CN202692016U - Flue gas waste heat recovery system for concurrent boiler - Google Patents
Flue gas waste heat recovery system for concurrent boiler Download PDFInfo
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- CN202692016U CN202692016U CN 201220327646 CN201220327646U CN202692016U CN 202692016 U CN202692016 U CN 202692016U CN 201220327646 CN201220327646 CN 201220327646 CN 201220327646 U CN201220327646 U CN 201220327646U CN 202692016 U CN202692016 U CN 202692016U
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Abstract
The utility model discloses a flue gas waste heat recovery system for a concurrent boiler. The flue gas waste heat recovery system comprises a first heat exchanger and a second heat exchanger, the first heat exchanger is arranged on a high-temperature side of a flue and comprises a heat absorption section and a heat release section, wherein the heat absorption section and the heat release section are connected to form a circulating loop through a first pipeline, and the heat absorption section is arranged in the flue. The second heat exchanger is arranged on a low-temperature side of the flue and comprises an inlet header and an outlet header of a second pipeline, the first heat exchanger and the second heat exchanger are connected through a third pipeline, the heat release section of the first heat exchanger is arranged in the third pipeline, and media to be heated flow into the third pipeline, enter the second heat exchanger through the inlet header of the second heat exchanger and flow out through the outlet header of the second heat exchanger. By the aid of the flue gas waste heat recovery system, the temperature of flue gas can be reduced to be lower, boiler flue gas waste heat energy-saving recovery space is greatly enlarged, the temperature of the boiler flue gas entering a desulfurization and dust removal device is reduced, and the operating cost of the desulfurization and dust removal device is saved.
Description
Technical field
The utility model belongs to the energy environment protection field, relates to specifically a kind of downflow type residual heat from boiler fume recovery system.
Background technology
The fuel of the present most boilers of China or take coal as main wherein contains the S element, so that contain sour gas in the flue gas of boiler emission, their were understood with the form of gaseous state each heating surface of boiler of flowing through when cigarette temperature was high after burning.When the cigarette temperature is lower than a certain temperature, their can with flue gas in steam be combined into sulfuric acid and corrode heat transmission equipment.Cold end corrosion appears in the low economizer of the cold junction of boiler air preheater and feed temperature usually.When the temperature of heating surface was lower than the dew point of flue gas, the sulfuric acid that the sulfur trioxide that generates behind the steam in the flue gas and the coal combustion (the just seldom part of the fuel Products of sulphur) is combined into can condense on the heating surface heavy corrosion heating surface.Reveal corrosion for the acid of avoiding heated surface at the end of boiler, the exhaust gas temperature design is higher usually, and about 140 ℃ of new boilers tended to up to 160 ℃ after operation a period of time.
In order to reach the discharge standard of national environmental protection regulation, reduce acid rain and form harm, this a part of flue gas must be processed through desulfurization, namely removes the sour gas such as SO2, SO3 in the flue gas; Dry and wet state in sweetening process can be divided into desulfur technology again wet method, dry method and half-dried (half is wet) method by absorbent and desulfurization product.Wet technique is desulfurization and processing desulfurization product under wet condition with the solution that contains absorbent or slurries, this method has that desulphurization reaction speed is fast, equipment is simple, the desulfuration efficiency advantages of higher, therefore no matter be large-scale electricity generation boiler, or mediumand smallscale industrial boilers, leading position all occupied.
Known to aforementioned, general 140 ~ 160 ℃ of the smoke evacuation of boiler, for improving desulfuration efficiency and protection desulfurizing tower equipment of itself, can be to the boiler smoke that the enters desulfurizing tower processing of lowering the temperature during desulfurization, generally be down to below 60 ℃, flue-gas temperature is down to 60 ℃ from 140 ~ 160 ℃, has not only wasted a large amount of fume afterheats, and improves the desulfurization operation cost; Reclaim this part fume afterheat, reduce the flue-gas temperature that enters desulfurizing tower, with it equipment economical operation, environmental protection and energy saving are all of great advantage.
