CN106090973A - Smoke processing system and method - Google Patents
Smoke processing system and method Download PDFInfo
- Publication number
- CN106090973A CN106090973A CN201610458287.1A CN201610458287A CN106090973A CN 106090973 A CN106090973 A CN 106090973A CN 201610458287 A CN201610458287 A CN 201610458287A CN 106090973 A CN106090973 A CN 106090973A
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- Prior art keywords
- flue gas
- fin
- fluid flow
- heat
- flow tube
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Links
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000000779 smoke Substances 0.000 title claims abstract description 22
- 238000012545 processing Methods 0.000 title claims abstract description 18
- 239000003546 flue gas Substances 0.000 claims abstract description 114
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 111
- 239000012530 fluid Substances 0.000 claims abstract description 66
- 239000007789 gas Substances 0.000 claims abstract description 47
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 21
- 239000000428 dust Substances 0.000 claims abstract description 20
- 230000023556 desulfurization Effects 0.000 claims abstract description 19
- 239000003517 fume Substances 0.000 claims abstract description 19
- 238000010438 heat treatment Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 13
- 238000010792 warming Methods 0.000 claims abstract description 5
- 238000012546 transfer Methods 0.000 claims description 84
- 229910000831 Steel Inorganic materials 0.000 claims description 9
- 239000010959 steel Substances 0.000 claims description 9
- 238000003466 welding Methods 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 6
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 4
- 239000010962 carbon steel Substances 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- 238000000465 moulding Methods 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 238000003672 processing method Methods 0.000 abstract description 3
- 235000019504 cigarettes Nutrition 0.000 description 9
- 238000010586 diagram Methods 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 238000013517 stratification Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 230000004927 fusion Effects 0.000 description 4
- 238000004364 calculation method Methods 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 239000004071 soot Substances 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 238000005097 cold rolling Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000004806 packaging method and process Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000005530 etching Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000000611 regression analysis Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012795 verification Methods 0.000 description 1
- 238000012800 visualization Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J11/00—Devices for conducting smoke or fumes, e.g. flues
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/10—Nitrogen; Compounds thereof
- F23J2215/101—Nitrous oxide (N2O)
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2215/00—Preventing emissions
- F23J2215/20—Sulfur; Compounds thereof
-
- 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
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
Smoke processing system and method.The method includes: be passed through recirculated water in the circulation line that the fluid flow tube of gas cooler and the fluid flow tube of Smoke-heating device of the present invention is formed；Fume dust remover and flue gas desulfurization device is sequentially entered after the flue gases of about 140 DEG C are cooled to about 90 DEG C by gas cooler；Smoke stack emission is passed through after flue gas by being lowered the temperature further after flue gas desulfurization device is warming up to about 90 DEG C again by flue gas heater；And recirculated water is flowed into gas cooler and to be not less than the temperature cycles outflow gas cooler of 100 DEG C with the temperature cycles being not less than 70 DEG C.The flue gas processing method of the present invention maximises the service life of gas cooler, and selectivity implements the thermal energy exchange of upstream flue gas and downstream fume gas simultaneously, has reached high-efficient energy-saving environment friendly purpose.
Description
Technical field
This patent disclosure relates generally to fume treatment technology.
Background technology
The oval base tube H type fin proposed in flue gas heat-exchange unit patent CN101762199B obtained before applicant passes
Heat pipe has that Soot Performance wear-resistant, anti-is good, flow resistance is little, low in energy consumption, compact conformation, unit space can accommodate more being subject to
The advantages such as hot side.Obtain application in had under its command power plant such as Huaneng Group group, Shen Neng group, CITIC Groups in recent years, and obtain preferably
Effect.
But, harsh because of environmental requirement in recent years, minimum discharge technology and low temp. electric cleaner unit technology obtain to be greatly developed
And popularization, cigarette cooler is arranged at electric cleaner upstream, and dust concentration is up to 10000～60000mg/Nm3, flue dust abrasion adds
Play, dust stratification is serious all the more, and flue gas cool-down amplitude is up to 50 DEG C, therefore to the flow resistance of heat-transfer pipe, the power consumption that flows, heat transfer energy
Power etc. all propose requirements at the higher level.
Additionally, lack organic combination between existing each step of fume treatment process, cause whole process energy consumption excessive.
Summary of the invention
It is an object of the invention to provide the fume treatment technology of improvement, it can overcome certain or some of prior art to lack
Fall into.
