standard central tube 4A and right standard central tube 4C is lower than large discharge central tube 4B;
The overall resistance of described left side separator A and right side separator C is greater than intermediate separator B.
Described left standard separator inlet flue 2A and right standard separator inlet flue 2C inlet area are the 80%-95% of large discharge separator inlet flue 2B inlet area.
The sectional area of described left side acceleration flow guiding dummy club 3A and right side acceleration flow guiding dummy club 3C is 1.05-1.25 times of centre acceleration flow guiding dummy club 3B sectional area, and described left side acceleration flow guiding dummy club 3A, centre acceleration flow guiding dummy club 3B and right side acceleration flow guiding dummy club 3C are built by high-strength fireproof high-abrasive material and form.
The velocity of flue gas of described large discharge separator inlet flue 2B is 20-35ms/, and the velocity of flue gas of described left standard separator inlet flue 2A and right standard separator inlet flue 2C is 16-30ms/.
Described left standard central tube 4A, right standard central tube 4C and large discharge central tube 4B shape are cylindrical shape, truncated cone-shaped or truncated cone; Be arranged in left side separator upper shell 5A, the geometric center of right side separator upper shell 5C and intermediate separator upper shell 5B or arranged off-centre, left standard central tube 4A and right standard central tube 4C lower diameter are less than large discharge central tube 4B lower diameter 100-800mm.
Insertion depth ha and hc of described left standard central tube 4A and right standard central tube 4C is the insertion depth hb of 30% ~ 120%, large discharge central tube 4B of left side separator upper shell 5A cylindrical shell height H a and right side separator upper shell 5C cylindrical shell height H c is respectively 15% ~ 100% of intermediate separator upper shell 5B cylindrical shell height H b.
The overall resistance of described left side separator A and right side separator C is 0.6 ~ 2.6kPa, and the overall resistance of intermediate separator B is 0.4 ~ 2.2kPa.
Compared to the prior art comparatively, the present invention possesses following advantage:
1. this method improves the flow distribution of three separators, significantly improves separative efficiency, optimizes boiler operatiopn operating mode;
2. intermediate separator running resistance is lower, and separative efficiency is higher, effectively eliminates the high-temperature area in burner hearth, reduces SO in boiler smoke
2and NO
xprimary generation, decrease lime stone and denitrification reducing agent consumption;
3. Reconstruction in field short construction period, transformation difficulty is low, and method is applicable to new-built unit and in-service unit energy-conserving and environment-protective transformation.
Accompanying drawing explanation
Fig. 1 is existing large circulating fluidized bed boiler three separator arrangement schematic diagram.
Fig. 2 is three separator arrangement mode schematic diagrames of the present invention.
Fig. 3 is cyclone separator arrangement schematic diagram of the present invention.
Fig. 4 is central tube tube structure schematic diagram of the present invention, Fig. 4 (a) is short cylinder shape central tube, Fig. 4 (b) is oval tubular central tube, and Fig. 4 (c) is truncated cone-shaped central tube, and Fig. 4 (d) is truncated cone central tube.
Fig. 5 is central tube arranged off-centre schematic diagram of the present invention.
Fig. 6 is the application note (before enforcement) of embodiment one.
Fig. 7 is the application note (after implementing) of embodiment one.
Fig. 8 is the application note of embodiment three.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.But it will be appreciated by those skilled in the art that the present invention is not only limited to these detailed description of the invention, any improvement of making on basis of the present invention and change, all within protection scope of the present invention.
Embodiment 1
Certain 300MW grade recycle fluidized-bed combustion boiler, see Fig. 2-Fig. 4, Fig. 6-Fig. 7.
Former design 3 cyclone separator arrangement consistent size, wherein barrel diameter is 8.6m, and the height of gas approach is 8.5m, width is 3.5m, and central tube diameter is 4.2m, and insertion depth is 3.5m, time at full capacity, gas approach flow velocity is 20m/s, actual measurement isolation resistance about 1500Pa.
During boiler operatiopn, average bed temperature is about 940 DEG C, and peak can reach 980 DEG C, and middle part average bed temperature is higher than both sides 40-80 DEG C, and when calcium to sulphur mole ratio is 3 ~ 5, SNCR system EIAJ, NOx emission concentration is 60-90mg/Nm
3, and there is escape ammonia and exceed standard.
