CN203810393U - Circulating fluidized bed boiler by using integrated transformation technology - Google Patents
Circulating fluidized bed boiler by using integrated transformation technology Download PDFInfo
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- CN203810393U CN203810393U CN201420136403.4U CN201420136403U CN203810393U CN 203810393 U CN203810393 U CN 203810393U CN 201420136403 U CN201420136403 U CN 201420136403U CN 203810393 U CN203810393 U CN 203810393U
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- air port
- separator
- overfire air
- improved
- returning device
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- 230000009466 transformation Effects 0.000 title abstract description 63
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 52
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 49
- 238000009826 distribution Methods 0.000 claims abstract description 26
- 238000001816 cooling Methods 0.000 claims abstract description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003546 flue gas Substances 0.000 claims abstract description 11
- 239000000463 material Substances 0.000 claims description 70
- 239000000839 emulsion Substances 0.000 claims description 27
- 239000002893 slag Substances 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 14
- 238000009418 renovation Methods 0.000 claims description 13
- 239000004744 fabric Substances 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 10
- 239000003082 abrasive agent Substances 0.000 claims description 6
- 230000002787 reinforcement Effects 0.000 claims description 6
- 239000012528 membrane Substances 0.000 claims description 5
- 230000004048 modification Effects 0.000 claims description 5
- 238000012986 modification Methods 0.000 claims description 5
- 238000009991 scouring Methods 0.000 claims description 5
- 229910001220 stainless steel Inorganic materials 0.000 claims description 5
- 239000010935 stainless steel Substances 0.000 claims description 5
- 239000000725 suspension Substances 0.000 claims description 5
- 239000007789 gas Substances 0.000 claims description 4
- 125000006850 spacer group Chemical group 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 abstract description 10
- 235000019738 Limestone Nutrition 0.000 abstract description 8
- 239000006028 limestone Substances 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000002956 ash Substances 0.000 abstract 3
- 239000010882 bottom ash Substances 0.000 abstract 1
- 238000010586 diagram Methods 0.000 description 21
- 239000000428 dust Substances 0.000 description 12
- 230000007613 environmental effect Effects 0.000 description 9
- 239000000446 fuel Substances 0.000 description 5
- 230000005540 biological transmission Effects 0.000 description 4
- 238000005520 cutting process Methods 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- 239000008186 active pharmaceutical agent Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000003134 recirculating effect Effects 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008707 rearrangement Effects 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
Abstract
The utility model discloses a circulating fluidized bed boiler by using an integrated transformation technology. The circulating fluidized bed boiler comprises a transformed screen type heating surface, a transformed return system, a transformed air distribution system, a transformed secondary air nozzle system, a transformed ash residue cooling system and a transformed desulfurizing agent adding system. According to the transformed circulating fluidized bed boiler, the concentration of SO2 and NOx in flue gas is finally reduced to 30-70 percent of that of the boiler before transformation, the concentration of flying ash is reduced to 70-90 percent of that of flying ash before transformation, newly increased equipment is needless, and the operating environment-friendly characteristics of the boiler can be remarkably enhanced. The circulating fluidized bed boiler has the advantages of low investment cost, short transformation cycle, stable boiler operation and the like, the integrated transformation is realized, the problems existing in the original heating surface arrangement, a hood, a separator, a bottom ash cooler and a limestone conveying system of the boiler can be synchronously solved, and the economical efficiency, stability and safety of boiler operation are comprehensively improved.
Description
Technical field
The utility model belongs to CFBB environmental transformation technical field, is specifically related to a kind of CFBB of application continuum renovation technique.
Background technology
Recirculating fluidized bed (Circulating Fluidized Bed, CFB) boiler technology is at home and abroad developed rapidly because of its superior environmental-protecting performance and good fuel tolerance, and heap(ed) capacity has reached the overcritical grade of 600MW.At present, main force's unit of domestic CFB boiler has developed into 300MW, and China has been that the CFB boiler quantity that puts into operation is maximum in the world, the country of installed capacity maximum.Because CFB boiler is short at Chinese Applicative time, what mainly use is inferior fuel, these fuel values are low, sulphur content is high, ash content is high and be difficult to burning, and the flow behavior of himself, combustion process, heat-transfer character are different from conventional pulverized-coal stove, therefore its more problems exposing in design, operation, repair and maintenance, on its feature of environmental protection index particularly Air Pollutant Emission have remarkable impact.
