CN102191959A - Step recycling method and device of boiler flue gas waste heat - Google Patents
Step recycling method and device of boiler flue gas waste heat Download PDFInfo
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- CN102191959A CN102191959A CN2011100772022A CN201110077202A CN102191959A CN 102191959 A CN102191959 A CN 102191959A CN 2011100772022 A CN2011100772022 A CN 2011100772022A CN 201110077202 A CN201110077202 A CN 201110077202A CN 102191959 A CN102191959 A CN 102191959A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 121
- 239000003546 flue gas Substances 0.000 title claims abstract description 121
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000002918 waste heat Substances 0.000 title claims abstract description 28
- 238000004064 recycling Methods 0.000 title abstract 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 91
- 230000004888 barrier function Effects 0.000 claims description 104
- 230000008676 import Effects 0.000 claims description 42
- 238000006477 desulfuration reaction Methods 0.000 claims description 31
- 239000003517 fume Substances 0.000 claims description 31
- 230000023556 desulfurization Effects 0.000 claims description 30
- 238000010521 absorption reaction Methods 0.000 claims description 22
- 238000011084 recovery Methods 0.000 claims description 22
- 230000007246 mechanism Effects 0.000 claims description 10
- 239000002253 acid Substances 0.000 claims description 7
- 239000007769 metal material Substances 0.000 claims description 3
- 238000012423 maintenance Methods 0.000 claims description 2
- 230000008569 process Effects 0.000 description 18
- 230000007423 decrease Effects 0.000 description 15
- 239000003245 coal Substances 0.000 description 13
- 230000000694 effects Effects 0.000 description 9
- 238000004458 analytical method Methods 0.000 description 7
- 239000000428 dust Substances 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- 238000010438 heat treatment Methods 0.000 description 7
- 238000013461 design Methods 0.000 description 6
- 239000012716 precipitator Substances 0.000 description 6
- 239000000779 smoke Substances 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 235000019504 cigarettes Nutrition 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 239000002956 ash Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- 238000005530 etching Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 239000003500 flue dust Substances 0.000 description 2
- 239000010881 fly ash Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000013517 stratification Methods 0.000 description 2
- 238000011144 upstream manufacturing 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
- 238000013459 approach Methods 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000411 inducer Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
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Abstract
The invention discloses a step recycling method of boiler flue gas waste heat. The method is used for a steam turbine generator unit, and comprises temperature rise generated by multistage heat exchange and work of parts in a flue gas passage in an energy step reclamation mode. The invention also discloses a boiler flue gas waste heat recycling device for implementing the method. The device comprises multistage heat exchangers, wherein the flue gas sides of the heat exchangers are arranged at different positions in the flue gas passage, and the water sides of the heat exchangers are connected with a low-pressure water supply system of the steam turbine generator unit. According to the method and the device, work energy of equipment such as a draught fan, a booster fan and the like in a flue gas system can be optimally utilized and absorbed, the arrangement is more flexible, and the conventional equipment and the conventional system are affected and changed little.
Description
Technical field
The present invention relates to method and device thereof that a kind of residual heat from boiler fume step is recycled, be used for Turbo-generator Set.
Background technique
Traditional low-pressure coal saver is a kind of conservation measures that utilizes the boiler exhaust gas waste heat.As shown in Figure 1, low-pressure coal saver is a heat exchanger 30, fume side is installed in boiler 10 back-end ductworks, its water side is connected in the low pressure feed water components of system as directed (A, B) of steam turbine, low pressure feed water absorbs smoke exhaust heat in low-pressure coal saver, reduce temperature of exhaust fume, self is heated, returns the steam turbine low-pressure water supply system again behind the elevated temperature, the effect of instead of part low-pressure heater is a constituent element of thermodynamic system of steam tur.Low-pressure coal saver passes through low-pressure heater after low pressure feed water is heated, low pressure feed water after the heating will squeeze the regenerative steam of part steam turbine, under the constant situation of steam turbine throttle flow, the amount of being squeezed of drawing gas is equivalent to return steam turbine from extraction opening, continues expansion working.Therefore, under the constant situation of fuel consumption, can obtain electric power more, improve the Economy of unit.
For traditional coal fired power generation unit that is not equipped with desulphurization system, low-pressure coal saver can be installed between the air preheater and deduster of boiler usually, the waste heat of flue gas is used for heating the low pressure feed water of unit, and feedwater is returned the low-pressure heater system absorb heat in low-pressure coal saver after again.Because the importing of this part flue gas heat has been squeezed the part low pressure (LP) cylinder and has been drawn gas, make steam turbine under the constant situation of low pressure (LP) cylinder steam consumption, produced the electric work of extra increase, produced considerable economic.But bypass is not generally established in boiler flue design, in case fault such as low temperature dewfall, acid etching appear in low-pressure coal saver, fume side cigarette ash stops up or leak will directly threaten the safe operation of unit even causes stopping transport, economic loss is very big.
This traditional arrangement exists following shortcoming:
1. be high dust-laden zone in the middle of air preheater and the deduster, the fly ash content height, with the electrical precipitator is example, its dust removal efficiency calculates according to 99.8%, flue gas flying dust concentration before and after the electrical precipitator differs and reaches 500 times, high fly ash content can aggravate the wearing and tearing of pipeline heating surface, shortens the working life of heat-transfer pipe, and the safety coefficient of equipment decreases.