Common way is the feedwater of reclaiming this part fume afterheat heating boiler, and we know into the water general flow of boiler is that first desalination is softening, again deoxygenation, and then the process economizer is to boiler; The feedwater of fume afterheat heating boiler namely refers to add the desalination demineralized water of heat abstraction oxygen; For the general industry boiler, desalination demineralized water temperature is environment temperature, about 25 ℃, changes with variation of ambient temperature; If directly take this part demineralized water cooling pan kiln gas Mist heat recovering, can make the heat exchanger wall surface temperature that contacts with flue gas excessively low, cause the sour gas dewfall in the flue gas to corrode heat transmission equipment in the heat exchanger wall.Domestic technology for reclaiming this part fume afterheat is mainly: the mature technologies such as low-pressure coal saver, heat exchange of heat pipe and phase-change heat-exchanger are arranged.
Low-pressure coal saver technology main object on the reduction exhaust gas temperature is the boiler of domestic big-and-middle-sized power plant, it is installed in the boiler back end ductwork, utilize the condensate water of the low-pressure heater water side in the Steam Turbine Regenerative System but not high-pressure feed water comes cooled flue gas, its heat transfer boundary condition is similar to economizer, but the pressure of water side is well below the pressure of economizer, therefore claim its low-pressure coal saver.The installation of low-pressure coal saver is so that the steam turbine heat-exchange system obtains a heat credit, saved the part gas that draws gas, and well reclaims heat loss due to exhaust gas, improved the thermal efficiency of full factory.
Heat pipe is to rely on self internal work liquid phase-change to realize the element that conducts heat.Heat pipe can be divided into evaporator section, two parts of condensation segment, when thermal source at evaporator section during to its heat supply, working medium self-heat power heat absorption vaporization becomes steam, and along the center-aisle high velocity stream to the other end, steam is condensed into liquid at condensation segment to steam after low-temperature receiver is emitted latent heat under the effect of pressure reduction; When working medium is evaporated at evaporator section, its gas-liquid interface is recessed, form many meniscus, produce capillary pressure, liquid refrigerant returns again evaporator section under the backflow dynamic action of tube core capillary pressure and gravity etc., continue the heat absorption evaporation, so move in circles, evaporation and the condensation of working medium just constantly are delivered to cold junction to heat from the hot junction.Because heat pipe is to utilize the phase-change heat-exchange of working medium to come transferring heat, so heat pipe has very large heat-transfer capability and heat transfer efficiency.
Phase-change heat-exchanger has been done again further extension on the basis of heat pipe, original hot tube bundle has been done UNICOM, its interior media can be flowed arbitrarily, and the operating pressure of interior media can random adjustment can be discharged the on-condensible gas in the hot tube bundle at any time with the change of load.
Yet above-mentioned three kinds of heat transfer technologies all are to utilize the wall surface temperature of heat transmission equipment to be higher than the acid dew-point temperature of flue gas and to make the equipment acid and alkali reveal corrosion, the factors such as the heat transfer temperature difference of consideration, and the temperature amplitude that therefore reduces flue gas is very little.In recent years along with the extensive use of resistant material, so that there has been further lifting in the temperature drop space.
Publication number is the Chinese utility model application of CN1477333A, be a kind of combined type heat transfer technology, feedwater is preheated by the flue gas cold junction through phase-change heat-exchanger first, pass through again economizer by the direct heat transfer of flue gas hot junction, thereby reach higher heating water temperature, this cold fluid is first through being heated by the flue gas low-temperature section, then the flow direction that flows to the further heating of fume high-temperature section is called reverse-flow, its scope of application is that low temperature cold source---boiler feedwater is less, and the heat of recovery can all utilize to heated feed water; Suppose that the flue gas dew point temperature is 80 ℃, leave certain safe clearance and heat transfer temperature difference, for assurance equipment normally moves, its final exhaust gas temperature is still more than 100 ℃;
Publication number is the Chinese utility model patent of 201844388U, is a kind of reverse-flow flue gas waste heat recovery apparatus, and feedwater through being positioned at the separate type heat pipe exchanger of flue low-temperature zone, then flows to the in-line pipe heat exchanger that is positioned at the flue high temperature section first.
Yet for guaranteeing that the heat exchanger acid and alkali reveals the impact of corrosion, counter-flow heat exchanger has certain requirement to inflow temperature, and it is limited that its flue-gas temperature interval utilizes, and lowers the temperature still not thorough.
