CN205299496U - Circulating fluidized bed boiler separator of bed temperature homogeneity and minimum discharge structure is improved - Google Patents
Circulating fluidized bed boiler separator of bed temperature homogeneity and minimum discharge structure is improved Download PDFInfo
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- CN205299496U CN205299496U CN201521137265.2U CN201521137265U CN205299496U CN 205299496 U CN205299496 U CN 205299496U CN 201521137265 U CN201521137265 U CN 201521137265U CN 205299496 U CN205299496 U CN 205299496U
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Abstract
The utility model provides a circulating fluidized bed boiler separator of bed temperature homogeneity and minimum discharge structure is improved, be provided with furnace, standard separator entry flue, large -traffic separator entry flue, guide protruding stage accelerates, a standard center section of thick bamboo, a large -traffic center section of thick bamboo and riser, the resistance mode of matcing through three separators of above -mentioned part adjustment, reduce flow deviation and efficiency deviation between the separator, the material total amount of separator separation in the middle of increasing, improve furnace central zone material concentration, reduce the middle part bed temperature, through the utility model discloses can reduce the original formation concentration of SO2 and NOx, reduce lime stone and denitration reductant consumption, realize the minimum discharge of low cost, can also reduce the lime -ash phosphorus content simultaneously, improve circulating fluidized bed boiler operation's the feature of environmental protection and economic nature, the method is applicable to newly -built unit and is using as a servant the energy -concerving and environment -protective upgrading transformation of unit.
Description
Technical field
This utility model belongs to Sector of Cfb Boilers, is specifically related to a kind of circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge.
Background technology
Separator is one of critical component of CFBB, and its Main Function is to be separated from air-flow by a large amount of high-temp solid materials, sends burner hearth back to, and the fast fluidization to maintain burner hearth runs. Separator type selecting and the important component part that design is always 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.
Big quantity research shows: the asymmetric arrangement of 3 separators can bring the difference of separation efficiency, and then cause ring ash quantity uneven and run difference. The practical operation situation of observer nation's internal circulating fluidized-bed boiler it is seen that, relatively 2 separator circulation fluidized-bed combustion boilers are poor for the operation characteristic of 3 separator circulation fluidized-bed combustion boilers, it being embodied in: 1) boiler operatiopn bed temperature is higher, bed temperature deviation big (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 SO2Original discharge concentration high; 5) limestone and denitrification reducing agent consumption are big.
Along with the increasingly stringent of national environmental standard, large circulating fluidized bed boiler is easily separated device structure optimization, improves bed temperature uniformity, reduce CFBB SO to greatest extent2And NOxBeing originally generated concentration, reduce limestone and denitrification reducing agent consumption, finally stably realize minimum discharge, 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, the purpose of this utility model is in that to provide a kind of circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge, reduce the flow deviation between separator and efficiency variation, increase the material total amount that intermediate separator separates, improve burner hearth central area material concentration, reduce middle part bed temperature.SO can be reduced by this utility model2And NOxIt is originally generated concentration, reduce limestone and denitrification reducing agent consumption, it is achieved the minimum discharge of low cost, ash content carbon can also be reduced simultaneously, improving the feature of environmental protection and economy that CFBB runs, method is applicable to new-built unit and in-service unit energy-conserving and environment-protective upgrading.
In order to achieve the above object, this utility model adopts the following technical scheme that
A kind of circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge, including the left side separator A, the intermediate separator B that are arranged on burner hearth 1 and right side separator C;
Described left side separator A includes left side separator upper shell 5A, the left standard separator inlet flue 2A connected 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, it is arranged in the left side separator cone 6A of separator upper shell 5A lower end, left side, is arranged in the left side separator lower shell 7A of separator cone 6A lower end, left side;
Described intermediate separator B includes intermediate separator upper shell 5B, the big traffic separator gas approach 2B connected with burner hearth 1, it is arranged in big traffic separator gas approach 2B and the middle of side, intermediate separator upper shell 5B boundary accelerates flow guiding dummy club 3B, insert the big flow central tube 4B in intermediate separator upper shell 5B, it is arranged in the intermediate separator cone 6B of intermediate separator upper shell 5B lower end, is arranged in the intermediate separator lower shell 7B of intermediate separator cone 6B lower end;
Described right side separator C includes right side separator upper shell 5C, the right standard separator inlet flue 2C connected 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, it is arranged in the right side separator cone 6C of separator upper shell 5C lower end, right side, is 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 the right standard separator inlet flue 2C sectional area less than big traffic separator gas approach 2B, flow guiding dummy club 3A is accelerated in left side and right side is accelerated the sectional area of flow guiding dummy club 3C and accelerated the sectional area of flow guiding dummy club 3B, the velocity of flue gas of left standard separator inlet flue 2A and the right standard separator inlet flue 2C velocity of flue gas lower than big traffic separator gas approach 2B more than centre;
The diameter of described left standard central tube 4A and the right standard central tube 4C diameter less than big flow central tube 4B, the insertion depth of left standard central tube 4A and right standard central tube 4C is longer than big flow central tube 4B, left standard central tube 4A and the velocity of flue gas in right standard central tube 4C lower than big flow central tube 4B;
The overall resistance of described left side separator A and right side separator C is more 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 big traffic separator gas approach 2B inlet area.