2. adopt such arrangement, the low-temperature zone of low-pressure coal saver is arranged in the high dust-laden zone of boiler, because of pipe row low temperature dewfall causes the risk of cigarette ash bonding to heighten, after in case this situation occurring, can cause pipe smoke evacuation ash bonding to be stopped up flue resistance is increased greatly, cause boiler load down even forced outage.
3. the low-temperature zone of low-pressure coal saver certainly leads to acid etching if pipe row low temperature dewfall occurs, and perforation is leaked in case pipeline is corroded, and the water of condensation of ejection can become the disaster of electrical precipitator or fiber bag precipitator and blower fan.And the boiler flue design does not consider to be provided with bypass usually, will directly cause the forced outage of unit in case leaking appears in system, and economic loss is very big.
4. be arranged in the low-pressure coal saver in the boiler back end ductwork, can't utilize the acting temperature rise of equipment such as induced draught fan, booster fan in the flue gas downstream thereby cause the waste of heat.
Coal dust can produce a large amount of sulfur dioxide (SO in the boiler internal combustion
2), desulphurization system is mainly to act as to handle SO in the boiler export flue gas
2The device of composition generally is arranged in the boiler flue downstream, mainly is made up of absorption tower, booster fan and the flue gas channel that is associated.Development along with the coal-fired unit desulphurization system of China, occur a kind of new flue gas waste heat recovery again and utilized system, as shown in Figure 2, in this system, heat exchanger 30 is located at the entry position of desulfuration absorbing tower 70, replace the cooling effect of former desulfurization GGH (flue gas heater), flue-gas temperature is reduced to about 80 ℃～90 ℃ enters desulfurizing tower, can reach the requirement of flue gas cool-down, satisfy desulfurized effect, can utilize the acting temperature rise of the waste heat and the equipment such as induced draught fan and booster fan of flue gas again, increase the Economy of unit.But, because the occupation of land of this scheme is bigger, load is heavier, and leeway is big, significantly increase exerting oneself of booster fan.Therefore higher requirement has all been proposed for the installation conditions at scene and the allowance of blower fan.
In fact, no matter be to adopt any in preceding two kinds of schemes, owing to be all with the flue gas waste heat recovery apparatus centralized arrangement, the therefore problem that all exists mounting point, foundation of civil work, steel structure basis, blower fan allowance to have relatively high expectations to the scene.For newly-built unit,, more easily meet the demands comparatively speaking if can just these factors be taken into account and reserve on-the-spot mounting point and equipment allowance in design phase and Plant model selection stage.But for the transformation of old unit, just exist bigger difficulty, equipment such as original flue, steel structure and blower fan are not transformed owing to having enough mounting points and blower fan allowance to have to spend very high cost inadequately.
Therefore, those skilled in the art is devoted to develop the acting temperature rise of equipment such as a kind of induced draught fan that can optimally utilize and absorb flue gas system, booster fan, again can be on arranging more flexibly, to the existing equipment influence with change method and the device thereof that minimum a kind of efficient and safe flue gas waste heat recovery utilizes.
Summary of the invention
Because the above-mentioned defective of prior art, technical problem to be solved by this invention provides the acting temperature rise of equipment such as a kind of induced draught fan that can optimally utilize and absorb flue gas system, booster fan, again can be on arranging more flexibly, to the existing equipment influence with change method and the device thereof that minimum a kind of efficient and safe residual heat from boiler fume is recycled.
For achieving the above object, the invention provides the method that a kind of novel residual heat from boiler fume step is recycled, be used for Turbo-generator Set, comprise through multistage heat exchange, in the mode that energy cascade reclaims, the temperature rise that utilizes the equipment acting in the flue gas channel to produce.
The device that the present invention also provides a kind of residual heat from boiler fume step of preceding method to recycle, comprise multi-stage heat-exchanger, form by a plurality of heat exchangers, the fume side of wherein said heat exchanger is separately positioned on the diverse location in the described flue gas channel, and the water side of described heat exchanger links to each other with the low pressure feed water system of described Turbo-generator Set.
In better embodiment of the present invention, described device comprises boiler, air preheater, deduster, induced draught fan, absorption tower and the chimney that is linked together successively with described flue gas channel; Be arranged on the interior first order heat exchanger of described flue gas channel of described absorption tower inlet, be arranged on the second level heat exchanger in the described flue gas channel between described air preheater and described deduster.Second level heat exchanger in the described flue gas channel also can be arranged in the flue between described deduster and the described induced draught fan.
Further, described device also comprises with described flue gas channel and is connected in booster fan between described induced draught fan and the described absorption tower.
In another better embodiment of the present invention, described device also comprises the bypass flue gas channel that is connected to described chimney from described induced draught fan outlet, be provided with the desulfurization by-pass damper in the described bypass flue gas channel, described booster fan inlet is provided with inlet baffle, and the outlet of described absorption tower is provided with outlet damper; When breaking down, described first order heat exchanger need stop when maintenance labour, by opening described desulfurization by-pass damper, closing described inlet baffle and described outlet damper, comprise that the desulphurization system of described first order heat exchanger is excised from described Turbo-generator Set.