Boiler atmosphere pollution mainly comprises SO
2, NO
xwith dust three parts; for strengthen environmental protection, realize target for energy-saving and emission-reduction; more strict environmental protection standard has been carried out by national environmental protection department; be < < fossil-fuel power plant atmospheric pollutant emission standard > > (GB13223-2011), its discharge standard emission limit compared with 2003 editions significantly tightens up.Recirculating fluidized bed (CFB) boiler is owing to having applied the technology such as furnace sorbent injection desulfurization, low-temperature burning and fractional combustion, and most CFB boilers can directly meet environmental requirement, its SO
2and NO
xconcentration of emission is generally 150～350mg/m
3, dust emission concentration is also lower.But also there are a considerable amount of CFB boiler SO
2and NO
xconcentration of emission slightly exceeds standard, and (30～100mg/m is only above standard
3), under prior art background, the CFB boiler that these slightly exceed standard will be realized SO
2and NO
xqualified discharge, need to install external desulfurzation system and SNCR denitrating system, and this can significantly increase the operating cost of enterprise and the transformation cycle is long, investment of equipment is very big.
Summary of the invention
The problem existing in order to solve above-mentioned prior art, the purpose of this utility model is to provide a kind of CFBB of application continuum renovation technique, can be under the prerequisite of avoiding high equipment investment and operation maintenance to drop into, give full play to the environmental protection characteristic of CFB boiler, meet the requirement of national up-to-date environmental protection standard.
For reaching above object, the utility model adopts following technical scheme:
A CFBB for application continuum renovation technique, comprises improved curtain wall A, improved revert system B, improved cloth wind system C, improved overfire air port system D, improved lime-ash cooling system E and improved desulfurizing agent add-on system F;
Described improved curtain wall A, has increased the length of curtain wall A and has restrained quantity, and improved curtain wall A bottommost is 10～20m apart from the distance of air distribution plate C1; 1～2m region, curtain wall A bottom is coated with curtain wall high-abrasive material A1 completely to prevent airflow scouring wearing and tearing, and curtain wall A outside is provided with the curtain wall reinforcement A2 that prevents its distortion simultaneously;
Described improved revert system B, at separator inlet flue B1, be provided with separator inlet flue guiding device B12, to entering the flue gas of separator, carry out rectification, and central cylinder of separator B4 fixed form and version are transformed, central cylinder of separator B4 top fixed form is that free suspension type is fixed, between central cylinder of separator B4 and Membrane Separator Cylinder for CFB Boiler B2, be freely to coordinate, can relative sliding; Central cylinder of separator B4 structure of modification form adopts bottom barrel dliameter arranged off-centre, and eccentric distance is 100～2000mm, and bottom barrel dliameter is 30～80% of top barrel dliameter;
Described improved cloth wind system C is provided with air compartment flow apron C4 one time in an air compartment C3, is furnished with blast cap C2 on air distribution plate C1, and blast cap C2 is bell-type windshield; The blast cap C2 percent opening of air distribution plate C1 surrounding is higher than central area;
Described improved overfire air port system D, adopt multilayer overfire air port to arrange, arrange that progression is 2 grades or 3 grades, be respectively overfire air port DH and lower overfire air port DL or upper overfire air port DH, middle overfire air port DM and lower overfire air port DL, the Secondary Air of described upper overfire air port DH, middle overfire air port DM and lower overfire air port DL is tilted to down and sends into along the 1 short transverse layering of burner hearth emulsion zone, 5～65 °, its angle of inclination;
Described improved lime-ash cooling system E, the slag cooler E2 of employing is air-water combined slag cooler, utilizes the slag cooler E2 can be by the thin grey loopback burner hearth emulsion zone 1 of a part, the loopback amount of thin ash is total grey quantity of slag 5～30%;
Described improved desulfurizing agent add-on system F is provided with desulfurizing agent and adds a mouthful F2 on material returning device refeed line B10, sends into burner hearth emulsion zone 1 together with the heat ash that desulfurizing agent separates with separator BA.
Described improved revert system B, also comprises the flow passage component of material returning device BB is adjusted, and the circulation area of material returning device returning charge chamber B7 is 1.5～3 times of circulation area of the loosening chamber B5 of material returning device; Between the loosening air compartment B6 of material returning device returning charge air compartment B8 and material returning device, be provided with material returning device air compartment baffle B9, answer between the loosening chamber B5 of material returning device returning charge chamber B7 and material returning device and be provided with material returning device upper spacer B11, to tackle the increase of material outside circulation amount.
Described improved revert system B, is also included in central cylinder of separator B4 inside deflector B13 in central cylinder of separator is installed.
Described improved desulfurizing agent add-on system F, also comprise that desulfurizing agent adopts pneumatic conveying mode, conveying source of the gas is compressed air, the desulfurizing agent using is lime stone, carbide slag or high calcium-containing material, in desulfurizing agent, CaO content is more than 52%, desulfurizing agent average grain diameter is 150～750 μ m, and maximum particle diameter is less than 2.0mm.
Described central cylinder of separator B4 is heat-resistance stainless steel, wall thickness 5～25mm.
The resistance of described bell-type windshield is 2.5～5.5kPa, and spacing is each other 100～400mm.