The heat exchanger wall surface temperature owing to separating out without sulfuric acid vapor, can be similar to regard as and not corrode heat exchanger during greater than the acid dew-point temperature of flue gas, and above technology and listed patent just are being based on this; Along with the reduction of wall surface temperature, sulfuric acid begins to condense, and is very high owing to sulfuric acid concentration during beginning, the amount of condensing is also few, therefore corrosion rate is not very fast, reduces with wall temperature, condensation number increases, and corrosion is accelerated, and reaches maximum at the following 20-30 of dew-point temperature ℃, temperature reduces again, metal and acid liquid reaction activity decreased, corrosion rate also decreases, when wall surface temperature is lower than flue gas water dew point temperature, a large amount of steam are separated out, and corrosion has increase; The zone that therefore two seriously corrodeds are arranged for flue gas heat-exchange unit: 1, wall temperature is following 20 ~ 30 ℃ of zones of acid dew point; 2, wall temperature is that water dew point is with lower area.
Above technology and listed patent make the wall surface temperature of flue gas heat-exchange unit be higher than the flue gas acid dew point temperature and avoid acid dew etching problem, yet as aforementioned analysis, compared to 160 ℃ of flue-gas temperatures be down to 60 ℃ this can utilize the space, there is the halfway problem of cooling, based on this kind situation, provide the listed solution of the utility model.
The utility model content
The technical problems to be solved in the utility model provides a kind of downflow type residual heat from boiler fume recovery system, the total flow direction of flue gas water is following current, First Heat Exchanger heats first cold water, cold water after preheating goes the heating of the second heat exchanger again, cold water through being heated by the fume high-temperature section, then further heats with the flue gas low-temperature section first like this, and this main-process stream is following current, can control well like this wall temperature of two-stage heat exchanger, can be lower cigarette temperature drop ground.
The utility model is by the following technical solutions:
A kind of downflow type residual heat from boiler fume recovery system, comprise first, second heat exchanger, described First Heat Exchanger is located at the flue high temperature side, comprises endotherm section and heat release section, described endotherm section, heat release section connect into closed circuit by the first pipeline, and described endotherm section is located in the flue; Described the second heat exchanger is located at the flue low temperature side, and described the second heat exchanger comprises inlet header, the outlet header of the second pipeline; Described first, second heat exchanger connects by the 3rd pipeline, the heat release section of described First Heat Exchanger places in the 3rd pipeline, and medium to be heated flows in described the 3rd pipeline that inlet header by the second heat exchanger enters the second heat exchanger and the outlet header by described the second heat exchanger flows out again.
Preferably, described the 3rd pipeline comprises the first branch road, is used for the second branch road of Flow-rate adjustment, the first branch road and the second branch circuit parallel connection, and the heat release section of described First Heat Exchanger places in described the first branch road.
Preferably, the second branch road of described the 3rd pipeline is provided with control valve, and the aperture of described control valve is controlled by control device.
Preferably, connect the endotherm section of described First Heat Exchanger and the first pipeline between the heat release section and be provided with temperature point, this temperature point is delivered to control device with temperature signal.
The utility model mainly comprises the two-stage heat exchanger, is respectively First Heat Exchanger and the second heat exchanger, and wherein First Heat Exchanger is arranged in the high temperature side of flue, first with it heat exchange of flue gas, and the second heat exchanger is arranged in the low temperature side of flue;
Wherein First Heat Exchanger of the present utility model is divided into endotherm section and two parts of heat release section; Endotherm section is installed in the flue behind the boiler dust remover, absorbs the waste heat of the flue gas of flowing through; Endotherm section and heat release section are connected to a closed circuit circulatory system by pipeline, are connected to a circulating pump on the connecting line; Medium is forced circulation water in the pipeline;
The heat release section heating that band heat medium (the low temperature feedwater that namely will heat) removes first First Heat Exchanger wherein is provided with a bypass (i.e. the second branch road), is connected to a control valve in the bypass, regulates the flow of bypass feedwater; The heating of the second heat exchanger is gone in the feedwater that feedwater after the heating and bypass come after converging;
The second heat exchanger of the present utility model is the heat exchanger of economizer formula, is divided into importing and exporting collector and tube bank; First Heat Exchanger heat release section and the second branch road pipeline link to each other with the inlet header of the second heat exchanger, then connect the second heat exchanger tube, the flue gas direct heat transfer that the feedwater that heat is walked in the pipe and pipe is outer; The utility model the second heat exchanger material can be corrosion resisting steel according to the case of implementation, also can be ordinary carbon steel.