In another better embodiment of the present invention, described device also comprises the inter-stage heat exchanger that is arranged between described induced draught fan and described booster fan.
In another better embodiment of the present invention, the water side pipes at different levels road coupled in series of described heat exchanger.
Further, also comprise the bypass mechanism corresponding respectively in the device of the present invention with each grade of described heat exchanger; Described bypass mechanism and described heat exchanger link to each other with described low pressure feed water system; When any one-level in the described heat exchanger broke down, described bypass mechanism should be excised from described device by the described heat exchanger of level.
Further, described bypass mechanism comprise the outlet barrier valve of the water intake import barrier valve that is arranged on described heat exchanger water side, described heat exchanger water side water outlet, with described water intake and the direct coupled bypass water pipe of described water outlet be arranged on bypass barrier valve on the described bypass water pipe; When any one-level in the described heat exchanger breaks down, by opening corresponding described bypass barrier valve, close described import barrier valve and described outlet barrier valve, described bypass mechanism should be excised from described device by the described heat exchanger of level.
In another better embodiment of the present invention, described Turbo-generator Set also comprises the desulfurization zone, the described heat exchanger of one-level at least in the described multi-stage heat-exchanger is arranged in the described flue gas channel in the described desulfurization zone, the described heat exchanger of one-level at least in the described multi-stage heat-exchanger is arranged between the described air preheater and described deduster of flue gas channel of described boiler tail, perhaps is arranged between the described deduster and described induced draught fan of flue gas channel of described boiler tail.
In order farthest to reduce flue gas resistance, improve heat exchange efficiency and to reduce manufacture cost, the heat exchanger in this programme adopts the common metal material, adopts the fin tube form in the selection of cast.
For the cold end corrosion of anti-locking apparatus, guarantee the long-term safety operation of equipment, the heat exchanger water side entering water temp in this programme should be higher than the acid dew-point temperature of flue gas.
In another better embodiment of the present invention, described deduster is an electrical precipitator.
The technique effect that the present invention has many other flue gas waste heat recoveries to utilize system not possess:
1. can more effectively utilize the acting temperature rise of equipment such as induced draught fan, booster fan in the flue gas downstream.
2. the high temperature section with heat exchanger is arranged in the flue of boiler induced-draft fan inlet upstream, because this place's heat exchange temperature is higher, no dewfall risk has effectively been avoided the problem that pipe row dust stratification blocks and acid etching is leaked that causes because of the low temperature dewfall.
The low-temperature zone of heat exchanger is arranged in booster fan is exported to low dust-containing area between desulfurizing tower, just in case the water of acid dew-point temperature occurring being lower than enters or occurs that sulphur content exceeds standard in the flue gas, cause into water side pipe row dewfall,, reduce greatly so pipe row dust stratification blocks risk because of this place's dust contained flue gas rate is extremely low.In addition, leak,, have no security risk because of the fume side downstream is a desulfurizing tower just in case corrosion occurs.In addition, this grade heat exchanger is furnished with the bypass of water side, can be with the excision separately of this level.And, also can excise desulphurization system so that this grade heat exchanger is overhauled if desulphurization system has disposed gas bypass.
3. adopt after the hierarchical arrangement mode, the heat exchanger that is in induced draught fan inlet Upstream section absorbs that the cigarette temperature drop is low after the flue gas heat, flue gas flow rate reduces, flue gas resistance becomes quadratic relationship to reduce with flow velocity.If flue-gas temperature reduces about 20 degree, flue gas volume and flow velocity will descend about 5% synchronously, and it is about 10% that the allowance of induced draught fan and booster fan is released, like this, and can the corresponding heat exchange areas of arranging more.In addition, if this grade heat exchanger is arranged in the flue between air preheater and the deduster, though the increase of smoke content can increase the wear rate (this can suitably increase the heat exchanger wall thickness and solve) of heat exchanger in the flue gas, but the ratio resistance that flue-gas temperature decline causes and the synchronous reduction of flue gas flow rate will be improved the dust removal efficiency of electrical precipitator.Flue dust frequently clashes into the heat exchanger wall in addition, and the laminar flow boundary layer of meeting disarrangement device wall surface improves heat exchanger cigarette side heat exchange efficiency, and simultaneously, the physics heat of flue dust self also will be partially recovered.
4. from the configuration of system, because the temperature levels of boiler exhaust gas waste heat is lower, heat transfer temperature difference is little, cause the bulky of heat exchanger in the one-level formula arrangement in the past, foundation of civil work and steel structure load cost are very high, the fume side resistance is very big in addition, need induced draught fan or booster fan to bear separately, this requirement to induced draught fan or booster fan is very high.And when carrying out Plant reconstruction plant modernization, can bring a large amount of surcharges owing to the blower fan surplus more ventilating fan of having to inadequately.And heat-exchanger rig is divided into two-stage or multistage cloth postpone, under the constant situation of heat exchanger total capacity, the fume side resistance is distributed into two-part and is born by induced draught fan and booster fan respectively, induced draught fan and booster fan all have certain surplus to be released in addition, so it is general all within the type selecting margin range of blower fan, do not need more ventilating fan, reduced reforming cost greatly.In addition, because after volume, the weight of hierarchical arrangement equipment all reduces, on-the-spot location arrangements more flexibly, the civil engineering cost reduces greatly.