Symmetry or asymmetric arrangement between described upper overfire air port DH, middle overfire air port DM and lower overfire air port DL, under the bottom, overfire air port DL is positioned at air distribution plate C1 top 400～1600mm, and the air quantity of described upper overfire air port DH, middle overfire air port DM and lower overfire air port DL all can independently regulate.
2 covers are set described desulfurizing agent add-on system F or more than 2 covers, wherein having 1 cover system at least is back-up system.
Compared to the prior art, tool has the following advantages the utility model:
1. can synchronously reduce SO in boiler smoke
2, NO
xwith the concentration of emission of dust, the fume emission of improved boiler can meet national up-to-date environmental protection standard requirement, obvious environment benefit.
2. avoided the high equipment investment of newly-increased external desulfurzation system and SNCR denitrating system, land occupation not, the transformation cycle is short, risk is little.
3. transform not newly added equipment, do not increase the repair and maintenance workload of existing equipment, without newly-increased personnel, can not increase operating cost.
4. when carrying out integrated transformation, can synchronously solve the existing problems such as the existing heating surface layout of boiler, blast cap, separator, slag cooler and lime stone handling system, improve economy, stability and the security of boiler operatiopn comprehensively.
Accompanying drawing explanation
Fig. 1 is the overall structure schematic diagram before an integrated transformation of CFBB is implemented.
Fig. 2 is the top view before an integrated transformation of CFBB is implemented.
Fig. 3 is the overall structure schematic diagram after an integrated transformation of CFBB is implemented.
Fig. 4 is the top view after an integrated transformation of CFBB is implemented.
Fig. 5 compares schematic diagram before and after curtain wall transformation, and wherein: Fig. 5 a is schematic diagram before curtain wall transformation, Fig. 5 b is schematic diagram after curtain wall transformation.
Fig. 6 is that curtain wall reinforcement installs schematic diagram additional, wherein: Fig. 6 a is schematic diagram after curtain wall transformation, and Fig. 6 b is the local enlarged front view of Fig. 6 a circled, and Fig. 6 c is the top view of Fig. 6 b.
Fig. 7 compares schematic diagram before and after reform of separator, wherein: Fig. 7 a is schematic diagram before reform of separator, and Fig. 7 b is schematic diagram after reform of separator.
Fig. 8 is central cylinder of separator eccentric structure schematic diagram.
Fig. 9 is baffle arrangement schematic diagram in central cylinder of separator, and wherein: Fig. 9 a is front view, Fig. 9 b is top view.
Figure 10 is the free suspension type fixed form of central cylinder of separator schematic diagram.
Figure 11 compares schematic diagram before and after material returning device transformation, and wherein: Figure 11 a is schematic diagram before material returning device transformation, Figure 11 b is schematic diagram after material returning device transformation.
Figure 12 compares schematic diagram before and after blast cap transformation; Wherein, Figure 12 a is schematic diagram before blast cap transformation, and Figure 12 b is schematic diagram after blast cap transformation, and the blast cap C2 percent opening that after transformation, air distribution plate C1 surrounding is used is higher than central area (blast cap shown in circle void).
Figure 13 is overfire air port system layout schematic diagram.
Figure 14 is the overall structure schematic diagram after an integrated transformation part of CFBB is implemented.
In figure:
A---curtain wall B---revert system
C---cloth wind system D---overfire air port system
E---lime-ash cooling system F---desulfurizing agent add-on system
1---burner hearth emulsion zone 2---burner hearth dilute-phase zone
3---coal bunker 4---coal spout
5---back-end ductwork 6---back-end ductwork heating surface
A1---curtain wall high-abrasive material A2---curtain wall reinforcement
BA---separator BB---material returning device
B1---separator inlet flue B2---Membrane Separator Cylinder for CFB Boiler
B3---separator standpipe B4---central cylinder of separator
Material returning device becomes flexible air compartment to B5---material returning device becomes flexible chamber B6---
B7---material returning device returning charge chamber B8---material returning device returning charge air compartment
B9---material returning device air compartment baffle B10---material returning device refeed line
B11---material returning device upper spacer B12---separator inlet flue guiding device
Deflector in B13---central cylinder of separator
C1---air distribution plate C2---blast cap
An air compartment flow apron of C3---an air compartment C4---
The middle overfire air port of DH---upper overfire air port DM---
DL---lower overfire air port DF---returning charge wind
A wind of DS---loosening wind DP---
E1---slag dropping tube E2---slag cooler
E3---slag cooler backwind tube E4---slag cooler scum pipe
E5---roller slag cooler
F1---desulfurizing agent storage warehouse F2---desulfurizing agent adds mouth
The specific embodiment
Below in conjunction with drawings and the specific embodiments, the utility model is described in further detail.
As shown in Figure 3 and Figure 4, the CFBB of a kind of application continuum renovation technique of the utility model, comprises improved curtain wall A, improved revert system B, improved cloth wind system C, improved overfire air port system D, improved lime-ash cooling system E and improved desulfurizing agent add-on system F.