According to the first aspect of the invention, it is provided that a kind of smoke processing system, including:
The gas cooler being arranged in cooling stack, gas cooler is connected with each other by multiple heat-transfer pipes and forms, each
Heat-transfer pipe comprises:
Middle part has a fluid flow tube of oval cross section, a length of 2a of the major axis of wherein said ellipse, a length of 2b of short axle,
Wherein the ratio of a and b is between 1.9 to 2.9；And
Along the axial multipair flue gas fin spaced apart from each other of fluid flow tube on fluid flow tube outer surface, every pair of flue gas fin includes phase
Mutually alignment and be collectively forming the first flue gas fin and the second flue gas fin, the length of wherein said rectangle of rectangle outline
The a length of A on limit, a length of B of minor face, the shape of the first flue gas fin and the second flue gas fin is identical, is provided with oval
The elliptic arc breach that tube outer surface shape is suitable, has between the first flue gas fin and the second flue gas fin of every pair of flue gas fin
There is the gap, outside along described transverse direction,
It is positioned at the fume dust remover in cooling stack downstream, for the flue gas from cooling stack is carried out dust removal process；
It is positioned at the flue gas desulfurization device in fume dust remover downstream, for the flue gas after fume dust remover dedusting
Carry out desulfurization process；
It is positioned at the Smoke-heating device in flue gas desulfurization device downstream, there is fluid flow tube, for through flue gas desulfurization device
Flue gas after desulfurization carries out heat treated；And
It is positioned at the chimney in Smoke-heating device downstream, discharges the flue gas after Smoke-heating device heats,
Wherein the fluid flow tube of gas cooler connects with the fluid flow tube of Smoke-heating device and forms circulation line.
The smoke processing system of the present invention is owing to have employed heat-transfer pipe or the gas cooler of improvement, and uses from upstream cigarette
The heat energy that gas is reclaimed carrys out heated downstream flue gas to be discharged, thus significantly reduces the energy consumption during whole fume treatment, with
Enter the energy-conserving and environment-protective improvement requirement that such as power plant etc. is constantly proposed by country.
A specific embodiment according to the present invention, smoke processing system can also include: is positioned at gas cooler upstream
The air preheater with air pipe line, be positioned at air preheater upstream equipment for denitrifying flue gas and be positioned at denitrating flue gas dress
Putting the boiler of upstream, wherein equipment for denitrifying flue gas carries out denitration process to the flue gas from boiler, and air preheater utilizes denitration
After flue gas the air in its air pipe line is carried out the pre-heat treatment, the wherein burning of the air pipe line of air preheater and boiler
Room connects.This embodiment arranges air preheater and reclaims to utilize while to flue gas continued down in gas cooler upstream
Energy heats air also sends into boiler furnace, thus improves boiler combustion efficiency, and makes fume emission more environmentally-friendly.
Air preheater can be made up of the back-end surfaces of boiler.
The single tube embodiment of the heat-transfer pipe according to the present invention, each heat-transfer pipe only comprises single fluid flow tube, the ratio of A Yu 2a
Between 1.3 to 2.3 and the ratio of B and 2b is between 2.0 to 4.0.In a further preferred embodiment, the ratio of A and 2a
Value can between 1.5 to 2.2, further preferably can between 1.6 to 2.0, more preferably about 1.8；The ratio of B Yu 2b
Can between 2.2 to 3.0, further preferably can between 2.3 to 2.8, more preferably about 2.5.
The two-tube embodiment of the heat-transfer pipe according to the present invention, each heat-transfer pipe includes and only two fluid flow tubes, A and 2a
Ratio between 2.6 to 4.6 and the ratio of B and 2b is between 2.0 to 4.0.In a further preferred embodiment, A with
The ratio of 2a can between 3.0 to 4.4, further preferably can between 3.2 to 4.0, more preferably about 3.6；B and 2b
Ratio can between 2.2 to 3.0, further preferably can between 2.3 to 2.8, more preferably about 2.5.
The preferred embodiment of the heat-transfer pipe according to the present invention, the equivalent diameter of the cross section ellipse of fluid flow tube can be at 32mm
Between 51mm, more preferably 32mm or 38mm.Here equivalent circular refers to: one mother metal pipe of direct cold rolling and form mesh
Mark elliptical tube, wherein for Target ellipse pipe, the diameter of mother metal pipe is exactly its equivalent diameter.A diameter of 32mm or
The mother metal pipe of 38mm or 51mm is commercially available specification pipe, and acquisition is convenient.
The preferred embodiment of the heat-transfer pipe according to the present invention, gap, the outside thickness between upper and lower fin can at 6mm extremely
Between 12mm, preferably about 8mm.
The preferred embodiment of the heat-transfer pipe according to the present invention, the fluid flow tube of gas cooler and/or the material of flue gas fin
Can be selected from carbon steel, ND steel and rustless steel, and flue gas fin and the most independent molding of fluid flow tube be linked to be by welding
Integrally.
The most preferred embodiment of the heat-transfer pipe according to the present invention, the ratio of a Yu b is about 2.5.
Different specific embodiments according to the present invention: the thickness of flue gas fin can be between 1.5mm to 4mm；Fluid flow tube
Pipe thickness can be between 3mm to 5mm；The axial spacing of phase adjacency pair flue gas fin can be between 10mm to 30mm.
According to another specific embodiment of the present invention, the two end portions of fluid flow tube can have circular cross-section.This two
The fluid flow tube of end circular cross-section design is convenient uses conventional criteria joint to be attached in follow-up assembling process.