5. from the Security of operation, the Security of hierarchical arrangement is the highest.Each level can be excised from system one by one, but also single-stage excision.Any one-level in the heat exchanger in the boiler back end ductwork and the heat exchanger of desulfurization duct is if fault all can be excised from system respectively, and operation is independent of each other between every grade.After one-level was wherein stopped transport, one-level can also normal operation reclaim flue gas heat in addition, not only can not cause the stoppage in transit of unit, still can also produce economic benefit.And, all system all must be stopped transport in case any all faults occur for the scheme of preceding two kinds of prior aries.
6. on engineering cost, two kinds of traditional centralized arrangement patterns are applicable to newly-built unit.Be to newly-built unit and transform the characteristics that unit all has flexible arrangement and adopt after the mentality of designing of the present invention, because weight, volume and the resistance of each grade all reduce greatly, general all within the scope that original blower fan and flue can bear, do not need existing equipment is made amendment, so investment cost reduces greatly.
Be described further below with reference to the technique effect of accompanying drawing, to understand purpose of the present invention, feature and effect fully design of the present invention, concrete structure and generation.
Description of drawings
Fig. 1 is the working principle schematic representation of a kind of traditional low-pressure coal saver of prior art;
Fig. 2 is the working principle schematic representation of a kind of desulfurization fume exhaust heat recovery system of prior art;
Fig. 3 is the working principle schematic representation of a preferred embodiment of the present invention;
Fig. 4 is the heat exchange efficiency analysis chart of prior art shown in Figure 1;
Fig. 5 is the heat exchange efficiency analysis chart of prior art shown in Figure 2;
Fig. 6 is a heat exchange efficiency analysis chart embodiment illustrated in fig. 3 of the present invention;
Fig. 7 is the working principle schematic representation of specific embodiments embodiment illustrated in fig. 3;
Fig. 8 is the working principle schematic representation of second preferred embodiment of the present invention;
Fig. 9 is the working principle schematic representation of the 3rd preferred embodiment of the present invention;
Figure 10 is the working principle schematic representation of the 4th preferred embodiment of the present invention;
Figure 11 is the working principle schematic representation of the 5th preferred embodiment of the present invention.
Embodiment
In general, along with the difference in season, boiler export flue gas temperature of exhaust fume after passing through deduster, induced draught fan, booster fan one by one can raise about 5 ℃-10 ℃.With the summer is example, temperature rise can reach near 10 ℃, this part heat is very considerable, because the flue gas temperature difference that can utilize from boiler exhaust gas UTILIZATION OF VESIDUAL HEAT IN angle only also has only 40-50 ℃, this a part of temperature rise has increased 5-10 ℃ on the basis of the original temperature difference, that is to say the available heat that has increased 10%-20%.
Explain this principle from the angle of heat transfer temperature difference, can be with reference to the heat exchange efficiency analysis of figure 4-6, t represents fluid temperature variations among the figure, X represents the heat exchanger distance.What Fig. 4 represented is that traditional low-pressure coal saver absorbs flue gas heat in boiler back end ductwork, and flue-gas temperature descends gradually, the process that feed temperature rises gradually.Fig. 5 is the heat exchange efficiency analysis that is arranged on the flue gas waste heat recovery device in the desulfurization duct in the prior art.Smoke absorption after the acting energy of induced draught fan and booster fan temperature risen 10 ℃, therefore the heat transfer temperature difference of inducer is increased to Δ t '+10 ℃ by original Δ t ', the area of dash area increases among the figure, therefore adopt the good effect of heat exchange of second kind of scheme in first kind of scheme, the equipment caloric receptivity also increases thereupon, and economic benefit is more considerable.
The arrangement of device of the present invention such as Fig. 3 make full use of the ladder grade of energy, and traditional flue gas waste heat recovery apparatus is divided into two to be placed on respectively in boiler back end ductwork and the desulfurization duct.After second level heat exchanger 32 absorbs the part of smoke heat earlier, enter desulfurization duct after deduster 40, induced draught fan 50 and booster fan 60 intensifications of flue gas through the downstream, arrange first order heat exchanger 31, continue the low pressure feed water of heating unit again.Such layout can be utilized the flue gas temperature rise greatly, absorbs more heats.Fig. 6 has represented heat exchange efficiency analysis of the present invention.From heat exchange efficiency, the area of dash area after the heat exchanger surface integration two stage arrangement there has been tangible increase, tangible steppedly increases has suddenly appearred in heat transfer temperature difference, and this illustrates that the third scheme has made full use of the temperature rise of flue gas, and further optimization has been arranged on the heat exchange effect relatively.
Mix the first order and the second level exists an optimal proportion at the branch of heat exchange area in theory, can make the heat exchange effect reach optimum, and how the ratio of two-stage distributes not significant limitation in implementation process, can be definite after concrete calculating according to conditions such as the allowance of the execution conditions at scene, civil engineering load, flue-gas temperature level, feed temperature levels.