Described improved lime-ash cooling system E, the slag cooler E2 of employing is air-water combined slag cooler, utilizes the slag cooler E2 can be by the thin grey loopback burner hearth emulsion zone 1 of a part, the loopback amount of thin ash is total grey quantity of slag 5～30%; After transformation is implemented, can improve burner hearth middle part differential pressure to 1.5～3.0kPa, improve upper furnace differential pressure to 0.5～1.5kPa.
Described improved desulfurizing agent add-on system F, by desulfurizing agent being added to a mouthful F2, to be arranged on material returning device refeed line B10 upper, sends into burner hearth emulsion zone 1 together with the heat ash that desulfurizing agent separates with separator.Preferably, 2 covers are set described desulfurizing agent add-on system F or more than 2 covers, wherein having 1 cover system at least is back-up system, utilizes and increase the method for system reserve coefficient raising system reliability.Improved desulfurizing agent add-on system F, also comprise that desulfurizing agent adopts pneumatic conveying mode, conveying source of the gas is compressed air, the desulfurizing agent using is lime stone, carbide slag or high calcium-containing material, in desulfurizing agent, CaO content is more than 52%, desulfurizing agent average grain diameter is 150～750 μ m, and maximum particle diameter is less than 2.0mm.
As shown in Figure 5 and Figure 6, improved curtain wall A, the length and the tube bank quantity that have increased curtain wall A realize, and after heating surface rearrangement, its area change, heat-transfer effect are strengthened.Improved curtain wall A bottommost is 10～20m apart from the distance of air distribution plate C1; In 1～2m region, curtain wall A bottom, cover curtain wall high-abrasive material A1 completely to prevent airflow scouring wearing and tearing, in curtain wall A outside, the curtain wall reinforcement A2 that prevents its distortion is installed simultaneously.
As shown in Figure 7, improved revert system B, carries out not adjusting under the integrally-built prerequisite of separator BA, at separator inlet flue B1, separator inlet flue guiding device B12 is set, and to entering the flue gas of separator, carries out rectification.Central cylinder of separator B4 fixed form and version are transformed, and result is to improve separator, and strengthening separator BA, to fine grain capturing ability in flying dust, increases material outside circulation amount.As shown in figure 10, central cylinder of separator B4 top fixed form is that free suspension type is fixed, and between central cylinder of separator B4 and Membrane Separator Cylinder for CFB Boiler B2, is freely to coordinate, can relative sliding; As shown in Figure 8, central cylinder of separator B4 structure of modification form is adopted to bottom barrel dliameter arranged off-centre, eccentric distance is 100～2000mm, and bottom barrel dliameter is 30～80% of top barrel dliameter.Preferably, described central cylinder of separator B4 is heat-resistance stainless steel, wall thickness 5～25mm.
As shown in Figure 9, improved revert system B, is also included in central cylinder of separator B4 inside deflector B13 in central cylinder of separator is installed, and for improving flow field, reduces fine grain carrying secretly.
After central cylinder of separator B4 transformation, improve separator, can avoid the agstone that drops into boiler directly to enter back-end ductwork without separator trapping, single-pass boiler, due to the time lengthening that after transformation, agstone contacts with flue gas, utilization rate increases, and can further improve desulfuration efficiency.
As shown in figure 11, improved revert system B, also comprise the flow passage component of material returning device BB is adjusted, the circulation area of the corresponding material returning device returning charge chamber B7 of material returning device returning charge air compartment B8 is 1.5～3 times of circulation area of the loosening chamber B5 of the corresponding material returning device of the loosening air compartment B6 of material returning device; Between the loosening air compartment B6 of material returning device returning charge air compartment B8 and material returning device, there is material returning device air compartment baffle B9, answer between the loosening chamber B5 of material returning device returning charge chamber B7 and material returning device and have material returning device upper spacer B11, with the increase of reply material outside circulation amount, after transformation, the loosening air quantity of material returning device is reduced to 30%～50% of material returning device returning charge air quantity.
As shown in Figure 3, improved cloth wind system C is provided with air compartment flow apron C4 one time in an air compartment C3, and it is for improving the uniformity of air current flow in an air compartment.As shown in figure 12, arrange blast cap C2 on air distribution plate C1, blast cap C2 is bell-type windshield; For improving air distribution plate flow uniformity, the blast cap C2 percent opening that air distribution plate C1 surrounding is used is higher than central area; Preferably, the resistance of described bell-type windshield is 2.5～5.5kPa, and spacing is each other 100～400mm.
The NO that CFB boiler produces
xmainly fuel type NO
x, control fuel type NO
xgenerating effective measures is air stage feeding burnings.In the time of can being reduced to oepration at full load due to improved critical flow wind transmission amount 25%～40% of primary air flow, and it is 20～40% that run duration primary air flow only accounts for total blast volume ratio, be subject to lack of air impact, in reducing atmosphere, the intermediate product of nitrogen burning can not further be oxidized to NO, is reduced into neutral N
2, and then suppressed NO
xgeneration.Other oxygen amounts of burning required are filled into by Secondary Air, can effectively guarantee efficiency of combustion like this.