According to the second aspect of the invention, it is provided that a kind of side utilizing above-mentioned smoke processing system to carry out fume treatment
Method, including:
It is passed through circulation in the circulation line that the fluid flow tube of gas cooler and the fluid flow tube of Smoke-heating device are formed
Water；
Sequentially enter after the flue gases of about 140 DEG C are cooled to about 90 DEG C by gas cooler fume dust remover and
Flue gas desulfurization device；
Flue gas by being lowered the temperature further after flue gas desulfurization device is warming up to about 90 DEG C again by flue gas heater
After pass through smoke stack emission；And
Recirculated water is flowed into gas cooler and to be not less than the temperature cycles of 100 DEG C with the temperature cycles being not less than 70 DEG C
Flow out gas cooler.
The flue gas processing method of the present invention maximises the service life of gas cooler, and selectivity implements upstream cigarette simultaneously
Gas and the thermal energy exchange of downstream fume gas, reached high-efficient energy-saving environment friendly purpose.
One specific embodiment of the method according to the invention, flue gas can be dropped further by after flue gas desulfurization device
Temperature is to about 50 DEG C.
Another specific embodiment of the method according to the invention, flue gas comes from the boiler smoke of about 300 DEG C, flows successively
About 140 DEG C can be cooled to before entering gas cooler after flue gas desulfurization device and air preheater.
The flue gas processing method of the present invention passes through further Optimizing Process Parameters, and the linking of each processing step can be made to join
Close more smooth smoothness.
Additionally, according to the gas cooler of the present invention, for above-mentioned single tubing type and the heat-transfer pipe of two-tube type, it is on-the-spot
Assemble method is also different.
For the heat-transfer pipe of single tubing type, the method forming gas cooler in being assembled in flue includes:
Heat-transfer pipe is arranged in flue at least one side wall, and every face wall is each perpendicular to flow of flue gas direction in flue, often
The fluid flow tube setting parallel with one another of the heat-transfer pipe in face wall, the fluid flow tube of each heat-transfer pipe is the most horizontally disposed and makes gap, outside cloth
It is set to just to flow of flue gas direction (parallel with flow of flue gas direction)；
Flue sidewall is all stretched out at the two ends of each fluid flow tube；
Union elbow is provided；And
Use union elbow by the same level height in every face wall adjacent along flow of flue gas direction outside flue
The two ends of fluid flow tube are sequentially connected in series, and are thus assembled into heat exchanger.
For the heat-transfer pipe of two-tube type, the method forming gas cooler in being assembled in flue includes:
Heat-transfer pipe is arranged in flue at least one side wall, and every face wall is each perpendicular to flow of flue gas direction in flue, often
The fluid flow tube setting parallel with one another of the heat-transfer pipe in face wall, the fluid flow tube of each heat-transfer pipe is the most horizontally disposed and makes gap, outside cloth
It is set to just to flow of flue gas direction, and makes the first fluid flow tube of each heat-transfer pipe be positioned at the upstream of flow of flue gas of the second fluid flow tube
Direction；
Flue sidewall is all stretched out at the two ends of each fluid flow tube；
First big syphon joint and the second little union elbow are provided；
Use the first big syphon joint by one end of the first fluid flow tube of each heat-transfer pipe in every face wall outside flue
Same side with the second fluid flow tube of the heat-transfer pipe of the same level height along an adjacent face wall in downstream, flow of flue gas direction
It is connected in series；And
Use the second little union elbow by one end of the second fluid flow tube of each heat-transfer pipe in every face wall outside flue
Same side with the first fluid flow tube of the heat-transfer pipe of the same level height along an adjacent face wall in downstream, flow of flue gas direction
It is connected in series,
Thus, it is assembled into heat exchanger.
According to the present invention, fluid flow tube is preferably formed by the pipe direct cold rolling of diameter 32mm or 38mm or 51mm.It addition, liquid
Flow tube two end portions (the non-fin region outside intermediate body portion) can be reverted to round tube shape again so that using circle
Pipe joint is directly interconnected assembly operation.
Use above-mentioned assemble method, can the heat-transfer pipe of the present invention be assembled the most such as power plant's flue
Become gas cooler or the heat exchanger of required specification, and packaging efficiency and quality have been effectively ensured.
Accompanying drawing explanation
Fig. 1 is the axonometric chart of the single-tube heat-transfer pipe according to the present invention；
Fig. 2 is the schematic cross-section of the single-tube heat-transfer pipe according to the present invention；
Fig. 3 is the sectional dimension schematic diagram of the single-tube heat-transfer pipe of existing example；
Fig. 4 is the corresponding oval base tube sectional dimension corresponding to Φ 32 equivalent pipe single-tube heat-transfer pipe according to the present invention
Schematic diagram；
Fig. 5 is the corresponding oval base tube sectional dimension corresponding to Φ 38 equivalent pipe single-tube heat-transfer pipe according to the present invention
Schematic diagram；
Fig. 6 is the axonometric chart of the double-tube type heat-transfer pipe according to the present invention；
Fig. 7 is the schematic cross-section of the double-tube type heat-transfer pipe according to the present invention；
Fig. 8 is the cross section chi of the corresponding oval base tube corresponding to Φ 32 equivalent pipe double-tube type heat-transfer pipe according to the present invention
Very little schematic diagram；
Fig. 9 is the cross section chi of the corresponding oval base tube corresponding to Φ 38 equivalent pipe double-tube type heat-transfer pipe according to the present invention
Very little schematic diagram；
Figure 10 is the schematic top plan view during double pipe structure using the different union elbow interconnection present invention；
Figure 11 is the fluid separation in pipe downstream and whirlpool；
Figure 12 is the fluid separation in elliptical tube downstream and whirlpool；
Figure 13 is along with elliptical tube ratio of semi-minor axis length increases, the schematic diagram moved after burble point；
Figure 14 is the boiler of power plant smoke processing system according to the present invention.