It is 1.05-1.25 times of centre acceleration flow guiding dummy club 3B sectional area that the sectional area of flow guiding dummy club 3A and right side acceleration flow guiding dummy club 3C is accelerated in described left side, and flow guiding dummy club 3A, middle acceleration flow guiding dummy club 3B are accelerated in described left side and right side acceleration flow guiding dummy club 3C is built by high-strength fireproof high-abrasive material and forms.
The velocity of flue gas of described big traffic separator gas approach 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 big flow central tube 4B shape are cylindrical shape, truncated cone-shaped or truncated cone; It is 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 less than big flow central tube 4B lower diameter 100-800mm.
Insertion depth ha and the hc of described left standard central tube 4A and right standard central tube 4C is the 30%��120% of left side separator upper shell 5A cylinder height Ha and right side separator upper shell 5C cylinder height Hc respectively, and the insertion depth hb of big flow central tube 4B is the 15%��100% of intermediate separator upper shell 5B cylinder height Hb.
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 relatively, this utility model possesses following advantage:
1. this method improves the flow distribution of three separators, significantly improves separation efficiency, optimizes boiler operatiopn operating mode.
2. intermediate separator running resistance is lower, and separation efficiency is higher, effectively eliminates the high-temperature area in burner hearth, reduces SO in boiler smoke2And NOxPrimary generation, decrease limestone 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 diagrams of the present utility model.
Fig. 3 is cyclone separator arrangement schematic diagram of the present utility model.
Fig. 4 is central tube tube structure schematic diagram of the present utility model, 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 utility model.
Fig. 6 is the application note (before enforcement) of embodiment one.
Fig. 7 is the application note (after enforcement) 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, this utility model is described in further detail. It will be appreciated by those skilled in the art that this utility model is not only limited to these detailed description of the invention, any improvement made on this utility model basis and change, all within protection domain of the present utility model.
Embodiment 1
Certain 300MW grade recycle fluidized-bed combustion boiler, referring to Fig. 2-Fig. 4, Fig. 6-Fig. 7.
Original 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, surveys isolation resistance about 1500Pa.
During boiler operatiopn, average bed temperature is about 940 DEG C, and peak is up to 980 DEG C, and middle part average bed temperature is higher than 40-80 DEG C, both sides, and calcium to sulphur mole ratio is 3��5, and during SNCR system EIAJ, NOx emission concentration is 60-90mg/Nm3, and there is escape ammonia and exceed standard.
Implement technological transformation for this, left side separator A and right side separator C transformed: 1) add left side acceleration flow guiding dummy club 3A and right side acceleration flow guiding dummy club 3C (in Fig. 7 filled black part);2) being changed 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 increase to 3.8m; 3) intermediate separator C remains original design constant.
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 calcium to sulphur mole ratio reduces to 2��3.5, and under SNCR system EIAJ, NOx emission concentration is 25-30mg/Nm3, 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 ��m, and operation conditions and environmental protection characteristic significantly improve.
Embodiment 2
Certain newly-built 720t/h CFBB (200MW grade), referring to Fig. 2-Fig. 5, this boiler design characteristic includes: 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 acceleration 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 big traffic separator gas approach 2B tip speed.
After this boiler is gone into operation, bed temperature is about 880 DEG C, and NOx original discharge concentration is 90-120mg/Nm3, by SNCR system, ammonia nitrogen than be 0.6 condition be final NOx emission concentration be 20-40mg/Nm3, meet the technology requirement of country's minimum discharge.