As shown in figure 13, improved overfire air port system D, adopt multilayer overfire air port to arrange, be respectively overfire air port DH, middle overfire air port DM and lower overfire air port DL, the layout progression of described upper overfire air port DH, middle overfire air port DM and lower overfire air port DL is more than 2 grades or 2 grades, Secondary Air is tilted to down and sends into along the 1 short transverse layering of burner hearth emulsion zone, 5～65 °, its angle of inclination.Preferably, symmetry or asymmetric arrangement between described upper overfire air port DH, middle overfire air port DM and lower overfire air port DL, under the bottom, overfire air port DL is positioned at air distribution plate C1 top 400～1600mm, and the air quantity of described upper overfire air port DH, middle overfire air port DM and lower overfire air port DL all can independently regulate.
The utility model by above-mentioned transformation after, can reduce average ignition temperature to 800～850 ℃ of burner hearth emulsion zone, improve the temperature homogeneity of burner hearth emulsion zone, the difference of emulsion zone each point temperature can be reduced to average ignition temperature ± 100 ℃.
After transformation, stable operation of the boiler is being suitable for the temperature range of desulfuration in furnace and low NOx drainage, the most at last SO in flue gas
2and NO
xconcentration is reduced to 30%～70% before transformation, and flying dust concentration is reduced to 70%～90% before transformation.While reducing critical flow wind transmission amount to oepration at full load 25%～40% of a wind DP amount, it is 20～40% that wind DP amount of run duration accounts for total blast volume ratio;
After transformation, the separative efficiency of separator BA is increased to more than 99%, reduces flying dust meso-position radius to 15～35 μ m, cutting particle diameter to 60～100 μ m, reduces flying dust share to 20%～50%; The loosening wind DS amount of material returning device BB is reduced to 30%～50% of material returning device returning charge wind DF amount;
By above-mentioned transformation, improve burner hearth middle part differential pressure to 1.5～3.0kPa, improve upper furnace differential pressure to 0.5～1.5kPa.
Embodiment 1:
As Fig. 1～Fig. 4, relate to 1 480t/h CFBB, the boiler before transformation comprises burner hearth emulsion zone 1 and burner hearth dilute-phase zone 2, is provided with each 3 of 6 stove inner screen type heating surface A(left and right side walls in burner hearth dilute-phase zone 2).Burner hearth dilute-phase zone 2 is connected by separator inlet flue B1 with separator BA, totally 2 of separator BA, and the flue gas after separator dedusting is entered and in back-end ductwork 5, is furnished with back-end ductwork heating surface 6, the cooling rear discharge of flue gas by central cylinder of separator B4.
920 ℃ of burner hearth emulsion zone 1 ignition temperatures before transformation, burner hearth emulsion zone 1 each point temperature is 780～1050 ℃, burner hearth middle part differential pressure 1.2kPa, upper furnace differential pressure 0.4kPa, SO in flue gas
2concentration of emission be 350～450mg/m
3, NO
xconcentration of emission be 180～220mg/m
3.Boiler total blast volume is 500000Nm
3/ h, wind DP amount of boiler is 280000Nm
3/ h, blast cap C2 adopts T shape blast cap, and air distribution plate C1 resistance is 2kPa, the cooling employing roller slag cooler of lime-ash E5.Through measuring the separative efficiency of separator BA, be 97.5%, flying dust meso-position radius 55 μ m, cutting particle diameter 120 μ m, flying dust share 55%.Between the loosening air compartment B6 of material returning device returning charge air compartment B8 and material returning device, be interconnected, the loosening wind DS amount of material returning device and material returning device returning charge wind DF amount are by a pipeline co-controlling.The layout progression of overfire air port DH and DL is 2 grades, and bottom overfire air port DL is positioned at the upper 2000mm of air distribution plate C1.The desulfurizing agent of desulfurizing agent add-on system F adds a mouthful F2 and is arranged on overfire air port DH above, and desulfurizing agent add-on system arranges 1 cover, while normally moving, all uses, and the desulfurizing agent of use is the lime stone of CaO purity 50%, limestone particle size 75 μ m.
For reducing SO in boiler smoke
2and NO
xconcentration of emission, boiler is carried out to integrated transformation, concrete transformation comprises:
(1) curtain wall A transformation.Increase by 1 of curtain wall A length 4m and tube bank, its area change 15% after curtain wall A transformation, improved curtain wall A bottommost is 15m apart from the distance of air distribution plate C1, use heating surface high-abrasive material A1 to cover 2m region, curtain wall A bottom completely to prevent airflow scouring wearing and tearing, curtain wall A outside is provided with curtain wall reinforcement A2 for preventing distortion simultaneously.