Control system of the present utility model mainly comprises a control device and is installed on the temperature point of the forced circulation pump port of export, the temperature signal that temperature point records is passed to control device, control device controls to adjust the aperture of valve according to the temperature signal of gained, realizes regulating the feedwater flow of bypass.
Description of drawings
Fig. 1 is the systematic schematic diagram of the downflow type residual heat from boiler fume recovery system that relates to of the utility model.
Wherein:
The 1-control device; The 2-control valve; 3-First Heat Exchanger heat release section; 4-the second heat exchanger water outlet collector; 5-the second heat exchanger water inlet collector; 6-the second heat exchanger tube; 7-First Heat Exchanger endotherm section; The 8-flue; The 9-temperature point; The 10-forced circulation pump; 11-the first pipeline; 12-the second pipeline; 13-the 3rd pipeline; 14-the first branch road; 15-the second branch road
The specific embodiment
Referring to Fig. 1, the systematic schematic diagram of the downflow type residual heat from boiler fume recovery system that relates to for the utility model.Comprise first, second heat exchanger, described First Heat Exchanger is located at flue 8 high temperature sides, comprises endotherm section 7 and heat release section 3, and described endotherm section 7, heat release section 3 connect into closed circuit by the first pipeline 11, and described endotherm section 7 is located in the flue 8; Described the second heat exchanger is located at flue 8 low temperature sides, and described the second heat exchanger comprises inlet header 5, the outlet header 4 of the second pipeline 12; Described first, second heat exchanger connects by the 3rd pipeline 13, described the 3rd pipeline 13 comprises the first branch road 14, the second branch road 15, the heat release section 3 of establishing described First Heat Exchanger on described the first branch road 14, with heat medium flow through described the first branch road 14, the second branch road 15 converge after inlet header 5 by the second heat exchanger enter the second heat exchanger and flow out by the outlet header 4 of the second heat exchanger again.The second branch road 15 of described the 3rd pipeline 13 is provided with control valve 2, the aperture of described control valve 2 is by control device 1 control, and being provided with temperature point 9 at the endotherm section 7 and the first pipeline 11 between the heat release section 3 that connect described First Heat Exchanger, this temperature point 9 is delivered to control device 1 with temperature signal.Mobile forced circulation water is provided with circulating pump 10 at the first pipeline 11 in the first pipeline 11 of described First Heat Exchanger.And the boiler low-temperature feedwater of all flowing on the first branch road 14 of described the 3rd pipeline 13, the second branch road 15.In addition, the tube bank 6 of described the second heat exchanger is corrosion resisting steel or ordinary carbon steel with the material of flue gas contact portion.
The coupling system flow chart is now set forth enforcement of the present utility model; In order to reduce to a greater degree the flue-gas temperature that enters desulphurization plant, reclaim more fume afterheat; The utility model is divided into First Heat Exchanger and the second heat exchanger; Minute two-stage heat exchange is carried out waste heat recovery to flue gas; The First Heat Exchanger purpose is the low temperature feedwater of preliminary heating boiler, low temperature feedwater after the heating is converged with the feedwater of bypass (i.e. the second branch road 15), then enter in the second economizer formula heat exchanger and flue gas heat exchange, Mist heat recovering reduces the flue-gas temperature that enters desulphurization plant.
For the convenient anticorrosion mechanism of setting forth two heat exchangers of the utility model, now carry out analytic explanation take a certain concrete case: suppose that the exhaust gas temperature behind certain boiler air preheater is 125 ℃, reduce to 120 ℃ through its temperature behind the deduster; The acid dew point of supposing its flue gas is 90 ℃, and the water dew point temperature is 45 ℃; The desalination feed temperature that condensator outlet advances low-pressure heater (or oxygen-eliminating device) is 40 ℃.Before boiler energy-saving was transformed, 120 ℃ of flue gases behind the deduster directly entered cooling, desulfurizing in the desulphurization plant, and then discharging causes very large energy dissipation.