Detailed description of the invention
Below in conjunction with embodiment and accompanying drawing, the present invention will be further described, it should be appreciated by those skilled in the art that enforcement
Example and accompanying drawing are intended merely to be more fully understood that the present invention, are not used to make any restriction.
See Fig. 1, include single elliptical tube 10 and the longitudinal direction along elliptical tube 10 according to the single-tube heat-transfer pipe of the present invention
Or the axial arranged multipair fin (maybe can be referred to as " H type fin ") being mutually aligned.According to practical situation needs, the every pair of fin with
The spacing of 10-30mm is evenly spaced.Every pair of fin includes fin 21 and lower fin 22.Elliptical tube 10, upper fin 21 and
The material of lower fin 22 can be selected from carbon steel, ND steel and rustless steel, and respective independent molding is the highest by welding subsequently
Strobe light electric resistance welding is connected again.Heat-transfer pipe can further be assembled into heat exchanger (also referred to as " heat exchanger " or " cigarette
Gas Cooler ") it is arranged in the flue of such as power plant, describe in further detail as rear.
Elliptical tube 10 is generally passed through liquid to be heated such as water, is therefore also referred to as " fluid flow tube ".Although diagram elliptical tube
10 total lengths are consistent oval cross section, but elliptical tube 10 can also be designed to two ends remains as circular cross-section, are intended only as main
Oval cross section is made at the middle part of body.This two ends have the elliptical tube 10 of circular cross-section and have excellent during later stage assembly and connection
Gesture, can still use the circular section union elbow of routine to be interconnected.
Upper fin 21 and lower fin 22 are typically directly in high temperature with high dust flue gas or the smoky environment of such as flue, because of
This is also referred to as " the first flue gas fin " and " the second flue gas fin ".Upper fin 21 is identical or basic with lower fin 22 shape
Identical (illustrating mirror image each other), is substantially respectively provided with rectangle outline, and middle body is offered suitable with elliptical tube external surface shape
Or the elliptic arc breach matched is welded on elliptical tube 10 with smooth.The upper fin 21 of every pair of fin and lower fin 22 phase each other
Generally form rectangle outline after being welded on the most between two parties on elliptical tube 10 mutually, but have each other along transverse side
To gap, outside (also referred to as " crack width ") W, gap, outside W live apart symmetrically elliptical tube 10 both sides.
Single-tube embodiment as shown in Figure 2, the long axis length mark of the cross section of the elliptical tube 10 of the present invention oval (outline)
Being shown as 2a, minor axis length is denoted as 2b, and elliptical tube wall thickness is denoted as S.The upper fin 21 of every pair of fin and lower fin 22 institute are common
The long edge lengths of the overall rectangle outline formed is denoted as A, and bond length is denoted as B, between upper fin 21 and lower fin 22
The horizontal outer side gap thickness or the upper and lower distance that are formed are denoted as W.
Fig. 3 shows the relevant of as disclosed in CN101762199B one example of existing actually used oval-shaped heat transfer pipe
Size；It is representative corresponding to pipe equivalent caliber (Φ 32 He that Fig. 4 and Fig. 5 then respectively illustrates two kinds according to the present invention
Φ 38) the corresponding oval base tube of single-tube heat-transfer pipe and each relative dimensions of fin, the most as shown in table 1 below.
Table 1
Referring back to Fig. 6, include, according to the double-tube type heat-transfer pipe of the present invention, the first elliptical tube 11 and that parallel spaced apart is arranged
Two elliptical tubes 12 and the multipair fin being mutually aligned longitudinally or axially arranged along elliptical tube (maybe can be referred to as " H type wing
Sheet ").First elliptical tube 11 is identical with the second elliptical tube 12 shape.According to practical situation needs, every pair of fin is with 10-30mm's
Spacing is evenly spaced.Every pair of fin includes fin 21 and lower fin 22.First elliptical tube the 11, second elliptical tube 12, upper fin
The material of sheet 21 and lower fin 22 can be selected from carbon steel, ND steel and rustless steel, and respective independent molding also passes through weldering subsequently
Connect such as high frequency flashing light electric resistance welding to be connected again.Heat-transfer pipe can further be assembled into heat exchanger (also referred to as " heat exchange
Device ") it is arranged in the flue of such as power plant, describe in further detail as rear.
