CN106123014A - Film-type evaporation phase-change heat-exchange air preheater - Google Patents
Film-type evaporation phase-change heat-exchange air preheater Download PDFInfo
- Publication number
- CN106123014A CN106123014A CN201610739161.1A CN201610739161A CN106123014A CN 106123014 A CN106123014 A CN 106123014A CN 201610739161 A CN201610739161 A CN 201610739161A CN 106123014 A CN106123014 A CN 106123014A
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- Prior art keywords
- evaporator section
- temperature
- heat exchange
- film
- micro mist
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Links
- 238000001704 evaporation Methods 0.000 title claims abstract description 12
- 230000008020 evaporation Effects 0.000 title claims abstract description 12
- 239000007789 gas Substances 0.000 claims abstract description 53
- 239000003595 mist Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000003546 flue gas Substances 0.000 claims abstract description 18
- 230000033228 biological regulation Effects 0.000 claims abstract description 14
- 239000000428 dust Substances 0.000 claims abstract description 6
- 238000013517 stratification Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 16
- 239000000126 substance Substances 0.000 claims description 11
- 239000000779 smoke Substances 0.000 claims description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 2
- 239000002253 acid Substances 0.000 abstract description 10
- 235000019504 cigarettes Nutrition 0.000 abstract description 4
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 238000009529 body temperature measurement Methods 0.000 abstract 1
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000013461 design Methods 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 238000012544 monitoring process Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 230000006641 stabilisation Effects 0.000 description 3
- 238000011105 stabilization Methods 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
- F23L15/00—Heating of air supplied for combustion
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D15/00—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies
- F28D15/02—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes
- F28D15/0266—Heat-exchange apparatus with the intermediate heat-transfer medium in closed tubes passing into or through the conduit walls ; Heat-exchange apparatus employing intermediate heat-transfer medium or bodies in which the medium condenses and evaporates, e.g. heat pipes with separate evaporating and condensing chambers connected by at least one conduit; Loop-type heat pipes; with multiple or common evaporating or condensing chambers
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Air Supply (AREA)
Abstract
A kind of film-type evaporation phase-change heat-exchanger to air heating, including: evaporator section, steam pipe, vapour gas heat exchanging segment, solidifying water pipe, ultra micro mist film generating means and control system.Wherein: evaporator section is placed in flue, evaporator section is connected with vapour gas heat exchanging segment by steam pipe, and vapour gas heat exchanging segment is connected with evaporator section by solidifying water pipe, ultra micro mist film generating means, constitutes a closed loop system；The ultra micro mist film generator of ultra micro mist film generating means is placed in evaporator section fin heat exchange pipe.Control system is connected with cigarette temperature measuring point, evaporator section wall temperature measurement point and air channel regulation valve in flue respectively.The present invention is applicable to the various forms flue gas residual heat utilization of Industrial Boiler, kiln, heating furnace, solves a difficult problem for flue inner fin heat exchange tube easily acid dew burn into dust stratification, and heat exchange efficiency is higher than common phase-change heat-exchanger.
Description
Technical field
The present invention relates to one utilizes Industrial Boiler, kiln and heating furnace afterbody low-temperature flue gas waste heat to inlet air of boiler
The film-type evaporation phase-change heat-exchange air preheater of heating.
Background technology
Boiler is one of highly energy-consuming equipment in commercial production, in the factors affecting boiler thermal output, flue gas loss
Accounting for the 70～80% of the whole heat loss of boiler, exhaust gas temperature height is one of main index of boiler heat loss, is to weigh pot
" significant " parameter of furnace thermal efficiency.Exhaust gas temperature often reduces by 15 DEG C, can improve boiler efficiency about 1%.Reduce exhaust gas temperature not only
Boiler efficiency can be improved, it is also possible to reduce carbon dioxide, sulfur dioxide, the discharge of nitrogen oxides, be effectively protected environment.
At present, utilizing field at low-temperature flue gas waste heat, widely used heat-pipe air preheater is reducing exhaust gas temperature, is carrying
High boiler thermal output, reduction disposal of pollutants aspect have really played certain effect, but there is also series of problems and be difficult to solve,
That is: cold end corrosion, dust stratification and heat pipe are because of on-condensible gas Problem of Failure, and common phase-change heat-exchanger cannot due to its reasons in structure
Apply at vertical gas pass, can only be in horizontal flue application etc., such various reasons utilizes reducing energy consumption to residual heat from boiler fume
Bring many difficulties.