Implement technological transformation for this reason, left side separator A and right side separator C is transformed: 1) add left side and accelerate flow guiding dummy club 3A and right side acceleration flow guiding dummy club 3C (in Fig. 7 filled black part); 2) change left standard central tube 4A, right standard central tube 4C into truncated cone by cylindrical shape, central tube lower diameter has 4.2m to be decreased to 3.8m, and insertion depth has 3.5m to be increased to 3.8m; 3) to maintain former design constant for intermediate separator C.
By above-mentioned transformation, boiler average bed temperature is reduced to about 900 DEG C, and peak temperature is reduced to 930 DEG C, and it is 25-30mg/Nm that calcium to sulphur mole ratio is reduced to NOx emission concentration under 2 ~ 3.5, SNCR system EIAJ
3, escape ammonia meets emission request.Actual measurement left and right sides isolation resistance about 1650Pa, intermediate separator resistance is still about 1500Pa.Actual measurement boiler fly ash median is 20-25 μm, and operation conditions and environmental protection characteristic significantly improve.
Embodiment 2
Certain newly-built 720t/h CFBB (200MW grade), see Fig. 2-Fig. 5, this boiler design characteristic comprises: 1) left standard central tube 4A, right standard central tube 4C adopt arranged off-centre; 2) left standard separator inlet flue 2A and right standard separator inlet flue 2C is separately installed with left side and accelerates flow guiding dummy club 3A and right side acceleration flow guiding dummy club 3C, flue gas is 24m/s at left standard separator inlet flue 2A and right standard separator inlet flue 2C tip speed, and flue gas is 26m/s in large discharge separator inlet flue 2B tip speed.
After the operation of this boiler, bed temperature is about 880 DEG C, and NOx original discharge concentration is 90-120mg/Nm
3, by SNCR system, be final NOx emission concentration at ammonia nitrogen than the condition being 0.6 be 20-40mg/Nm
3, meet the technical requirement of national minimum discharge.
Embodiment 3
Certain newly-built 600MW supercritical circulating fluidized bed boiler, see Fig. 2-Fig. 4, Fig. 8, this boiler design has 6 separators, and separator adopts and is arranged symmetrically with, wherein: 1) first, the third, fourth, oneself 4 Membrane Separator Cylinder for CFB Boiler diameters are 8.5m, the height of gas approach is 7.5m, width is 3.8m, and central tube diameter is 4m, and insertion depth is 3.6m, time at full capacity, gas approach flow velocity is 22m/s, design isolation resistance 1450Pa; 2) second, penta 2 Membrane Separator Cylinder for CFB Boiler diameters are 8.8m, and the height of gas approach is 7.5m, and width is 4.0m, and central tube diameter is 4.2m, and insertion depth is 3.8m, and time at full capacity, gas approach flow velocity is 24m/s, design isolation resistance 1350Pa; 3) first, the third, fourth, oneself 4 separators are provided with acceleration flow guiding dummy club, and second, penta 2 separators do not arrange acceleration flow guiding dummy club.
Claims (7)
1. Circulating Fluidized Bed Temperature uniformity is improved and a minimum discharge system, it is characterized in that: comprise the left side separator (A) be arranged on burner hearth (1), intermediate separator (B) and right side separator (C);
Described left side separator (A) comprises left side separator upper shell (5A), the left standard separator inlet flue (2A) be communicated with burner hearth (1), flow guiding dummy club (3A) is accelerated in the left side being arranged in left standard separator inlet flue (2A) and left side separator upper shell (5A) side, boundary, insert the left standard central tube (4A) in left side separator upper shell (5A), be arranged in the left side separator cone (6A) of separator upper shell (5A) lower end, left side, be arranged in left side separator lower shell (7A) of separator cone (6A) lower end, left side,
Described intermediate separator (B) comprises intermediate separator upper shell (5B), the large discharge separator inlet flue (2B) be communicated with burner hearth (1), be arranged in middle acceleration flow guiding dummy club (3B) of large discharge separator inlet flue (2B) and intermediate separator upper shell (5B) side, boundary, insert the large discharge central tube (4B) in intermediate separator upper shell (5B), be arranged in the intermediate separator cone (6B) of intermediate separator upper shell (5B) lower end, be arranged in the intermediate separator lower shell (7B) of intermediate separator cone (6B) lower end,
Described right side separator (C) comprises right side separator upper shell (5C), the right standard separator inlet flue (2C) be communicated with burner hearth (1), flow guiding dummy club (3C) is accelerated on the right side being arranged in right standard separator inlet flue (2C) and right side separator upper shell (5C) side, boundary, insert the right standard central tube (4C) in right side separator upper shell (5C), be arranged in the right side separator cone (6C) of separator upper shell (5C) lower end, right side, be arranged in right side separator lower shell (7C) of separator cone (6C) lower end, right side,
The sectional area of described left standard separator inlet flue (2A) and right standard separator inlet flue (2C) is less than the sectional area of large discharge separator inlet flue (2B), the sectional area that left side accelerates flow guiding dummy club (3A) and right side to accelerate flow guiding dummy club (3C) is greater than the sectional area of middle acceleration flow guiding dummy club (3B), and the velocity of flue gas of left standard separator inlet flue (2A) and right standard separator inlet flue (2C) is lower than the velocity of flue gas of large discharge separator inlet flue (2B);
The diameter of described left standard central tube (4A) and right standard central tube (4C) is less than the diameter of large discharge central tube (4B), the insertion depth of left standard central tube (4A) and right standard central tube (4C) is longer than large discharge central tube (4B), and the velocity of flue gas in left standard central tube (4A) and right standard central tube (4C) is lower than large discharge central tube (4B);
The overall resistance of described left side separator (A) and right side separator (C) is greater than intermediate separator (B).