First elliptical tube 11 and the second elliptical tube 12 are generally passed through liquid to be heated such as water, are therefore also referred to as " liquid stream
Pipe ".Although diagram the first and second elliptical tube total lengths are consistent oval cross section, but elliptical tube can also be designed to two ends still
Being so circular cross-section, oval cross section is made at the middle part being intended only as main body.This two ends have the elliptical tube of circular cross-section rear
During phase assembly and connection, there is advantage, can still use the circular section union elbow of routine to be interconnected.
Upper fin 21 and lower fin 22 are typically directly in high temperature with high dust flue gas or the smoky environment of such as flue, because of
This is also referred to as " the first flue gas fin " and " the second flue gas fin ".Upper fin 21 is identical or basic with lower fin 22 shape
Identical (illustrating mirror image each other), is substantially respectively provided with rectangle outline, symmetrically offers and fits mutually with elliptical tube external surface shape
Two the elliptic arc breach joined or match are welded on two elliptical tubes with smooth.The upper fin 21 of every pair of fin and lower fin
22 be welded on the most alignedly on elliptical tube after generally form rectangle outline, but have each other along transverse
Gap, outside (also referred to as " crack width ") W, gap, outside W in direction lives apart the first elliptical tube 11 and second oval symmetrically
Outside the two of pipe 12 and extend between the two elliptical tube.
Double-tube type embodiment as shown in Figure 7, the long axis length of the cross section of the elliptical tube of the present invention oval (outline) indicates
For 2a, minor axis length is denoted as 2b, and elliptical tube wall thickness is denoted as S.The common shape of the upper fin 21 of every pair of fin and lower fin 22 institute
The long edge lengths of the overall rectangle outline become is denoted as A, and bond length is denoted as B, institute between upper fin 21 and lower fin 22
The horizontal outer side gap thickness or the upper and lower distance that are formed are denoted as W.
It is representative corresponding to pipe equivalent caliber (Φ 32 that Fig. 8 and Fig. 9 then respectively illustrates two kinds according to the present invention
With Φ 38) the corresponding oval base tube of double-tube type heat-transfer pipe and each relative dimensions of fin, the most as shown in table 2 below.
Table 2
Inventor finds when simulation study (as described in detail by rear), and the ratio of semi-minor axis length a/b of elliptical tube is a weight
Want parameter.Ratio of semi-minor axis length value a/b of the elliptical tube of existing heat-transfer pipe such as example shown in Fig. 3 is on the low side (before inventor not
Recognize the importance of this ratio), fail to give full play to heat-transfer capability after base tube is changed into elliptical tube by pipe and significantly improve, flow
The advantage that resistance is greatly reduced, anti-dust stratification ability strengthens and tube bank compactedness is improved.
Be it turned out with optimization and experimental verification by numerical analysis, Flow visualisation, regression analysis: run work at cigarette cooler
Under the conditions of condition, the long and short axle of oval base tube than a/b should between 1.9～2.9, a/b be fluid along elliptical tube flow time, stream
Moving and the important parameter of heat transfer property, it mainly affects as follows.
Can be seen that from Figure 11 and Figure 12, compared with pipe, move behind the position of elliptical tube downstream separation point, whirlpool district (wake flow
District) range shorter, whirlpool strength reduction, make the flow resistance of elliptical tube significantly lower than pipe.And with the increase of a/b, separate
Moving behind the position of point, the range shorter of whirlpool district (wake zone), whirlpool strength reduction, flow resistance reduces further.Figure 13 is
According to the result of calculation of boundary layer theory of laminar, wherein M is minimum pressure point；S is laminar separation point；U∞For speed of incoming flow (m/
s).The analytical calculation of inventor also shows: in the flow resistance of external finned tube, and the resistance of light tube outer surface accounts for drag overall
About 40%, therefore improve the a/b of elliptical tube, be extremely effective to reducing flow resistance.
Compared with the pipe of same cross section, with the increase of a/b, the girth of elliptical tube increases, and heat exchange area increases；This
Outward, along with the increase of a/b, elliptical tube wake boundary layer thickness is thinning, makes the coefficient of heat transfer of elliptical tube also increase.Numerical analysis and
Experiment confirms: the elliptical tube outer surface coefficient of heat transfer of a/b=2.75 is higher than the outer surface coefficient of heat transfer of a/b=1.67 elliptical tube
Go out about 25%, owing to heat exchange area and the coefficient of heat transfer of elliptical tube outer surface increase simultaneously, make total biography of elliptical tube outer surface
Heat energy power is significantly improved.Even if the heat transfer area in view of elliptical tube exterior light tube portion only accounts for total heat-transfer area outside fin
Long-pending about 1/5, the light pipe portion coefficient of heat transfer has the raising of about 25% also will to make the heat transfer of total heat conduction area outside opposite fins
Coefficient can have the raising of about 5%, and the most surprising in the raising of this degree of field of heat transfer.
For the tube bank of in-line arrangement, dust stratification occurs mainly in the whirlpool district in the region near the front stationary point of pipe and downstream,
Therefore with the increase of a/b, the flow stagnation region near the most front stationary point is reduced, and owing to range shorter and the whirlpool in whirlpool district are strong
Degree weakens, and makes the dust stratification amount in rear vortex district also significantly reduce.
