CN108722162A - A kind of flue gas depth takes off white minimum discharge apparatus and method - Google Patents
A kind of flue gas depth takes off white minimum discharge apparatus and method Download PDFInfo
- Publication number
- CN108722162A CN108722162A CN201810942555.6A CN201810942555A CN108722162A CN 108722162 A CN108722162 A CN 108722162A CN 201810942555 A CN201810942555 A CN 201810942555A CN 108722162 A CN108722162 A CN 108722162A
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- Prior art keywords
- flue gas
- desulfurizing tower
- white
- heat pipe
- heat exchange
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Links
- 239000003546 flue gas Substances 0.000 title claims abstract description 136
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 135
- 238000000034 method Methods 0.000 title claims abstract description 23
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 78
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 238000005507 spraying Methods 0.000 claims abstract description 21
- 230000000694 effects Effects 0.000 claims abstract description 20
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 19
- 230000023556 desulfurization Effects 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 57
- 238000001816 cooling Methods 0.000 claims description 12
- 239000000779 smoke Substances 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 10
- 230000005494 condensation Effects 0.000 claims description 10
- 239000000428 dust Substances 0.000 claims description 10
- 230000003020 moisturizing effect Effects 0.000 claims description 9
- 239000013049 sediment Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 5
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 238000010792 warming Methods 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 2
- 230000005611 electricity Effects 0.000 claims 1
- 230000001105 regulatory effect Effects 0.000 claims 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 abstract description 8
- 235000019504 cigarettes Nutrition 0.000 abstract description 5
- 230000000007 visual effect Effects 0.000 abstract description 4
- 239000013618 particulate matter Substances 0.000 abstract description 2
- 230000001869 rapid Effects 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 3
- 239000003595 mist Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 235000014121 butter Nutrition 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- PZZOEXPDTYIBPI-UHFFFAOYSA-N 2-[[2-(4-hydroxyphenyl)ethylamino]methyl]-3,4-dihydro-2H-naphthalen-1-one Chemical group C1=CC(O)=CC=C1CCNCC1C(=O)C2=CC=CC=C2CC1 PZZOEXPDTYIBPI-UHFFFAOYSA-N 0.000 description 1
- 206010019133 Hangover Diseases 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000012870 ammonium sulfate precipitation Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 230000003116 impacting effect Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000010079 rubber tapping Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- XOSXWYQMOYSSKB-LDKJGXKFSA-L water blue Chemical compound CC1=CC(/C(\C(C=C2)=CC=C2NC(C=C2)=CC=C2S([O-])(=O)=O)=C(\C=C2)/C=C/C\2=N\C(C=C2)=CC=C2S([O-])(=O)=O)=CC(S(O)(=O)=O)=C1N.[Na+].[Na+] XOSXWYQMOYSSKB-LDKJGXKFSA-L 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The invention discloses a kind of flue gas depth to take off white minimum discharge apparatus and method, is related to flue gas after desulfurization deep treatment field, including desulfurizing tower, heat exchange of heat pipe A, air-introduced machine and Tuo Bai devices；The desulfurizing tower includes that desulfurizing tower carries effect tower tray, and desulfurizing tower spraying layer restrains rapid ball condensing unit, demister and desulfurizing tower outlet；The heat exchange of heat pipe A is connect by the air-introduced machine with the desulfurizing tower；In the inside of the desulfurizing tower, it is sequentially arranged the desulfurizing tower from bottom to top and has carried effect tower tray, the desulfurizing tower spraying layer, the rapid ball condensing unit of the tube bank and the demister；The desulfurizing tower is circumscribed with the de- white device, including liquid drop separator, heat exchange of heat pipe B take off white temperature raising wind turbine and the first electric control valve.The present invention realizes flue gas emission particulate matter and is not higher than 5mg/m3, sulfur dioxide is not higher than 35mg/m3.The substantially visible white cigarette of no visual really realizes the requirement of minimum discharge.
Description
Technical field
The present invention relates to flue gas after desulfurization deep treatment fields more particularly to a kind of flue gas depth to take off white minimum discharge device
With method.