All technology in the technical background and listed patent, only be higher than acid dew-point temperature from the heat exchanger wall surface temperature, flue gas is carried out waste heat recovery, when therefore the flue gas acid dew point temperature is 90 ℃, add the factors such as heat transfer temperature difference, after this reducing energy consumption, its exhaust gas temperature is approximately about 110 ℃, the reducing energy consumption space only has 10 ℃, so the cooling energy-saving returns of investment are not obvious.
The utility model way is minute two heat exchangers, and wherein First Heat Exchanger preheats 40 ℃ of desalination feedwater; First Heat Exchanger is divided into endotherm section 7 and 3 two parts of heat release section, endotherm section 7 absorbs the waste heat of flue gas, it is passed to the forced circulation water of flowing through, recirculated water feeds water 40 ℃ of desalinations of heat transferred in heat release section 3 again, control the flow of bypass desalination feedwater by the aperture of regulating bypass valve 2, indirectly controlled the heat output of First Heat Exchanger heat release section 3, thereby controlled the temperature of forced circulation water in First Heat Exchanger heat release section 3 and endotherm section 7 closed cycles, reached First Heat Exchanger endotherm section 7 and avoided the purpose that corrosion is revealed in acid; As aforesaid all technology, the maximum energy saving space of First Heat Exchanger is about 10 ℃, and its exhaust gas temperature is about about 110 ℃;
Can be heated to a certain temperature to 40 ℃ of partial deionization feedwater like this, by favorably situated heating surface, can be controlled at mixed demineralized water temperature about 45 ℃, if the water dew point temperature of flue gas is 42 ℃, can tune up bypass flow, the heat exchange amount of First Heat Exchanger heat release section 3 is reduced, and the exhaust gas temperature of First Heat Exchanger endotherm section 7 can be higher than (perhaps equaling) 110 ℃ at this moment.
Be about the water dew point temperature 45 C of flue gas by the First Heat Exchanger mixed desalination water temperature of coming, enter in the second economizer formula heat exchanger this moment directly and flue gas heat exchange (should guarantee that the flow media temperature that inlet header 5 by the second heat exchanger enters the second heat exchanger is the water dew point temperature of flue gas), we know that the wall surface temperature of economizer formula heat exchanger and flue gas contact side at this moment is about the temperature of the demineralized water of flowing through+about 5 ℃; Therefore this moment the second heat exchanger wall surface temperature be about 50 ℃, be higher than the water dew point temperature of flue gas, suppose that flue gas is down to 70 ℃, it is 20 ℃ that total caloric receptivity can make the temperature rise of demineralized water, so 65 ℃ of the outlet temperatures of demineralized water; Such the second heat exchanger and the wall surface temperature interval flue gas contact side are 50 ~ 70 ℃, reveal corrosion although avoided near the acid the flue gas water dew point, yet the second heat exchanger part wall temperature may drop on the heavy corrosion zone in following 20 ~ 30 ℃ of zones of acid dew point, adopt corrosion resisting steel for this part second heat exchanger tube 6, perhaps adjust total amount of energy saving, the acid dew point of the concrete model of bonded boiler, flue gas, the combined factors such as water dew point of flue gas are considered in a word, draw optimum energy-saving scheme.
Claims (8)
1. downflow type residual heat from boiler fume recovery system, it is characterized in that comprising first, second heat exchanger, described First Heat Exchanger is located at flue (8) high temperature side, comprise endotherm section (7) and heat release section (3), described endotherm section (7), heat release section (3) connect into closed circuit by the first pipeline (11), and described endotherm section (7) is located in the flue (8); Described the second heat exchanger is located at flue (8) low temperature side, and described the second heat exchanger comprises inlet header (5), the outlet header (4) of the second pipeline (12); Described first, second heat exchanger connects by the 3rd pipeline (13), the heat release section of described First Heat Exchanger (3) places in the 3rd pipeline (13), and medium to be heated flows in described the 3rd pipeline (13) that inlet header (5) by the second heat exchanger enters the second heat exchanger and the outlet header (4) by described the second heat exchanger flows out again.