Along with the increase of a/b, elliptical tube is streamlined more preferably, and the reduction of short axle makes the horizontal spacing of tube bank reduce, and saves
Taking up space of pipe group, makes compactedness (heat transfer surface area m can arranged in unit volume of tube bank2/m3) improve.
It addition, even more important being the discovery that of inventor, the width (long limit) of the fin of above-mentioned existing example, highly (short
Limit), the size of crack width and ellipse long and short shaft the most crucial.Because the inappropriate of these sizes all can make whole wing
The fin efficiency of sheet is on the low side, it is impossible to gives full play to base tube and is changed into the enhancing heat transfer effect of fin after elliptical tube by pipe.Based on below
Described simulation study and substantial amounts of on-the-spot test, inventor finally determines fin width A, comprises slotted fin width
Extend up and down at interior fin and exist between total height B, ellipse long and short shaft length and can close by the mutual of the above-mentioned performance of materially affect
System, i.e. the ratio of A Yu 2a and the ratio of B Yu 2b play a key effect jointly, and (attention parameters B has contained the width W that cracks
And up and down the height sum of fin rather than refer to the height of single fin again).
One of leading indicator parameter evaluating fin performance is fin efficiency, and analytical calculation shows, is oval for base tube
The rectangular fin of pipe, the part fin surface that at and wing root relatively low in fin height, radius of curvature is bigger, its local fin
Efficiency has the highest value, and suitable A/2a and B/2b can be greatly improved the local fin efficiency along fin height direction, its
Value is up to more than 90% so that the average fin efficiency of fin is more than 80%.
Suitably A/2a and B/2b can improve fin and the welding fusion angle of oval base tube, and welding fusion angle reflects H wing
Sheet and the welding contact length of oval base tube, the size of the latter's appreciable impact fin efficiency.Analyze and experiment all confirms: Fig. 3 institute
The welding fusion angle showing existing example is 149 °, and welds fusion angle in an embodiment of the present invention and all can improve to 168 °, increases
Nearly 20 ° are added.
Suitably A/2a and B/2b can improve the fluid average heat transfer coefficient at H fin outer surface, improves the heat transfer of fin
Ability.
The searching exactly that optimizes of fin surface makes the heat transfer coefficient of finned tube, inned coefficient, fin efficiency and flow resistance
A/2a and B/2b time the most optimal, or under certain inned coefficient, suitable A/2a and B/2b can make the biography of fin surface
Hot coefficient, fin efficiency and flow resistance comprehensively reach optimum.
Additionally, the width W that cracks of H type fin also has the effect that self
Dust stratification on the most bootable flue gas purging pipe and fin, obtains certain from ash-removal effect；
The proper width of 2.W can make H fin produce slight self-oscillation, makes fin surface be difficult to dust stratification, has from clear
Ash ability；
Stagnation region near the most front stationary point and the whirlpool district after downstream separation point are that in fin area, heat transfer effect is poor
Region, and the existence of gap W is equivalent to region in this section and is not provided with heat-transfer area.Though arranging a part of heat-transfer area less
Long-pending, but total heat-transfer capability of fin increases.Research shows, with the increase of a/b, cracking (gap) width W can be corresponding
Having reduced, on the basis of optimizing research, the width that cracks of current H type fin may determine that to be 6～12mm.
At least have the advantage that according to the heat-transfer pipe after the improvement of the present invention
1. flow resistance reduces by 7～about 10% further, and the reduction of flow resistance can reduce the power consumption of blower fan further,
Save the operating cost of cigarette cooler.As a example by the cigarette cooler of 1 1000MW unit, station service about 500000 kilowatts can be saved every year
Time.
2. reducing condition and the cost of fan improvement, under suitable conditions, blower fan can not be transformed or small-scale changes
Making, only this item can save the most up to ten million millions of improvement expenses.
3. total heat-transfer capability improves about 10%, as a example by the cigarette cooler of 1 1000MW unit, can save steel weight about
80～100 tons, reduce the manufacturing cost of cigarette cooler.
4. improve the compactedness that pipe group is arranged, compared with former scheme, compactedness (m2/m3) about can improve 5%～8%.
5. there is raising further from deashing ability ability, the number of soot blower can be reduced, saved use steam or compression
The cost of air soot blower and operation energy consumption.
6. make the variation of product piping, ease of assembly, be suitable for and meet the demand in market.
The most such as power plant's flue is briefly described as a example by first there is the single-tube heat-transfer pipe of circular cross-section below by two ends
How to be assembled into heat exchanger.
First, heat-transfer pipe is arranged in flue the some face walls adjacent along flue depth direction.Every face wall is the most vertical
Flow of flue gas direction in flue.Same face wall is arranged multiple horizontal heat-transfer pipe from top to bottom, the edge, two ends of its fluid flow tube
Horizontal direction vertically passes the opposing sidewalls of flue, the most up and down the gap, outside between fin just to flow of flue gas direction (or
Gap, outside longitudinal length bearing of trend is parallel with flow of flue gas direction or consistent).In same face wall, fluid flow tube is parallel with one another sets
Put；Use standard circular cross section union elbow by same in upstream and downstream (for flow of flue gas direction) adjacent wall outside flue
The two ends connection in sequential series of the fluid flow tube of level height, is thus assembled into heat exchanger.