Summary of the invention
The present invention is directed to existing boiler tail flue gas waste heat recovery exist dust stratification, cold end corrosion and heat exchange efficiency low, be subject to
The problems such as flue shaped position restriction, propose a kind of diaphragm type evaporative phase-change heat exchange air preheater, solve above-mentioned engineering
An application difficult problem.
The technical scheme is that: a kind of film-type evaporation phase-change heat-exchange air preheater, including: evaporator section, steam pipe, vapour
Gas heat exchanging segment, solidifying water pipe, liquid working substance defecator, ultra micro mist film generating means and control system.Wherein: evaporator section is placed in cigarette
In road, the upper end of evaporator section is connected with the lower end of steam pipe by steam header, and the upper end of vapour gas heat exchanging segment is upper with steam pipe
End is connected, and the upper end of solidifying water pipe is connected with the lower end of vapour gas heat exchanging segment, and the other end passes through liquid working substance defecator and ultra micro mist
Film generating means is connected with the other end of evaporator section, control system respectively with steam pipe, vapour gas heat exchanging segment, the point for measuring temperature of flue and
Air channel regulation valve is connected.
Described vapour gas heat exchanging segment includes: vapour gas fin heat exchange pipe is arranged, wherein: vapour gas fin heat exchange pipe is arranged and arranged and is placed in
The inside of vapour gas heat exchanging segment；Vapour gas heat exchanging segment top is provided with even case, steam inlet, and vapour gas heat exchanging segment lower end is provided with solidifying water and goes out
Mouthful.
Described ultra micro mist film generating means, including: liquid working substance defecator, ultra micro mist film generator, force (forcing) pump and resistance
Dirt device；Wherein: defecator upper end is connected with solidifying water pipe lower end, the other end is occurred with ultra micro mist film by force (forcing) pump, antisludging equipment
Device is connected, and ultra micro mist film generator is placed in evaporator section fin heat exchange pipe row, to heat exchanger tube inwall spray ultra micro water smoke and at inwall
Form mist film.
Described evaporator section includes: fin heat exchange pipe row, steam header and connecting tube, wherein: fin heat exchange pipe be set with in
Vertically or horizontally in flue, the two ends of connecting tube are connected with fin heat exchange pipe row and steam header respectively, the position of steam header
Set high the upper end in bank of tubes.
Described control system, including: smoke inlet temperature point, flue gas exit temperature measuring point, vapor (steam) temperature measuring point, sky
Gas inlet temperature measuring point, air exit temp measuring point and air channel regulation valve, wherein: vapor (steam) temperature measuring point is arranged in connecting tube
End.Heat exchanger heat-exchanging tube wall surface temperature entirety uniformity, and controllable, it is maintained at more than dew point temperature, effectively prevent
The phenomenons such as the acid dew burn into dust stratification that ordinary heat exchanger causes because evaporator section fin heat exchange pipe row's wall surface temperature is uneven.
Described evaporator section fin heat exchange pipe row, vapour gas heat exchange bank of tubes are Influences of Structure of Spiral Finned Tube side by side.
The present invention is overall consistent and controllable except possessing good thermal conduction, heat exchanger each heat exchanger tube wall temperature, it is adaptable to level,
The various flue such as vertically, overcomes tradition phase-change heat-exchanger because being limited the most applicable drawback by field condition in engineering.
The operation principle of the present invention:
Membrane type evaporative phase-change heat exchange air preheater of the present invention, its evaporator section is arranged in boiler, kiln back-end ductwork, and vapour gas changes
Hot arc is arranged on the position higher than evaporator section, in heat exchanger, liquid working substance changes at evaporator section fin through ultra micro mist film generator
Producing ultra micro mist in heat pipe, micro-mist is uniformly attached to heat exchanger tube inwall, absorbs flue gas heat, and rapid vaporization, at fin heat exchange pipe
Interior generation saturated vapor, the saturated vapor in finned tube is collected in steam header by connecting tube, and steam header passes through steam
Pipe is connected to vapour gas heat exchanging segment and connects the steam inlet of case, and in vapour gas heat exchanging segment, by heat exchange, heated air absorbs heat
Amount, after temperature is increased to design temperature, enters inlet air of boiler pipeline；It is condensed into water, by vapour gas heat exchange after saturated vapor heat release
Section lower end is coagulated water pipe and is dropped to defecator, by force (forcing) pump, antisludging equipment, ultra micro mist film generator, again at finned tube inwall
Form ultra micro mist film, reciprocation cycle, reach to utilize the purpose of fume afterheat.Regulation air channel control valve opening, regulates air intlet
Air quantity, controls vapour gas heat exchanging segment vapour gas heat exchange rate with this, make steam measuring point temperature stabilization at design temperature so that in flue
Evaporator section fin heat exchange pipe wall temperature is controllable, it is ensured that it is consistently higher than acid dew-point temperature, it is to avoid acid dew corrosion.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention.