Certainly, also can same heat exchange area be divided into three grades of layouts according to the position at scene, for example increase the one-level residual neat recovering system again in the inlet flue duct of induced draught fan outlet and booster fan, every grade volume and weight is littler like this, arranges more flexible.
In theory, can heat exchanger be divided into many more grades, heat is carried out cascade utilization according to the temperature levels of flue gas.
In various embodiments of the present invention, the water side pipe road of a plurality of heat exchangers is cascaded up, constitute multi-stage heat-exchanger.The cascade system in the water side pipe road of a plurality of heat exchangers can adopt series connection, also can adopt parallel connection, or the series parallel connection combination.
In order farthest to reduce flue gas resistance, improve heat exchange efficiency and to reduce manufacture cost, heat exchanger can adopt the common metal material, can adopt the fin tube form in the selection of cast.
For the cold end corrosion of anti-locking apparatus, guarantee the long-term safety operation of equipment, the entering water temp of first order heat exchanger water side should be higher than the acid dew-point temperature of flue gas.
Specific embodiment 1:
As shown in Figure 7, flue gas waste heat recovery apparatus is divided into two stage arrangement in boiler back end ductwork and desulfurization duct.Wherein first order heat exchanger 31 is arranged between desulphurization system booster fan 60 and the absorption tower 70, and second level heat exchanger 32 is arranged between air preheater 20 outlets and deduster 40 imports of boiler back end ductwork.
In the desulfurization zone, also comprise the bypass flue gas channel that is connected to chimney 80 from induced draught fan 50 outlets, be provided with desulfurization by-pass damper 84 in the bypass flue gas channel, booster fan 60 ingress are provided with inlet baffle 82, and 70 outlet ports, absorption tower are provided with outlet damper 86; When miscellaneous part breaks down in first order heat exchanger 31 or the desulfurization zone, to open desulfurization by-pass damper 84, close inlet baffle 82 and outlet damper 86, the bypass flue gas channel can will comprise the desulphurization system excision of first order heat exchanger 31.
The flow process of fume side is as follows in the flue gas waste heat recovery apparatus: the flue gas that boiler 10 is discharged enters in the second level heat exchanger 32 of flue gas waste heat recovery device through behind the air preheater 20, do work through deduster 40, induced draught fan 50 and booster fan 60 behind the release portion heat, flue-gas temperature obtains 5 ℃-10 ℃ raising, enters into that the first order heat exchanger 31 that is arranged in the desulfurization duct further reduces temperature after discharge on absorption tower 70, outlet damper 86, chimney 80 again.Desulfurization by-pass damper 84 is a closed condition when normal operation, when breaking down appears in first order heat exchanger 31, can close outlet damper 86, opens desulfurization by-pass damper 84 with desulphurization system excision operation.
The flow process of water side is as follows in the flue gas waste heat recovery apparatus: open the first order import barrier valve 311 and first order outlet barrier valve 312, close first order bypass barrier valve 313, the unit low pressure feed water enters in the first order heat exchanger 31 from import A, along with flue-gas temperature decline self temperature constantly raises, enter into second level heat exchanger 32 inlets through first order outlet barrier valve 312; Open the second level import barrier valve 321 and second level outlet barrier valve 322, close second level bypass barrier valve 323, low pressure feed water enters in the second level heat exchanger 32, along with flue-gas temperature decline self temperature constantly raises, be back to unit low pressure feed water outlet B through second level outlet barrier valve 322.
It more than is the flow process of fume side and water side under the situation of the normal operation of equipment.
When breaking down the needs stoppage in transit as first order heat exchanger 31, the fume side flow process can remain unchanged.Water effluent journey is as follows: close the first order import barrier valve 311 and first order outlet barrier valve 312, open first order bypass barrier valve 313, the unit low pressure feed water directly enters into second level heat exchanger 32 inlets from first order bypass barrier valve 313, without first order heat exchanger 31; Open the second level import barrier valve 321 and second level outlet barrier valve 322, close second level bypass barrier valve 323, low pressure feed water enters in the second level heat exchanger 32, along with flue-gas temperature decline self temperature constantly raises, be back to unit low pressure feed water outlet B through second level outlet barrier valve 322.
When breaking down the needs stoppage in transit as second level heat exchanger 32, the fume side flow process remains unchanged.Water effluent journey is as follows: open the first order import barrier valve 311 and first order outlet barrier valve 312, close first order bypass barrier valve 313, the unit low pressure feed water enters in the first order heat exchanger 31, along with flue-gas temperature decline self temperature constantly raises, enter into second level heat exchanger 32 inlets through first order outlet barrier valve 312; Close the second level import barrier valve 321 and second level outlet barrier valve 322, open second level bypass barrier valve 323, low pressure feed water after the first order heating directly enters into the outlet of unit low pressure feed water from second level bypass barrier valve 323, without second level heat exchanger 32;
Break down when all needing to stop transport as first order heat exchanger 31, second level heat exchanger 32, the fume side flow process still can remain unchanged.Water effluent journey is as follows: close the first order import barrier valve 311 and first order outlet barrier valve 312, open first order bypass barrier valve 313, close the second level import barrier valve 321 and second level outlet barrier valve 322, open second level bypass barrier valve 323, unit low pressure feed water import A directly flows back into unit low pressure feed water outlet B from first order bypass barrier valve 313 and second level bypass barrier valve 323, without first order heat exchanger 31 and second level heat exchanger 32.