2. Circulating Fluidized Bed Temperature uniformity according to claim 1 is improved and minimum discharge system, it is characterized in that: described left standard separator inlet flue (2A) and right standard separator inlet flue (2C) inlet area are the 80%-95% of large discharge separator inlet flue (2B) inlet area.
3. Circulating Fluidized Bed Temperature uniformity according to claim 1 is improved and minimum discharge system, it is characterized in that: the sectional area on described left side acceleration flow guiding dummy club (3A) and right side acceleration flow guiding dummy club (3C) is 1.05-1.25 times of centre acceleration flow guiding dummy club (3B) sectional area, and described left side acceleration flow guiding dummy club (3A), centre acceleration flow guiding dummy club (3B) and right side acceleration flow guiding dummy club (3C) are built by high-strength fireproof high-abrasive material and formed.
4. Circulating Fluidized Bed Temperature uniformity according to claim 1 is improved and minimum discharge system, it is characterized in that: the velocity of flue gas of described large discharge separator inlet flue (2B) is 20-35ms/, the velocity of flue gas of described left standard separator inlet flue (2A) and right standard separator inlet flue (2C) is 16-30ms/.
5. Circulating Fluidized Bed Temperature uniformity according to claim 1 is improved and minimum discharge system, it is characterized in that: described left standard central tube (4A), right standard central tube (4C) and large discharge central tube (4B) shape are cylindrical shape, truncated cone-shaped or truncated cone; Be arranged in left side separator upper shell (5A), the geometric center of right side separator upper shell (5C) and intermediate separator upper shell (5B) or arranged off-centre, left standard central tube (4A) and right standard central tube (4C) lower diameter are less than large discharge central tube (4B) lower diameter 100-800mm.
6. Circulating Fluidized Bed Temperature uniformity according to claim 1 is improved and minimum discharge system, it is characterized in that: insertion depth ha and hc of described left standard central tube (4A) and right standard central tube (4C) is 30% ~ 120%, the insertion depth hb of large discharge central tube (4B) of left side separator upper shell (5A) cylindrical shell height H a and right side separator upper shell (5C) cylindrical shell height H c is respectively 15% ~ 100% of intermediate separator upper shell (5B) cylindrical shell height H b.
7. Circulating Fluidized Bed Temperature uniformity according to claim 1 is improved and minimum discharge system, it is characterized in that: the overall resistance of described left side separator (A) and right side separator (C) is 0.6 ~ 2.6kPa, the overall resistance of intermediate separator (B) is 0.4 ~ 2.2kPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201511020882.9A CN105570880A (en) | 2015-12-30 | 2015-12-30 | Bed temperature uniformity improving and ultralow emitting system of circulating fluidized bed boiler |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201511020882.9A CN105570880A (en) | 2015-12-30 | 2015-12-30 | Bed temperature uniformity improving and ultralow emitting system of circulating fluidized bed boiler |
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|---|---|
| CN105570880A true CN105570880A (en) | 2016-05-11 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201511020882.9A Pending CN105570880A (en) | 2015-12-30 | 2015-12-30 | Bed temperature uniformity improving and ultralow emitting system of circulating fluidized bed boiler |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108317508A (en) * | 2017-12-27 | 2018-07-24 | 北方华锦化学工业股份有限公司 | A kind of cyclone separator of circulating fluidized bed boiler renovation and improving method |
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| CN108317508A (en) * | 2017-12-27 | 2018-07-24 | 北方华锦化学工业股份有限公司 | A kind of cyclone separator of circulating fluidized bed boiler renovation and improving method |
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