Figure includes: 1, flue (1), 2, evaporator section (2), 3, fin heat exchange pipe row (3), 4, connecting tube (4), 5, temperature surveys
Point (5), 6, steam header (6), 7, steam pipe (7), 8, temperature point (8), 9, vapour gas heat exchanging segment (9), 10, fin heat exchange pipe row
(10), 11, temperature point (11), 12, solidifying water pipe (12), 13, liquid working substance defecator (13), 14, force (forcing) pump (14), 15,
Antisludging equipment (15), 16, ultra micro mist film generator (16), 17, control system (17), 18, smoke inlet temperature point (18), 19,
Flue gas exit temperature measuring point (19), 20, even case (20), 21, air channel regulation valve (21).
Detailed description of the invention
Below in conjunction with embodiment, the present invention is elaborated:
This example evaporator section (2) is placed in flue (1), and fin heat exchange pipe row (3) of evaporator section (2) is by connecting tube (4) and steaming
Vapour header (6) is connected, and steam header (6) upper end is connected with jet chimney (7) lower end, steam pipe (7) upper end and vapour gas heat exchanging segment
(9) upper end is connected, and the lower end of vapour gas heat exchanging segment (9) is connected with the upper end of solidifying water pipe (12), solidifying waterpipe (12) lower end and liquid
Work defecator (13) import is connected, and liquid working substance defecator (13) outlet is by force (forcing) pump (14), antisludging equipment (15) and surpasses
Micro-fog generator (16) be connected, ultra micro mist film generator (16) be built in fin heat exchange pipe row (3) pipe in, control system (17) with
Smoke inlet temperature point (18), flue gas exit temperature measuring point (19), vapor (steam) temperature measuring point (5), inlet air temp measuring point
(8), air exit temp measuring point (11), force (forcing) pump (14) and air channel regulation valve (21) are connected.
In this example, evaporator section (2) including: fin heat exchange pipe row (3), connecting tube (4), steam header (6), wherein: fin
Heat exchange bank of tubes (3) is placed in flue (1), and fin heat exchange pipe row (3) is connected with steam header (6) by connecting tube (4), vapor collection
(3) are arranged higher than fin heat exchange pipe in case (6) position.
In this example, vapour gas heat exchanging segment (9) including: soda pop fin heat exchange pipe row (10), wherein: vapour gas fin heat exchange pipe is arranged
And arrange and be placed in the inside of vapour gas heat exchanging segment (9) (10)；Vapour gas heat exchanging segment (9) top is provided with even case (20), steam inlet, vapour
Gas heat exchanging segment (9) lower end is provided with solidifying water out.
In this example, ultra micro mist film generating means includes: liquid working substance defecator (13), force (forcing) pump (14), antisludging equipment
(15) ultra micro mist film generator (16).In wherein ultra micro mist film generator (16) is placed in fin heat exchange pipe row (3) pipe.
In this example, control system (17) including: smoke inlet temperature point (18), flue gas exit temperature measuring point (19), steaming
Stripping temperature measuring point (5), inlet air temp measuring point (8), air exit temp measuring point (11), air channel regulation valve (21).Wherein: temperature
Degree measuring point (5) is arranged at connecting tube (4) upper end.
This example actual moving process: high-temperature flue gas is arranged, with the circulatory mediator in pipe through the fin heat exchange pipe of evaporator section
Heat exchange, cigarette temperature drop is low；Working medium in finned tube is the circulation formed at fin heat exchange pipe comb inwall through ultra micro mist film generator
Working medium liquid film, liquid film absorbs the heat of flue gas, and rapid vaporization forms water vapour, through connecting tube, steam header, jet chimney
After, enter in vapour gas heat exchanging segment, carry out heat exchange with heated inlet air of boiler, condense into water after heat release and drop pipeline under water through solidifying
Backflow, through liquid working substance defecator to ultra micro mist film generator, completes a circulation.