Embodiment 3
Certain newly-built 600MW supercritical circulating fluidized bed boiler, referring to 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, designs 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, designs isolation resistance 1350Pa; 3) first, the third, fourth, oneself 4 separators are provided with acceleration flow guiding dummy club, and second, penta 2 separators are not provided with accelerating flow guiding dummy club.
Claims (7)
1. the circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge, it is characterised in that: include the left side separator (A), intermediate separator (B) and the right side separator (C) that are arranged on burner hearth (1);
Described left side separator (A) includes left side separator upper shell (5A), left standard separator inlet flue (2A) connected 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), it is arranged in the left side separator cone (6A) of separator upper shell (5A) lower end, left side, it is arranged in left side separator lower shell (7A) of separator cone (6A) lower end, left side,
Described intermediate separator (B) includes intermediate separator upper shell (5B), the big traffic separator gas approach (2B) connected with burner hearth (1), it is arranged in big traffic separator gas approach (2B) and the middle of intermediate separator upper shell (5B) side, boundary accelerates flow guiding dummy club (3B), insert the big flow central tube (4B) in intermediate separator upper shell (5B), it is arranged in the intermediate separator cone (6B) of intermediate separator upper shell (5B) lower end, it is arranged in the intermediate separator lower shell (7B) of intermediate separator cone (6B) lower end,
Described right side separator (C) includes right side separator upper shell (5C), right standard separator inlet flue (2C) connected 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), it is arranged in the right side separator cone (6C) of separator upper shell (5C) lower end, right side, it is 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 big traffic separator gas approach (2B), the sectional area on left side acceleration flow guiding dummy club (3A) and right side acceleration flow guiding dummy club (3C) accelerates the sectional area of flow guiding dummy club (3B) more than centre, 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 big traffic separator gas approach (2B);
The diameter of described left standard central tube (4A) and right standard central tube (4C) is less than the diameter of big flow central tube (4B), the insertion depth of left standard central tube (4A) and right standard central tube (4C) is longer than big flow central tube (4B), left standard central tube (4A) and the velocity of flue gas in right standard central tube (4C) lower than big flow central tube (4B);
The overall resistance of described left side separator (A) and right side separator (C) is more than intermediate separator (B).
2. the circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge according to claim 1, it is characterised in that: described left standard separator inlet flue (2A) and right standard separator inlet flue (2C) inlet area are the 80%-95% of big traffic separator gas approach (2B) inlet area.
3. the circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge according to claim 1, it is characterized in that: it is 1.05-1.25 times of centre acceleration flow guiding dummy club (3B) sectional area that the sectional area on flow guiding dummy club (3A) and right side acceleration flow guiding dummy club (3C) is accelerated in described left side, described left side is accelerated flow guiding dummy club (3A), middle acceleration flow guiding dummy club (3B) and right side acceleration flow guiding dummy club (3C) and is built by high-strength fireproof high-abrasive material and form.
4. the circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge according to claim 1, it is characterized in that: the velocity of flue gas of described big traffic separator gas approach (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/.
5. the circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge according to claim 1, it is characterised in that: described left standard central tube (4A), right standard central tube (4C) and big flow central tube (4B) shape are cylindrical shape, truncated cone-shaped or truncated cone; It is 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 less than big flow central tube (4B) lower diameter 100-800mm.
6. the circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge according to claim 1, it is characterized in that: insertion depth ha and the hc of described left standard central tube (4A) and right standard central tube (4C) is the 30%��120% of left side separator upper shell (5A) cylinder height Ha and right side separator upper shell (5C) cylinder height Hc respectively, and the insertion depth hb of big flow central tube (4B) is the 15%��100% of intermediate separator upper shell (5B) cylinder height Hb.
7. the circulating fluidized bed boiler separator structure improving bed temperature uniformity and minimum discharge according to claim 1, 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.
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| CN201521137265.2U CN205299496U (en) | 2015-12-30 | 2015-12-30 | Circulating fluidized bed boiler separator of bed temperature homogeneity and minimum discharge structure is improved |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105570880A (en) * | 2015-12-30 | 2016-05-11 | 中国华能集团清洁能源技术研究院有限公司 | 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 |
|---|---|---|---|---|
| CN105570880A (en) * | 2015-12-30 | 2016-05-11 | 中国华能集团清洁能源技术研究院有限公司 | Bed temperature uniformity improving and ultralow emitting system of circulating fluidized bed boiler |
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