According to above operation, can be implemented in the free switching mutually between the two-stage heat exchanger, do not influence the normal operation of unit.
Specific embodiment 2:
As shown in Figure 8, along with country improves constantly the requirement of environmental protection facility, the main trend of development after the desulphurization system of fired power generating unit is not equipped with bypass and has become, thinking of the present invention is suitable for equally and is not equipped with on the unit of desulfurization bypass.
Flue gas waste heat recovery apparatus is to be divided into two stage arrangement in the flue and desulfurization duct of boiler 10 afterbodys equally.Wherein first order heat exchanger 31 is arranged between desulphurization system booster fan and the absorption tower, and second level heat exchanger 32 is arranged between the air preheater outlet and deduster import of boiler back end ductwork.
The flow process of the fume side of flue gas waste heat recovery apparatus is as follows: the flue gas that boiler 10 is discharged is through air preheater 20, after entering second level heat exchanger 32 interior release portion heats, through induced draught fan 50 and booster fan 60 actings, flue-gas temperature obtains 5 ℃-10 ℃ raising, enters into that the first order heat exchanger 31 that is arranged in the desulfurization duct further reduces temperature after discharge on absorption tower 70, outlet damper 86, chimney 80 again.
The water effluent journey and first embodiment are just the same, repeat no more here.
Specific embodiment 3:
As shown in Figure 9, flue gas waste heat recovery apparatus is divided into three grades and is arranged in boiler back end ductwork and the desulfurization duct.Wherein first order heat exchanger 31 is arranged between desulphurization system booster fan 60 and the absorption tower 70, second level heat exchanger 32 is arranged between air preheater 20 outlets and deduster 40 imports of boiler back end ductwork, increased inter-stage heat exchanger 33, be arranged in the flue between the import of induced draught fan 50 outlet and booster fan 60.
The flow process of fume side is as follows in the flue gas waste heat recovery apparatus: the flue gas that boiler 10 is discharged is through behind the air preheater 20, enter release portion heat in the second level heat exchanger 32, pass through deduster 40 then, induced draught fan 50 actings, flue-gas temperature obtains 2 ℃-5 ℃ raising, enter into and be arranged between induced draught fan 50 outlet and booster fan 60 imports in the inter-stage heat exchanger 33 in the flue, do work through booster fan 70 after the release heat, flue-gas temperature obtains 2 ℃-5 ℃ raising again and enters into the first order heat exchanger 31 that is arranged in the desulfurization duct, and a step is reduced temperature after absorption tower 70 again, outlet damper 86, chimney 80 is discharged.
The flow process of water side is as follows in the flue gas waste heat recovery apparatus: open the first order import barrier valve 311 and first order outlet barrier valve 312, close first order bypass barrier valve 313, the unit low pressure feed water enters in the first order heat exchanger 31 from import A, along with flue-gas temperature decline self temperature constantly raises, enter into inter-stage heat exchanger 33 inlets through first order outlet barrier valve 312; Open intergrade import barrier valve 331 and intergrade outlet barrier valve 332, close intergrade bypass barrier valve 333, low pressure feed water enters in the inter-stage heat exchanger 33, along with flue-gas temperature decline self temperature constantly raises, enter into second level heat exchanger 32 inlets through intergrade outlet barrier valve 332.Open the second level import barrier valve 321 and second level outlet barrier valve 322, close second level bypass barrier valve 323, low pressure feed water enters in the second level heat exchanger 32, along with flue-gas temperature decline self temperature constantly raises, be back to unit low pressure feed water outlet B through second level outlet barrier valve 322.
It more than is the flow process of fume side and water side under the situation of the normal operation of equipment.
When breaking down the needs stoppage in transit as first order heat exchanger 31, the fume side flow process remains unchanged.Water effluent journey is as follows: close the first order import barrier valve 311 and first order outlet barrier valve 312, open first order bypass barrier valve 313, the unit low pressure feed water directly enters into inter-stage heat exchanger 33 inlets from import A through first order bypass barrier valve 313, without first order heat exchanger 31; Open intergrade import barrier valve 331 and intergrade outlet barrier valve 332, close intergrade bypass barrier valve 333, low pressure feed water enters in the inter-stage heat exchanger 33, along with flue-gas temperature decline self temperature constantly raises, enter into second level heat exchanger 32 inlets through intergrade outlet barrier valve 332.Open the second level import barrier valve 321 and second level outlet barrier valve 322, close second level bypass barrier valve 323, low pressure feed water enters in the second level heat exchanger 32, along with flue-gas temperature decline self temperature constantly raises, be back to unit low pressure feed water outlet B through second level outlet barrier valve 322.