Background technology
Former boiler (kiln) flue gas all compares by wet-method desulfurized fume band water, band gypsum rain and sulfate, and dust-laden
It is more serious, while flue gas hangover reaches several kilometers, causes atmosphere pollution.By analysis expert, the substance is to cause haze weather
One of factor.The content of harmful substances from flue gases is reduced, the important topic in flue gas after desulfurization deep treatment field is just become.
Therefore, those skilled in the art is dedicated to developing a kind of smoke gas treatment tapping equipment and method, is promoted in flue gas
Depth dust removing effects.
Invention content
In view of the drawbacks described above of the prior art, the technical problem to be solved by the present invention is to how realize the de- butter depth of water
Spend dust removing effects.
To achieve the above object, the present invention provides a kind of flue gas depth to take off white minimum discharge device, including desulfurizing tower, heat
Heat exchange of heat pipe A, air-introduced machine and Tuo Bai devices；
The desulfurizing tower includes that desulfurizing tower carries effect tower tray, desulfurizing tower spraying layer, restrains rapid ball condensing unit, demister and
Desulfurizing tower exports；
The heat exchange of heat pipe A is connect by the air-introduced machine with the desulfurizing tower；In the inside of the desulfurizing tower, under
It has been sequentially arranged the desulfurizing tower on and and has carried effect tower tray, the desulfurizing tower spraying layer, the rapid ball condensing unit of the tube bank and described
Demister；Between the demister and desulfurizing tower outlet, the desulfurizing tower is circumscribed with the de- white device, including
Liquid drop separator, heat exchange of heat pipe B take off white temperature raising wind turbine and the first electric control valve；The liquid drop separator and the heat pipe
One end of heat exchanger B connects, and the other end of the heat exchange of heat pipe B is connected with the de- white temperature raising wind turbine, described to take off white temperature raising
Wind turbine is connected with first electric control valve again, after de- white temperature raising flue gas is adjusted in first electric control valve,
It is described to take off white temperature raising flue gas into desulfurizing tower outlet, it is discharged after being mixed with main flue gas.
Further, the heat exchange of heat pipe A and heat exchange of heat pipe B is close together；The heat exchange of heat pipe A is height
Heat exchange of heat pipe is warmed, is cooled down to flue gas；The heat exchange of heat pipe B is low temperature heat pipe heat exchanger, is heated to flue gas.
Further, the flue gas circulation of the heat exchange of heat pipe A is 37 ten thousand steres/hour, the heat exchange of heat pipe B
Flue gas circulation be 12 ten thousand steres/hour.
Further, the desulfurizing tower spraying layer is circumscribed with main desulfurization pump and doctor solution plate heat exchanger；The main desulfurization
For the doctor solution of pump discharge after doctor solution plate heat exchanger cooling, the doctor solution enters the institute inside the desulfurizing tower
Desulfurizing tower spraying layer is stated, with heat smoke haptoreaction.
Further, the rapid ball condensing unit of the tube bank is connected to condensate water circulatory storage tank, condensate pump, condensate liquid plate successively
Formula heat exchanger, is attached by pipeline each other, forms a set of circulation condensation device；It is produced after being condensed to flue gas
Flue gas condensing water is flow to described cold by raw condensed water by the liter gas water collector inside the desulfurizing tower by the pipeline
Condensate circulating storage groove is stored, the condensed water in the condensate water circulatory storage tank using the condensate pump pressurization and it is described
After condensate liquid plate heat exchanger carries out cooling, the rapid ball condensing unit of the tube bank is entered by the pipeline and continues cooled flue gas.
Further, the condensate water circulatory storage tank will produce partly precipitated object after recycling for a long time, through pump
Pressurization by the condensate water circulatory storage tank condensed water and sediment be sent to sediment piece-rate system, extra condensed water is by pumping
To advanced treatment of wastewater, the extra condensed water is made as system circulating water moisturizing circulation after being handled using film separation system
With；Water in the condensate water circulatory storage tank is supplemented by technique moisturizing, and the technique moisturizing comes from technique water tank.
Further, the de- white temperature raising wind turbine pressurizes to flue gas, and the air quantity for taking off white temperature raising wind turbine is 120,000
Cube m/h.