Briefly describe as a example by there is the double-tube type heat-transfer pipe of circular cross-section again by two ends the most such as that power plant's flue is how
It is assembled into heat exchanger.
As shown in Figure 10, first, heat-transfer pipe is arranged in flue along flue depth direction (i.e. along flow of flue gas side
To) adjacent some face walls.Every face wall is each perpendicular to flow of flue gas direction in flue.Same face wall is arranged from top to bottom many
Individual horizontal heat-transfer pipe, the two ends of its fluid flow tube the most vertically pass the opposing sidewalls 50 of flue, the most up and down fin it
Between just to flow of flue gas direction, (or gap, outside longitudinal length bearing of trend is parallel with flow of flue gas direction or one gap, outside
Cause).All first fluid flow tube 11 and the second fluid flow tube 12 settings parallel with one another in same face wall；First liquid stream of each heat-transfer pipe
Pipe 11 and the second fluid flow tube 12 are the most horizontally disposed.First fluid flow tube 11 of each heat-transfer pipe is positioned at the flue gas stream of the second fluid flow tube 12
Dynamic updrift side.Use big syphon joint 31 by the first fluid flow tube 11 of each heat-transfer pipe in every face wall outside flue
Second fluid flow tube 12 of one end and the hot heat-transfer pipe of the same level height along an adjacent face wall in downstream, flow of flue gas direction
Same side be connected in series.Equally, use little union elbow 32 by second of each heat-transfer pipe in every face wall outside flue
The first of the heat-transfer pipe of one end of fluid flow tube 12 and the same level height along an adjacent face wall in downstream, flow of flue gas direction
The same side of fluid flow tube 11 is connected in series.As shown in Figure 10, big syphon joint 31 is positioned at outside little union elbow 32, at flue two
Side is alternately arranged, and does not interfere with each other at same level height.First fluid flow tube 11 of same level height and the second fluid flow tube 12 are altogether
With a liquid main entrance 60 and liquid general export 70.
Fluid flow tube in this same face wall is in parallel but arrangement mode of the series connection of wall adjacent with downstream medium high liquid flow pipe can
To make full use of fume afterheat.It addition, the mode interconnecting fluid flow tube outside flue avoids the shadow of the internal severe atmosphere of flue
Ring, reduce the faults such as leakage and occur.
It addition, employing said method, easily the heat-transfer pipe Assembling of the present invention can be become required specification
Large-scale heat exchanger, has been effectively ensured packaging efficiency and quality, and has minimized the problems such as transport inconvenience.
Additionally, as the double pipe structure of shared fin, present invention could apply to the occasion that bank of tubes is longer, it is simple to entire row,
Structural rigidity is more preferable, and manufacturing man-hours and cost are the lowest.Although two-tube above multipipe structure is also feasible, but add in execution
Work, weld, the operation such as transport time will be limited.
Gas cooler is can serve as, at the such as power plant's pot shown in Figure 14 according to the heat exchanger that the present invention is assembled into
Stove back-end ductwork Mist heat recovering also heats neat stress to realize environment protection emission.Power plant shown in Figure 14 have employed low low temp. electric
The gas cleaning exhaust system of dedusting technology, can set up the gas cooler of the present invention before low low temp. electric cleaner unit, is formed
The smoke processing system of the present invention.
As shown in figure 14, after the flue gas of boiler 1 out about 300 DEG C enters SCR denitration system 2 denitration, enter
Air preheater 3 carries out heat exchange, and the air after preheating is admitted to the combustor of boiler.From air preheater 3 flue gas fall out
To about 140 DEG C, subsequently enter the gas cooler (heat exchanger) 4 of the present invention to follow with the heat that entrance temperature is about 70 DEG C
Ring water heat exchange, after heat exchange from gas cooler out time circulating water temperature be usually less than 100 DEG C.Go out from gas cooler 4
The flue gas come is down to about 90 DEG C, subsequently enters low low temp. electric cleaner unit 5 and carries out dedusting and enter back into desulfuration absorbing tower 6 and take off
Sulfur.It is down to about 50 DEG C from desulfuration absorbing tower 6 flue gas out, subsequently enters flue gas heater 7.Flue gas heater 7 and flue gas
Cooler 4 shares heat recirculated water, discharges entering back into chimney 8 after the neat stress of about 50 DEG C is warming up to about 90 DEG C.
It is about 70 DEG C that the inlet water temperature of the gas cooler of the present invention controls, and this can minimize gas cooler and suffer
Flue gas corrosion, takes into account heat exchanger effectiveness simultaneously.It addition, after utilizing common recycle hot water that neat stress is warming up to about 90 DEG C again
Row discharge is not only able to meet environmental requirement, has also taken into account the etching problem of chimney.