When breaking down the needs stoppage in transit as second level heat exchanger 32, the fume side flow process remains unchanged.Water effluent journey is as follows: open the first order import barrier valve 311 and first order outlet barrier valve 312, close first order bypass barrier valve 313, the unit low pressure feed water enters in the first order heat exchanger 31 from import A, along with flue-gas temperature decline self temperature constantly raises, enter into inter-stage heat exchanger 33 inlets through first order outlet barrier valve 312; Open intergrade import barrier valve 331 and intergrade outlet barrier valve 332, close intergrade bypass barrier valve 333, the unit low pressure feed water enters in the first order heat exchanger 31, along with flue-gas temperature decline self temperature constantly raises, enter into second level heat exchanger 32 inlets through intergrade outlet barrier valve 332; Close the second level import barrier valve 321 and second level outlet barrier valve 322, open second level bypass barrier valve 323, low pressure feed water after the intergrade heating directly enters into unit low pressure feed water outlet B from second level bypass barrier valve 323, without second level heat exchanger 32.
When breaking down the needs stoppage in transit as inter-stage heat exchanger 33, the fume side flow process remains unchanged.Water effluent journey is as follows: open the first order import barrier valve 311 and first order outlet barrier valve 312, close first order bypass barrier valve 313, the unit low pressure feed water enters in the first order heat exchanger 31 from import A, along with flue-gas temperature decline self temperature constantly raises, enter into inter-stage heat exchanger 33 inlets through first order outlet barrier valve 312; Close intergrade import barrier valve 331 and intergrade outlet barrier valve 332, open intergrade bypass barrier valve 333, low pressure feed water after the first order heating directly enters 32 imports of second level heat exchanger from intergrade bypass barrier valve 333, without inter-stage heat exchanger 33; Open the second level import barrier valve 321 and second level outlet barrier valve 322, close second level bypass barrier valve 323, low pressure feed water enters in the second level heat exchanger 32, along with flue-gas temperature decline self temperature constantly raises, be back to unit low pressure feed water outlet B through second level outlet barrier valve 322.
Break down when all needing to stop transport as first order heat exchanger 31, second level heat exchanger 32, inter-stage heat exchanger 33, the fume side flow process remains unchanged.Water effluent journey is as follows: close the first order import barrier valve 311 and first order outlet barrier valve 312, open first order bypass barrier valve 313, close the second level import barrier valve 321 and second level outlet barrier valve 322, open second level bypass barrier valve 323, close intergrade import barrier valve 331 and intergrade outlet barrier valve 332, open intergrade bypass barrier valve 333, the unit low pressure feed water from import A directly from first order bypass barrier valve 313, intergrade bypass barrier valve 333, second level bypass barrier valve 323 flows back into unit low pressure feed water outlet B, without first order heat exchanger 31, second level heat exchanger 32 and inter-stage heat exchanger 33.
By the operation of valve, any freedom that can be implemented between the three-stage heat exchanger is switched mutually, does not influence the normal operation of unit.
Specific embodiment 4:
As shown in figure 10, induced draught fan 50 and booster fan 60 are merged when designing for part of generating units, this programme equally also is suitable for.
Flue gas waste heat recovery apparatus is divided into two stage arrangement in boiler 10 back-end ductworks and desulfurization duct.Wherein the first order is arranged in the gas approach of desulphurization system absorption tower, and the second level is arranged between the air preheater outlet and deduster import of boiler back end ductwork.
The fume side flow process of flue gas waste heat recovery apparatus is as follows: the flue gas that boiler 10 is discharged is through entering into release portion heat in the second level heat exchanger 32 behind the air preheater 20, then through deduster 40, induced draught fan 50 actings, flue-gas temperature obtains 5 ℃-10 ℃ raising, enters into that the first order heat exchanger 31 that is arranged in the desulfurization duct further reduces temperature after discharge on absorption tower 70, outlet damper 86, chimney 80 again.
The water effluent journey and first embodiment are just the same, repeat no more here.
Specific embodiment 5:
As shown in figure 11, for part of generating units, can consider also that when engineering design second level heat exchanger 32 with flue gas waste heat recovery apparatus is arranged between the import of the outlet of deduster 40 of boiler back end ductwork and induced draught fan 50.
The flow process of the fume side of flue gas waste heat recovery apparatus is as follows: the flue gas that boiler 10 is discharged passes through air preheater 20 successively, after deduster 40 enters second level heat exchanger 32 interior release portion heats, through induced draught fan 50 and booster fan 60 actings, flue-gas temperature obtains 5 ℃-10 ℃ raising, enters into that the first order heat exchanger 31 that is arranged in the desulfurization duct further reduces temperature after discharge on absorption tower 70, outlet damper 86, chimney 80 again.
The water effluent journey and first embodiment are just the same, repeat no more here.
Thinking of the present invention is to make full use of flue gas acting temperature rise through equipment such as induced draught fans, booster fan in the boiler back end ductwork downstream, and the thinking of utilizing energy cascade to reclaim is divided into two-stage or three grades with flue gas waste heat recovery apparatus and reclaims flue gas heat respectively.Meanwhile, had on-the-spot arrangement convenience again concurrently, the surplus of induced draught fan, booster fan such as is necessarily discharged at a series of advantages.Therefore, be that the scheme of having utilized flue gas through this part heat of temperature rise of induced draught fan, booster fan heat exchanger classification (not limiting progression) to be arranged all should be included within the thinking of the present invention in every case.