Further, the de- white temperature raising wind turbine is also connect with the second electric control valve, second electric control valve pair
It is hot standby that the de- white temperature raising flue gas enters kiln original chimney after being adjusted；The flue gas circulation of first electric control valve
Flue gas circulation for 5-6 ten thousand steres/hour, second electric control valve is 6-7 ten thousand steres/hour.
Further, the height of the desulfurizing tower is 70 meters.
The present invention also provides a kind of methods that flue gas depth takes off white minimum discharge, the described method comprises the following steps：
Step 1, main flue gas exchanged heat into the heat exchange of heat pipe A after by the air-introduced machine enter the desulfurization
Tower, the main flue gas are the flue gas after boiler or kiln dedusting, are 150 DEG C -180 in the temperature for entering the heat exchange of heat pipe A
DEG C, the main flue gas is reduced to 100 DEG C -140 DEG C after heat exchange into the temperature of the desulfurizing tower；
Step 2, the main flue gas pass sequentially through the desulfurizing tower and put forward effect from bottom to top after entering in the desulfurizing tower
Tower tray and the desulfurizing tower spraying layer, after by the desulfurizing tower spraying layer temperature of the main flue gas will drop to 55 DEG C-
65℃；
Step 3, main flue gas continuation pass sequentially through the rapid ball condensing unit of the tube bank and demisting dress from below to up
It sets, carries out condensation desulfurization and dedusting demisting dehydration, condensed -47 DEG C of discharge flue-gas temperature≤45 DEG C, dust content<10mg/
Nm3；
25% to 35% discharge flue gas carries out de- white processing by the de- white device in step 4, the step 3, first
The heat exchange of heat pipe B is entered back by the liquid drop separator, between the discharge flue gas is warming up to 130 DEG C -160 DEG C,
Then it is divided into two-way under white temperature raising fan action in described take off, wherein be connected with first electric control valve all the way, described the
After the de- white temperature raising flue gas is adjusted in one electric control valve, the de- white temperature raising flue gas goes out into the desulfurizing tower
Mouthful, it is discharged after being mixed in step 3 65% to the 75% discharge flue gas, mixed flue-gas temperature is 68
℃-75℃。
The device and method that above-mentioned flue gas depth takes off white minimum discharge are applied in flue gas after desulfurization deep treatment field, hair
It is apparent now to take off butter water depth dust removing effects.Again by transformation condensation inside heat-exchange temperature control, desulfurizing tower and flue gas after desulfurization
The measures such as heating realize flue gas emission particulate matter and are not higher than 5mg/m3, sulfur dioxide is not higher than 35mg/m3.Summer (the 4-10 months)
Condensed smoke temperature reaches 47 DEG C hereinafter, flue gas reduces by 10% or less containing wet；Winter (March next year in November -) condensed smoke temperature
Reach 45 DEG C hereinafter, flue gas contains wet 15% or less.Smog discharge temperature reaches certain critical-temperature or more, and substantially no visual is visible
" white cigarette " really realizes the requirement of minimum discharge, substantially improves atmosphere pollution environment, build clear water blue sky environment.
The technique effect of the design of the present invention, concrete structure and generation is described further below with reference to attached drawing, with
It is fully understood from the purpose of the present invention, feature and effect.
Description of the drawings
Fig. 1 is the overall schematic of the preferred embodiment of the present invention.
Wherein, 1- desulfurizing towers, 101- desulfurizing towers carry effect tower tray, 102- desulfurizing tower spraying layers, the rapid ball condensation dress of 103- tube banks
It sets, 104- demisters, 105- desulfurizing towers outlet, 2- heat exchange of heat pipes A, 3- air-introduced machine, 4- takes off white device, 401- drop separations
Device, 402- heat exchange of heat pipes B, 403- take off white temperature raising wind turbine, the first electric control valves of 404-, the second electric control valves of 5-, 6- master
Desulfurization pumps, 7- doctor solution plate heat exchangers, 8- condensate water circulatory storage tanks, 9- sediment piece-rate systems, 10- advanced treatment of wastewater,
11- technique moisturizings, 12- film separation systems, 13- condensate pumps, 14- condensate liquid plate heat exchangers.