2. downflow type residual heat from boiler fume recovery system according to claim 1, it is characterized in that: described the 3rd pipeline (13) comprises the first branch road (14), is used for second branch road (15) of Flow-rate adjustment, the first branch road (14) and the second branch road (15) parallel connection, the heat release section of described First Heat Exchanger (3) places in described the first branch road (14).
3. downflow type residual heat from boiler fume recovery system according to claim 2, it is characterized in that: second branch road (15) of described the 3rd pipeline (13) is provided with control valve (2), and the aperture of described control valve (2) is controlled by control device (1).
4. downflow type residual heat from boiler fume recovery system according to claim 3, it is characterized in that: connect the endotherm section (7) of described First Heat Exchanger and the first pipeline (11) between the heat release section (3) and be provided with temperature point (9), this temperature point (9) is delivered to control device (1) with temperature signal.
5. downflow type residual heat from boiler fume recovery system according to claim 1 is characterized in that: mobile forced circulation water in first pipeline (11) of described First Heat Exchanger.
6. downflow type residual heat from boiler fume recovery system according to claim 1 is characterized in that: described medium to be heated is the boiler low-temperature feedwater.
7. downflow type residual heat from boiler fume recovery system according to claim 1 is characterized in that: the tube bank of described the second heat exchanger (6) is corrosion resisting steel with the material of flue gas contact portion.
8. it is characterized in that according to claim 1 or 4 described downflow type residual heat from boiler fume recovery systems: the tube bank of described the second heat exchanger (6) is ordinary carbon steel with the material of flue gas contact portion.
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220327646 CN202692016U (en) | 2012-07-06 | 2012-07-06 | Flue gas waste heat recovery system for concurrent boiler |
| PCT/CN2013/076917 WO2014005476A1 (en) | 2012-07-06 | 2013-06-07 | Flue gas waste heat recovery system for concurrent boiler |
| JP2015518806A JP2015525863A (en) | 2012-07-06 | 2013-06-07 | Co-current boiler flue gas residual heat recovery system |
| US14/578,476 US9476583B2 (en) | 2012-07-06 | 2014-12-21 | Recovery system of waste heat from flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220327646 CN202692016U (en) | 2012-07-06 | 2012-07-06 | Flue gas waste heat recovery system for concurrent boiler |
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| Publication Number | Publication Date |
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| CN202692016U true CN202692016U (en) | 2013-01-23 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220327646 Expired - Fee Related CN202692016U (en) | 2012-07-06 | 2012-07-06 | Flue gas waste heat recovery system for concurrent boiler |
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| Country | Link |
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| CN (1) | CN202692016U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102734787A (en) * | 2012-07-06 | 2012-10-17 | 上海伏波环保设备有限公司 | Concurrent recycling system for boiler smoke afterheat |
| WO2014005476A1 (en) * | 2012-07-06 | 2014-01-09 | 上海伏波环保设备有限公司 | Flue gas waste heat recovery system for concurrent boiler |
| CN108970165A (en) * | 2018-07-06 | 2018-12-11 | 天津博昶节能科技发展有限公司 | A kind of vapour gas separation method |
-
2012
- 2012-07-06 CN CN 201220327646 patent/CN202692016U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102734787A (en) * | 2012-07-06 | 2012-10-17 | 上海伏波环保设备有限公司 | Concurrent recycling system for boiler smoke afterheat |
| WO2014005476A1 (en) * | 2012-07-06 | 2014-01-09 | 上海伏波环保设备有限公司 | Flue gas waste heat recovery system for concurrent boiler |
| CN102734787B (en) * | 2012-07-06 | 2014-10-22 | 上海伏波环保设备有限公司 | Concurrent recycling system for boiler smoke afterheat |
| CN108970165A (en) * | 2018-07-06 | 2018-12-11 | 天津博昶节能科技发展有限公司 | A kind of vapour gas separation method |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130123 Termination date: 20150706 |
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| EXPY | Termination of patent right or utility model |