(2) revert system B transformation.Do not adjust under the integrally-built prerequisite of separator BA and carry out, at separator inlet flue B1, separator inlet flue guiding device B12 is set.Central cylinder of separator B4 top fixed form is that free suspension type is fixed, and between central cylinder of separator B4 and Membrane Separator Cylinder for CFB Boiler B2, is freely to coordinate, can relative sliding.Central cylinder of separator B4 structure of modification form adopts arranged off-centre, and bottom barrel dliameter is 80% of top barrel dliameter, and central cylinder of separator B4 inside is provided with deflector B13 in central cylinder of separator, for improving flow field, reduces fine grain carrying secretly.Central cylinder of separator B4 is heat-resistance stainless steel material, wall thickness 10mm.The corresponding material returning device returning charge of material returning device returning charge air compartment B8 chamber B7 circulation area is adjusted into 2 times of the loosening chamber of the corresponding material returning device of the loosening air compartment B6 of material returning device B5 circulation area; Between the loosening air compartment B6 of material returning device returning charge air compartment B8 and material returning device, set up material returning device air compartment baffle B9, use respectively independently pipeline to control.
(3) cloth wind system C transformation.Air compartment flow apron C4 is installed one time in an air compartment C3, changes the upper blast cap C2 arranging of air distribution plate C1 into bell-shaped by flechette-type, resistance is 5kPa, and blast cap C2 spacing is each other 200mm; The blast cap C2 percent opening that air distribution plate C1 surrounding is used is higher than central area, and improved critical flow wind transmission amount is 60000Nm
3/ h.
(4) overfire air port system D transformation.Overfire air port system D transformation adopts two-layer, cloth is set up overfire air port DH and lower overfire air port DL two-stage overfire air port respectively, along the 1 short transverse layering of burner hearth emulsion zone, be tilted to down and send into, 45 °, the angle of inclination of upper overfire air port DH and lower overfire air port DL, between upper overfire air port DH and lower overfire air port DL, adopt and be arranged symmetrically with, each overfire air port air quantity all can independently regulate, and wherein under the bottom, overfire air port DL is positioned at the upper 800mm of air distribution plate C1.
(5) lime-ash cooling system E transformation.Lime-ash cooling system E transformation transform slag cooler E2 as air-water combined slag cooler, and by thin grey loopback burner hearth emulsion zone 1, thin grey loopback amount be total grey quantity of slag 20%.
(6) desulfurizing agent add-on system F transformation.Desulfurizing agent is added to a mouthful F2 to be arranged on material returning device refeed line B10, together with the heat ash that desulfurizing agent separates with separator, send into burner hearth emulsion zone 1, after desulfurizing agent add-on system F transformation, desulfurizing agent adopts pneumatic conveying mode, conveying source of the gas is compressed air, the desulfurizing agent using is lime stone, desulfurizing agent CaO content is more than 52%, and desulfurizing agent average grain diameter is 250 μ m, and maximum particle diameter is less than 2.0mm.Desulfurizing agent add-on system F arranges 3 covers, and run duration 2 use 1 are standby.
By above transformation, the average ignition temperature to 860 ℃ of burner hearth emulsion zone 1, burner hearth emulsion zone 1 each point temperature is 780～920 ℃, the separative efficiency of separator BA is increased to more than 99.5%, reduce flying dust meso-position radius to 20 μ m, cutting particle diameter to 75 μ m, flying dust share is reduced to 40%, and the loosening wind DS amount of material returning device BB is reduced to 30% of material returning device returning charge wind DF amount.Burner hearth middle part differential pressure is increased to 2.0kPa, improves upper furnace differential pressure to 1.0kPa, and boiler total blast volume is 460000Nm
3/ h, wind DP amount of boiler is 180000Nm
3/ h, SO in flue gas
2concentration of emission be 160～190mg/m
3, NO
xconcentration of emission be 120～180mg/m
3.
Embodiment 2:
Referring to Figure 14, relate to 1 1024t/h CFBB, the boiler before transformation comprises burner hearth emulsion zone 1 and burner hearth dilute-phase zone 2, is provided with each 6 of 12 stove inner screen type heating surface A(left and right side walls in burner hearth dilute-phase zone 2), totally 3 of separator BA.
940 ℃ of burner hearth emulsion zone 1 ignition temperatures before transformation, burner hearth emulsion zone 1 each point temperature is 800～1080 ℃, burner hearth middle part differential pressure 1.5kPa, upper furnace differential pressure 0.6kPa, SO in flue gas
2concentration of emission be 300～500mg/m
3, NO
xconcentration of emission be 210～250mg/m
3.Boiler total blast volume is 950000Nm
3/ h, wind DP amount of boiler is 550000Nm
3/ h, blast cap C2 adopts bell shape blast cap, and air distribution plate C1 resistance is 5kPa, the cooling employing roller slag cooler of lime-ash E5.The layout progression of overfire air port DH and DL is 2 grades, and bottom overfire air port DL is positioned at the upper 1500mm of air distribution plate C1.The desulfurizing agent of desulfurizing agent add-on system F adds a mouthful F2 and is arranged on overfire air port DH above, and desulfurizing agent add-on system arranges 2 covers, while normally moving, all uses, and the desulfurizing agent of use is carbide slag, limestone particle size 100 μ m.