Specific implementation mode
Multiple preferred embodiments that the present invention is introduced below with reference to Figure of description, keep its technology contents more clear and just
In understanding.The present invention can be emerged from by many various forms of embodiments, and protection scope of the present invention not only limits
The embodiment that Yu Wenzhong is mentioned.
In the accompanying drawings, the identical component of structure is indicated with same numbers label, everywhere the similar component of structure or function with
Like numeral label indicates.The size and thickness of each component shown in the drawings are to be arbitrarily shown, and there is no limit by the present invention
The size and thickness of each component.In order to keep diagram apparent, some places suitably exaggerate the thickness of component in attached drawing.
As shown in Figure 1, the higher temperatures main flue gas after boiler (kiln) dedusting, temperature is between 150 DEG C -180 DEG C, first
Make heat exchange into the part lower temperature flue gas after heat exchange of heat pipe A2 and desulfurization, main flue gas is cooled down 40 DEG C -50 DEG C or so,
Main flue gas temperature control enters back into desulfurizing tower 1 at 130 DEG C -140 DEG C or so.Heat exchange of heat pipe A2 passes through air-introduced machine 3 and desulfurization
Tower 1 connects.In desulfurizing tower 1, main flue gas carries effect tower tray 101 by desulfurizing tower from bottom to top, desulfurizing tower spraying layer 102 enters pipe
Beam rapids ball condensing unit 103 is cooled down, and flue gas after cooling carries out demisting using demister 104.Due to the temperature of flue gas
Degree reduces, and the volume of flue gas also accordingly becomes smaller.Into after desulfurizing tower 1, the average upflow velocity of flue gas is also corresponding to become smaller, de-
Under conditions of sulphur section height is constant, using effect tower tray new technology is put forward, so that liquid-gas ratio is substantially reduced, flue gas evaporating capacity is reduced, from root
The generation of the vapour concentration of flue gas is reduced in sheet.Flue-gas temperature will after flue gas rises to desulfurizing tower spraying layer 102 in desulfurizing tower 1
It is down to 65 DEG C or so.If the temperature that flue gas enters desulfurizing tower 1 is 140 DEG C, flue gas rises to desulfurizing tower spray in desulfurizing tower 1
Flue-gas temperature is 55 DEG C after drenching layer 102, and seriously band water enters back into the tube bank rapids ball condensing unit on top to main flue gas at this time with mist
103 and demister 104, carry out condensation desulfurization and dedusting demisting dehydration, condensed discharge flue-gas temperature is at 45 DEG C or so, dust-laden
Concentration<10mg/Nm3, dehydrating demisting reaches industry advanced level.Main flue gas is through the rapid ball condensing unit 103 of tube bank and demister
After 104 processing, reach 47 DEG C hereinafter, flue gas reduces by 10% or less containing wet in summer (the 4-10 months) condensed smoke temperature；Winter (11
The March moon-next year) condensation after smoke temperature reach 45 DEG C hereinafter, flue gas contain wet 15% or less.In summer, although temperature≤45 DEG C, also
In 45 DEG C of saturated humidity.As direct emission also will present white cigarette when temperature is relatively low.
It is discharged from tower top outlet side duct with 30% or so flue gas, carrying out flue gas by de- white device 4 takes off in vain, first
Through flue by liquid drop separator 401, into after heat exchange of heat pipe B402, flue gas is warming up to 145 DEG C or so, and tolerance ratio is about
3:1.Flue gas after heating is divided into two-way after being pressurizeed by de- white temperature raising wind turbine 403, wherein routing the first electric control valve 404 control
System is adjusted, and the flue gas by taking off white temperature raising enters desulfurizing tower outlet 105 and mixes discharge with the main flue gas of 75% or so amount, after mixing
Flue-gas temperature between 68-75 DEG C, water vapour is far from saturation point.Summer smoke stack emission is substantially without visual white cigarette；?