Temperature point of the present invention, force (forcing) pump, air channel regulation valve constitute closed loop control by PLC control system, by monitoring
The temperature of temperature point, regulation air channel control valve opening, regulate air air quantity, control vapour gas heat exchanging segment vapour gas heat exchange speed with this
Rate, make steam measuring point temperature stabilization at design temperature so that evaporator section fin heat exchange pipe wall temperature is controllable in flue, it is ensured that
Heat exchanger tube wall temperature is consistently higher than flue gas acid dew point temperature, it is ensured that system safety operation.
The present embodiment is power plant's 75t/h coal-burning boiler, flue-gas temperature 154 DEG C, and acid dew-point temperature is 89.97 DEG C, flue gas
The outer surface arranged with fin heat exchange pipe through evaporator section directly contacts, and flue gas carries out heat exchange with the cycle fluid in fin bank of tubes
Rear temperature is reduced to 115 DEG C.
Through the uniform circulation working medium thin liquid film that ultra micro mist film generator is formed at fin heat exchange pipe row's inner tubal wall, added by flue gas
After heat, vaporization forms steam, and steam is by entering vapour gas heat exchanging segment after connecting tube, steam header, steam pipe, at vapour gas heat exchanging segment
Condensing into water after carrying out heat exchange with heated air, solidifying water is back to liquid working substance defecator by solidifying water pipe, final to super
Micro-fog generator forms closed circuit, and circulatory mediator moves in circles with vapour, liquid two phase in this closed circuit, it is achieved heat
Transmission.
At vapour gas heat exchanging segment, the heated air of 20 DEG C regulates valve through air channel, enters in vapour gas heat exchanging segment, is changed by fin
After cycle fluid is steam heated to 72 DEG C in heat pipe, enter air mother's pipeline.
Signal, by monitoring temperature point temperature, is sent air channel regulation valve, timely adjustment air channel regulation valve by control system
Aperture, regulates heated air air quantity, makes vapor (steam) temperature measuring point temperature stabilization at 100 DEG C, and evaporator section finned tube wall also keeps
At 100 DEG C, the acid dew-point temperature higher than 89.97 DEG C, effectively prevent the acid dew corrosion of heat exchanger.When temperature point value is less than
When 100 DEG C, the risk producing the phenomenons such as acid dew burn into dust stratification will strengthen.At this moment, control system will be the temperature letter of actual measurement
Number feed back to air channel regulation valve, regulate its aperture, reduce heated air flow, make measuring point temperature recovery and stably at 100 DEG C.
When temperature point value is more than 100 DEG C, exhaust gas temperature raises, and fume afterheat can not make full use of.At this moment, control system will be
The temperature signal of actual measurement feeds back to air channel regulation valve, regulates its aperture, increases heated air flow, makes measuring point temperature decline also
Stable at 100 DEG C, Mist heat recovering to greatest extent.
By monitoring steam pipe vapor (steam) temperature, by control system timely adjustment air channel control valve opening, finally make circulation
Medium temperature remains at about 100 DEG C, and evaporator section fin heat exchange pipe row's wall surface temperature also remains at about 100 DEG C,
Higher than dew point temperature 10 DEG C, film-type evaporation phase-change heat-exchanger outlet cigarette temperature is maintained at about 115 DEG C.The present invention is avoiding acid dew corruption
On the premise of erosion, reduce exhaust gas temperature to greatest extent, improve boiler efficiency.
Claims (6)
1. a film-type evaporation phase-change heat-exchange air preheater, it is characterised in that including: evaporator section (2), steam pipe (7), vapour gas
Heat exchanging segment (9), solidifying water pipe (12), ultra micro mist film generating means and control system (17), wherein: evaporator section (2) is placed in flue (1)
In, the upper steam header (6) of evaporator section (2) is connected with the lower end of steam pipe (7), the upper end of vapour gas heat exchanging segment (9) and
The upper end of steam pipe (7) is connected, and the lower end of vapour gas heat exchanging segment (9) is connected with the upper end of solidifying water pipe (12), under solidifying water pipe (12)
End is by liquid working substance defecator (13), force (forcing) pump (14), antisludging equipment (15), ultra micro mist film generator (16) and evaporator section
(2) the other end be connected, control system (17) respectively with evaporator section temperature point (5), inlet air temp measuring point (8), air
Outlet temperature measuring point (11), the point for measuring temperature (18) of flue entrance, the point for measuring temperature (19) of flue outlet, force (forcing) pump (14) and air channel are adjusted
Joint valve (21) is connected.