For reducing SO in boiler smoke
2and NO
xconcentration of emission, boiler is carried out to integrated transformation, concrete transformation comprises:
(1) curtain wall A transformation.Increase curtain wall A length 5m, improved curtain wall A bottommost is 18m apart from the distance of air distribution plate C1, uses heating surface high-abrasive material A1 to cover 1.5m region, curtain wall A bottom completely to prevent airflow scouring wearing and tearing.
(2) revert system B transformation.At separator inlet flue B1, separator inlet flue guiding device B12 is set.Central cylinder of separator B4 structure of modification form adopts arranged off-centre, and bottom barrel dliameter is 75% of top barrel dliameter.Central cylinder of separator B4 is heat-resistance stainless steel material, wall thickness 15mm.
(3) cloth wind system C transformation.Air compartment flow apron C4 is installed one time in an air compartment C3, and blast cap does not adjust, and improved critical flow wind transmission amount is 120000Nm
3/ h.
(4) overfire air port system D transformation.Overfire air port system D transformation adopts three layers, cloth is set up overfire air port DH, middle overfire air port DM and tri-grades of overfire air ports of lower overfire air port DL respectively, along the 1 short transverse layering of burner hearth emulsion zone, be tilted to down and send into, 30 °, the angle of inclination of upper overfire air port DH, middle overfire air port DM and lower overfire air port DL, between upper overfire air port DH, middle overfire air port DM and lower overfire air port DL, adopt asymmetric arrangement, each overfire air port air quantity all can independently regulate, and wherein under the bottom, overfire air port DL is positioned at the upper 800mm of air distribution plate C1.
(5) lime-ash cooling system E does not transform.
(6) desulfurizing agent add-on system F transformation.Desulfurizing agent is added to a mouthful F2 and be arranged on material returning device refeed line B10 above, set up 1 cover desulfurizing agent add-on system F after transformation, run duration 2 use 1 are standby.
By above transformation, the average ignition temperature to 880 ℃ of burner hearth emulsion zone 1, burner hearth emulsion zone 1 each point temperature is 800～940 ℃, the separative efficiency of separator BA is increased to more than 99%, reduces flying dust meso-position radius to 25 μ m, cutting particle diameter to 80 μ m.SO in boiler smoke
2concentration of emission be 150～180mg/m
3, NO
xconcentration of emission be 160～190mg/m
3.
The description of above embodiment is comparatively concrete; but can not therefore be interpreted as the restriction to the utility model scope; for the person of ordinary skill of the art; without departing from the concept of the premise utility; some distortion and the improvement made, these all belong to protection domain of the present utility model.
Claims (8)
1. a CFBB for application continuum renovation technique, is characterized in that: comprise improved curtain wall (A), improved revert system (B), improved cloth wind system (C), improved overfire air port system (D), improved lime-ash cooling system (E) and improved desulfurizing agent add-on system (F);
Described improved curtain wall (A), has increased the length of curtain wall (A) and has restrained quantity, and improved curtain wall (A) bottommost is 10～20m apart from the distance of air distribution plate (C1); 1～2m region, curtain wall (A) bottom is coated with curtain wall high-abrasive material (A1) completely to prevent airflow scouring wearing and tearing, and curtain wall (A) outside is provided with the curtain wall reinforcement (A2) that prevents its distortion simultaneously;
Described improved revert system (B), at separator inlet flue (B1), be provided with separator inlet flue guiding device (B12), to entering the flue gas of separator, carry out rectification, and central cylinder of separator (B4) fixed form and version are transformed, central cylinder of separator (B4) top fixed form is that free suspension type is fixed, between central cylinder of separator (B4) and Membrane Separator Cylinder for CFB Boiler (B2), be freely to coordinate, can relative sliding; Central cylinder of separator (B4) structure of modification form adopts bottom barrel dliameter arranged off-centre, and eccentric distance is 100～2000mm, and bottom barrel dliameter is 30～80% of top barrel dliameter;
Described improved cloth wind system (C) is provided with an air compartment flow apron (C4) in an air compartment (C3), is furnished with blast cap (C2) on air distribution plate (C1), and blast cap (C2) is bell-type windshield; Blast cap (C2) percent opening of air distribution plate (C1) surrounding is higher than central area;
Described improved overfire air port system (D), adopt multilayer overfire air port to arrange, arrange that progression is 2 grades or 3 grades, be respectively overfire air port (DH) and lower overfire air port (DL) or upper overfire air port (DH), middle overfire air port (DM) and lower overfire air port (DL), the Secondary Air of described upper overfire air port (DH), middle overfire air port (DM) and lower overfire air port (DL) is tilted to down and sends into along burner hearth emulsion zone (1) short transverse layering, 5～65 °, its angle of inclination;
Described improved lime-ash cooling system (E), the slag cooler (E2) adopting is air-water combined slag cooler, utilize the slag cooler (E2) can be by the thin grey loopback burner hearth emulsion zone of a part (1), the loopback amount of thin ash be total grey quantity of slag 5～30%;
Described improved desulfurizing agent add-on system (F) is provided with desulfurizing agent and adds mouthful (F2) on material returning device refeed line (B10), sends into burner hearth emulsion zone (1) together with the heat ash that desulfurizing agent separates with separator.