More than describe preferred embodiment of the present invention in detail.The ordinary skill that should be appreciated that related domain need not creative work and just can design according to the present invention make many modifications and variations.Therefore, all technician in the art all should be in the determined protection domain by claims under this invention's idea on the basis of existing technology by the available technological scheme of logical analysis, reasoning, or a limited experiment.
Claims (13)
1. the method that the residual heat from boiler fume step is recycled is used for Turbo-generator Set, it is characterized in that, through multistage heat exchange, comes recovery waste heat in the mode that energy cascade reclaims, thereby the temperature rise that the parts acting in the flue gas channel is produced can be utilized.
2. device that the residual heat from boiler fume step of realizing the method for claim 1 is recycled, it is characterized in that, comprise multi-stage heat-exchanger, described multi-stage heat-exchanger is made up of a plurality of heat exchangers, the fume side of wherein said heat exchanger is separately positioned on the diverse location in the described flue gas channel, and the water side of described heat exchanger all links to each other with the low pressure feed water system of described Turbo-generator Set.
3. device as claimed in claim 2, wherein said device also comprise boiler, air preheater, deduster, induced draught fan, absorption tower and the chimney that is linked together successively by described flue gas channel; First order heat exchanger is arranged in the described flue gas channel of ingress, described absorption tower, and second level heat exchanger is arranged in the described flue gas channel between described air preheater and described deduster.
4. device as claimed in claim 2, wherein said device also comprise boiler, air preheater, deduster, induced draught fan, absorption tower and the chimney that is linked together successively with described flue gas channel; First order heat exchanger is arranged in the described flue gas channel of ingress on described absorption tower, and second level heat exchanger is arranged in the described flue gas channel between described deduster and described induced draught fan.
5. as claim 3 or 4 described devices, wherein said device also comprises by described flue gas channel and is connected in booster fan between described induced draught fan and the described absorption tower.
6. device as claimed in claim 5, wherein said device also comprises the bypass flue gas channel that is connected to described chimney from the outlet of described induced draught fan, be provided with the desulfurization by-pass damper in the described bypass flue gas channel, the ingress of described booster fan is provided with inlet baffle, and the outlet port on described absorption tower is provided with outlet damper; When breaking down, described first order heat exchanger need stop when maintenance labour, by opening described desulfurization by-pass damper, closing described inlet baffle and described outlet damper, the described first order heat exchanger that is provided with in the flue gas channel with desulphurization system and described desulphurization system excises from described Turbo-generator Set together.
7. device as claimed in claim 5, wherein said device also comprise the inter-stage heat exchanger that is arranged between described induced draught fan and the described booster fan.
8. device as claimed in claim 5, the water side pipes at different levels road coupled in series of wherein said multi-stage heat-exchanger.
9. device as claimed in claim 8 wherein also comprises the bypass mechanism corresponding respectively with each grade of described multi-stage heat-exchanger; The described bypass mechanism described heat exchanger corresponding with it links to each other with described low pressure feed water system; When any one-level in the described multi-stage heat-exchanger breaks down, the described heat exchanger of this level can be excised from described device corresponding to the described bypass mechanism of this grade.
10. device as claimed in claim 9, wherein said bypass mechanism comprise the outlet barrier valve of the water side water outlet of the import barrier valve of the water side water intake that is arranged on described heat exchanger, described heat exchanger, with described water side water intake and the direct coupled bypass water pipe of described water side water outlet be arranged on bypass barrier valve on the described bypass water pipe; When any one-level in the described multi-stage heat-exchanger broke down, by opening corresponding described bypass barrier valve, closing described import barrier valve and described outlet barrier valve, described bypass mechanism should be excised from described device by the described heat exchanger of level.
11. device as claimed in claim 8, wherein said Turbo-generator Set also comprises the desulfurization zone, the described heat exchanger of one-level at least in the described multi-stage heat-exchanger is arranged in the described flue gas channel in the described desulfurization zone, and the described heat exchanger of one-level at least in the described multi-stage heat-exchanger is arranged in the flue gas channel between described air preheater and the described induced draught fan.
12. device as claimed in claim 2, wherein said heat exchanger adopt metallic material to make, the cast of described heat exchanger adopts the fin tube form.
13. as claim 3 or 4 described devices, the entering water temp of the water side of wherein said first order heat exchanger is higher than the acid dew-point temperature of flue gas.
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| CN2011100772022A CN102191959A (en) | 2011-03-29 | 2011-03-29 | Step recycling method and device of boiler flue gas waste heat |
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| CN2011100772022A CN102191959A (en) | 2011-03-29 | 2011-03-29 | Step recycling method and device of boiler flue gas waste heat |
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| CN105464729A (en) * | 2016-01-07 | 2016-04-06 | 上海维尔泰克螺杆机械有限公司 | Smoke and hot fluid waste heat recycling system |
| CN111664430A (en) * | 2020-06-18 | 2020-09-15 | 江苏永钢集团有限公司 | Industrial flue gas heat energy recycling device and method |
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| CN115540575A (en) * | 2022-09-19 | 2022-12-30 | 安徽正刚新能源科技有限公司 | Salicylic acid flash drying system |
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Application publication date: 20110921 |