Film-type evaporation phase-change heat-exchange air preheater the most according to claim 1, is characterized in that, described vapour gas heat exchanging segment
(9) including: soda pop fin heat exchange pipe row (10), wherein: vapour gas fin heat exchange pipe row (10) arrangement are placed in vapour gas heat exchanging segment (9)
Inside；Vapour gas heat exchanging segment (9) top is provided with even case (20), steam inlet, and vapour gas heat exchanging segment (9) lower end is provided with solidifying water and goes out
Mouthful.
Film-type evaporation phase-change heat-exchange air preheater the most according to claim 1, is characterized in that, described ultra micro mist film occurs
Device, including: liquid working substance defecator (13), force (forcing) pump (14), ultra micro mist film generator (16)；Wherein: defecator
(13) upper end is connected with solidifying water pipe (12) lower end, and the other end is by force (forcing) pump (14), antisludging equipment (15) and ultra micro mist film generator
(16) being connected, ultra micro mist film generator (16) is placed in evaporator section fin heat exchange pipe row (3) pipe.
Film-type evaporation phase-change heat-exchange air preheater the most according to claim 1, is characterized in that, described evaporator section (2)
Including: fin heat exchange pipe row (3), steam header (6) and connecting tube (4), wherein: fin heat exchange pipe row (3) is placed in vertically or water
In flat flue, connecting tube (4) is connected with fin heat exchange pipe row (3) and steam header (6), and the position of steam header (6) is higher than wing
The upper end of sheet heat exchange bank of tubes (3).
Film-type evaporation phase-change heat-exchange air preheater the most according to claim 1, is characterized in that, described control system
(17), including smoke inlet temperature point (18), flue gas exit temperature measuring point (19), vapor (steam) temperature measuring point (5), air intake
Temperature point (8), air exit temp measuring point (11), air channel regulation valve (21), wherein: temperature point (5) is arranged at connecting tube
(4) upper end, heat exchanger heat-exchanging tube wall surface temperature entirety uniformity and controllable, it is maintained at more than dew point temperature, effectively keeps away
Exempt from ordinary heat exchanger because of phenomenons such as the uneven sour dew burn into dust stratifications caused of evaporator section fin heat exchange pipe row's wall surface temperature.
Film-type evaporation phase-change heat-exchange air preheater the most according to claim 1, is characterized in that: described fin heat exchange pipe
Row (3), vapour gas heat exchange bank of tubes (10) are Influences of Structure of Spiral Finned Tube side by side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610739161.1A CN106123014A (en) | 2016-08-29 | 2016-08-29 | Film-type evaporation phase-change heat-exchange air preheater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610739161.1A CN106123014A (en) | 2016-08-29 | 2016-08-29 | Film-type evaporation phase-change heat-exchange air preheater |
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| CN106123014A true CN106123014A (en) | 2016-11-16 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610739161.1A Pending CN106123014A (en) | 2016-08-29 | 2016-08-29 | Film-type evaporation phase-change heat-exchange air preheater |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106871150A (en) * | 2017-01-23 | 2017-06-20 | 中国科学院广州能源研究所 | Efficient HEP flue gas heat-exchange units |
| CN110608626A (en) * | 2019-10-08 | 2019-12-24 | 苏州惠林节能材料有限公司 | Liquid-filled separated heat pipe |
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| CN104833138A (en) * | 2015-05-28 | 2015-08-12 | 上海东方低碳系统集成有限公司 | Ultrasonic atomization condenser |
| CN105841180A (en) * | 2016-05-16 | 2016-08-10 | 杭州华电能源工程有限公司 | Horizontal type phase change smoke waste heat recovering and double-effect heating system and control method thereof |
| CN206540164U (en) * | 2016-08-29 | 2017-10-03 | 河南益丰源科技有限公司 | Film-type evaporation phase-change heat-exchange air preheater |
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| CN106871150A (en) * | 2017-01-23 | 2017-06-20 | 中国科学院广州能源研究所 | Efficient HEP flue gas heat-exchange units |
| CN106871150B (en) * | 2017-01-23 | 2019-03-05 | 中国科学院广州能源研究所 | HEP flue gas heat-exchange unit |
| CN110608626A (en) * | 2019-10-08 | 2019-12-24 | 苏州惠林节能材料有限公司 | Liquid-filled separated heat pipe |
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Application publication date: 20161116 |