2. the CFBB of a kind of application continuum renovation technique according to claim 1, it is characterized in that: described improved revert system (B), also comprise the flow passage component of material returning device (BB) is adjusted, the circulation area of material returning device returning charge chamber (B7) is 1.5～3 times of the loosening chamber (B5) of material returning device circulation area; Between the loosening air compartment (B6) of material returning device returning charge air compartment (B8) and material returning device, be provided with material returning device air compartment baffle (B9), answer between the loosening chamber (B5) of material returning device returning charge chamber (B7) and material returning device and be provided with material returning device upper spacer (B11), to tackle the increase of material outside circulation amount.
3. the CFBB of a kind of application continuum renovation technique according to claim 1, it is characterized in that: described improved revert system (B), is also included in central cylinder of separator (B4) inside deflector (B13) in central cylinder of separator is installed.
4. the CFBB of a kind of application continuum renovation technique according to claim 1, it is characterized in that: described improved desulfurizing agent add-on system (F), also comprise that desulfurizing agent adopts pneumatic conveying mode, conveying source of the gas is compressed air, desulfurizing agent average grain diameter is 150～750 μ m, and maximum particle diameter is less than 2.0mm.
5. the CFBB of a kind of application continuum renovation technique according to claim 1, is characterized in that: described central cylinder of separator (B4) is heat-resistance stainless steel, wall thickness 5～25mm.
6. the CFBB of a kind of application continuum renovation technique according to claim 1, is characterized in that: the resistance of described bell-type windshield is 2.5～5.5kPa, and spacing is each other 100～400mm.
7. the CFBB of a kind of application continuum renovation technique according to claim 1, it is characterized in that: symmetry or asymmetric arrangement between described upper overfire air port (DH), middle overfire air port (DM) and lower overfire air port (DL), overfire air port under the bottom (DL) is positioned at air distribution plate (C1) top 400～1600mm, and the air quantity of described upper overfire air port (DH), middle overfire air port (DM) and lower overfire air port (DL) all can independently regulate.
8. the CFBB of a kind of application continuum renovation technique according to claim 1, is characterized in that: 2 covers are set described desulfurizing agent add-on system (F) or more than 2 covers, wherein having 1 cover system at least is back-up system.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420136403.4U CN203810393U (en) | 2014-03-24 | 2014-03-24 | Circulating fluidized bed boiler by using integrated transformation technology |
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|---|---|---|---|
| CN201420136403.4U CN203810393U (en) | 2014-03-24 | 2014-03-24 | Circulating fluidized bed boiler by using integrated transformation technology |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104279556A (en) * | 2014-09-30 | 2015-01-14 | 东方电气集团东方锅炉股份有限公司 | Secondary air distribution method for circulating fluidized bed boiler |
| CN106979514A (en) * | 2017-05-27 | 2017-07-25 | 贵州新能源开发投资股份有限公司 | A kind of sunken bed ballast group fluid bed and its application method for using super-low calorific value fuel |
| CN117053185A (en) * | 2023-06-21 | 2023-11-14 | 西安交通大学 | Transformation system for fire-pressing peak-shaving of circulating fluidized bed boiler |
-
2014
- 2014-03-24 CN CN201420136403.4U patent/CN203810393U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104279556A (en) * | 2014-09-30 | 2015-01-14 | 东方电气集团东方锅炉股份有限公司 | Secondary air distribution method for circulating fluidized bed boiler |
| CN106979514A (en) * | 2017-05-27 | 2017-07-25 | 贵州新能源开发投资股份有限公司 | A kind of sunken bed ballast group fluid bed and its application method for using super-low calorific value fuel |
| CN117053185A (en) * | 2023-06-21 | 2023-11-14 | 西安交通大学 | Transformation system for fire-pressing peak-shaving of circulating fluidized bed boiler |
| CN117053185B (en) * | 2023-06-21 | 2024-04-09 | 西安交通大学 | Transformation system for fire-pressing peak-shaving of circulating fluidized bed boiler |
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