Certainly, the gas cooler of the present invention can also have other suitable applications, such as, be used for heating municipal heating systems circulation
Water；Or it is used for heating steam turbine to draw gas heat regenerative system condenses water to reduce the steam amount of drawing gas in low-pressure heater,
And the quantity of steam saved enters and continues work done generating in low pressure (LP) cylinder, to reduce the rate of standard coal consumption etc. of Turbo-generator Set.
Claims (10)
1. a smoke processing system, including:
The gas cooler being arranged in cooling stack, gas cooler is connected with each other by multiple heat-transfer pipes and forms, each heat transfer
Pipe comprises:
Middle part has a fluid flow tube of oval cross section, a length of 2a of the major axis of wherein said ellipse, a length of 2b of short axle, wherein
The ratio of a and b is between 1.9 to 2.9；And
Along the axial multipair flue gas fin spaced apart from each other of fluid flow tube on fluid flow tube outer surface, it is the most right that the every pair of flue gas fin includes
Arrange and be collectively forming the first flue gas fin and the second flue gas fin of rectangle outline together, the long limit of wherein said rectangle
A length of A, a length of B of minor face, the shape of the first flue gas fin and the second flue gas fin is identical, outside being provided with elliptical tube
The elliptic arc breach that surface configuration is suitable, has edge between the first flue gas fin and the second flue gas fin of every pair of flue gas fin
The gap, outside in described transverse direction,
It is positioned at the fume dust remover in cooling stack downstream, for the flue gas from cooling stack is carried out dust removal process；
It is positioned at the flue gas desulfurization device in fume dust remover downstream, for the flue gas after fume dust remover dedusting is carried out
Desulfurization processes；
It is positioned at the Smoke-heating device in flue gas desulfurization device downstream, there is fluid flow tube, for through flue gas desulfurization device desulfurization
After flue gas carry out heat treated；And
It is positioned at the chimney in Smoke-heating device downstream, discharges the flue gas after Smoke-heating device heats,
Wherein the fluid flow tube of gas cooler connects with the fluid flow tube of Smoke-heating device and forms circulation line.
Smoke processing system the most according to claim 1, also includes:
It is positioned at the air preheater with air pipe line of gas cooler upstream, is positioned at the denitrating flue gas of air preheater upstream
Device and be positioned at the boiler of equipment for denitrifying flue gas upstream, wherein the flue gas from boiler is carried out at denitration by equipment for denitrifying flue gas
Reason, air preheater utilizes the flue gas after denitration that the air in its air pipe line is carried out the pre-heat treatment, wherein air preheater
The combustion chamber of air pipe line and boiler.
Smoke processing system the most according to claim 1, the most each heat-transfer pipe only comprises single fluid flow tube, the ratio of A Yu 2a
Between 1.3 to 2.3 and the ratio of B and 2b is between 2.0 to 4.0.
Smoke processing system the most according to claim 1, the most each heat-transfer pipe includes and only two fluid flow tubes, A and 2a
Ratio between 2.6 to 4.6 and the ratio of B and 2b is between 2.0 to 4.0.
Smoke processing system the most according to claim 1, the equivalent diameter of wherein said ellipse 32mm to 51mm it
Between.
Smoke processing system the most according to claim 1, wherein gap, outside thickness is between 6mm to 12mm.
Smoke processing system the most according to claim 1, the wherein fluid flow tube of gas cooler and/or the material of flue gas fin
Matter selected from carbon steel, ND steel and rustless steel, and flue gas fin and the most independent molding of fluid flow tube and is linked to be one by welding
Body.
8. utilize the method that the smoke processing system of one of claim 1-7 carries out fume treatment, including:
It is passed through recirculated water in the circulation line that the fluid flow tube of gas cooler and the fluid flow tube of Smoke-heating device are formed；
Fume dust remover and flue gas is sequentially entered after the flue gases of about 140 DEG C are cooled to about 90 DEG C by gas cooler
Desulfurizer；
Lead to after flue gas by being lowered the temperature further after flue gas desulfurization device is warming up to about 90 DEG C again by flue gas heater
Cross smoke stack emission；And
Recirculated water is flowed into gas cooler with the temperature cycles being not less than 70 DEG C and flows out to be not less than the temperature cycles of 100 DEG C
Gas cooler.
Method the most according to claim 8, wherein flue gas is cooled to about 50 DEG C further by after flue gas desulfurization device.
Method the most according to claim 8, wherein flue gas comes from the boiler smoke of about 300 DEG C, flows through flue gas desulfurization dress successively
Put and enter before gas cooler and be cooled to about 140 DEG C after air preheater.
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| CN107023818A (en) * | 2017-05-22 | 2017-08-08 | 山西中源科扬节能服务有限公司 | Improved cooling coal economizer for power stations |
| CN109289427A (en) * | 2018-09-06 | 2019-02-01 | 天津大学前沿技术研究院 | Disappear white anti-corrosive apparatus and the method for hot fume |
| CN111981501A (en) * | 2020-07-30 | 2020-11-24 | 中国大唐集团科学技术研究院有限公司西北电力试验研究院 | Anti-blocking heat exchange device of air preheater of pulverized coal boiler |
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| CN106090973B (en) | 2018-04-10 |
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