When environment temperature only has -10 DEG C or less, visual white cigarette amount is seldom.Another way is controlled to adjust by the first electric control valve 5, utilizes original
Flue send, hot standby direct exhausting when guarantee kiln emergent hot standby to concrete chimney, guarantee kiln safety operation.
Go out the after cooling in the rapid ball condensing unit 103 of tube bank containing the higher mixed flue gas of steam of desulfurizing tower spraying layer 102
Flue gas condensing water flow in condensate water circulatory storage tank 8 and follows by the liter gas water collector inside desulfurizing tower 1 by condensed water certainly
Ring cooling uses.Partly precipitated object after long-time recycles is sent to sediment piece-rate system 9 through pump pressurization, and condensed water follows
Water in ring storage tank 8 is supplemented by technique moisturizing 11, and technique moisturizing 11 comes from technique water tank.Extra condensate liquid is by being pumped to sewage
Advanced treating 10 using film separation system 12 handle after using the extra condensed water in this part as system circulating water moisturizing circulation
It uses, condenses water zero discharge, do not constitute secondary pollution.
It is pressurizeed by condensate pump 13, is entered by pipeline through 14 condensation cycle liquid after cooling of subcooling condensate plate heat exchanger and taken off
Tube bank rapids ball condensing unit 103 inside sulphur tower 1 continues cycling through the higher containing steam of the cooling outlet of desulfurizing tower spraying layer 102
Mixed flue gas realizes that flue gas cools.
The doctor solution of main 6 outlet of desulfurization pump doctor solution after the cooling of doctor solution plate heat exchanger 7 enters inside desulfurizing tower 1
Desulfurizing tower spraying layer 102, with heat smoke haptoreaction.While desulfuration efficiency raising being reduced due to temperature, the vapour of doctor solution
Rate is reduced, and desulfurizing tower internal steam concentration greatly reduces, and prerequisite is provided in vain for flue gas is de-.
During main smoke airflow is through the rapid ball condensing unit 103 of tube bank and demister 104, condensate water circulatory storage tank 8
The condensed liquid pump 13 of interior circulating condensing liquid pressurizes and after the cooling of subcooling condensate plate heat exchanger 14 through pipeline and nozzle, certainly super
The grade tube bank rapids bottoms ball dedusting demister A are inversely spraying with flue gas flow direction downwards, and a small amount of water mist is acted in main flue gas upflow velocity
Under enter together with main flue gas from the bottoms super tube bank rapids ball dedusting demister A, baffle at bottom effect under make multi-change speed
With deflecting campaign, make between the drop and drop of the different-grain diameter in flue gas, between micronic dust and micronic dust, is sent out between drop and micronic dust
Raw collision, to coalescence, grain size becomes larger, and in the case where the eddy flow power of flue gas is acted on upward towing force, keeps turbulence sphere " public in tube bank
Turn ", so that all turbulence spheres is generated " rotation " in the effect of the lower layer's ball revolution power and frictional force of turbulence sphere.
And flue gas, when impacting turbulence sphere, the water mist in flue gas is attracted on turbulence sphere, and more droplet is adsorbed on
On turbulence sphere, then the surface of turbulence sphere forms moisture film, and more drops, which are adsorbed on, makes the moisture film on turbulence sphere thicken on turbulence sphere
And water droplet is formed, desorption discharge；Micronic dust is equally adsorbed by liquid film, is desorbed with drop and big drop is discharged, under the effect of gravity
The super tube bank rapids ball dedusting demister B that super tube bank rapids ball dedusting demister bottom enters lower part together with spray liquid is discharged,
Clean flue gas is discharged from the super tube bank rapids ball dedusting demister on top, what most low temperature spray liquids took off with top
Drop containing micro grit is mixed with main flue gas adverse current, to absorb the heat in flue gas, makes flue gas cool-down, at the same absorb with it is molten
Enter harmful substance such as SO3, SO2 in flue gas, micronic dust etc., then is removed under the effect of gravity into the super tube bank rapids ball dedusting of lower layer
Day with fog B.
It is and inverse on the one hand due to the continuous variation of air velocity after condensate liquid enters super tube bank rapids ball dedusting demister B
The impact of flowing liquid makes drop generate more another typical material and increase the contact area with main flue gas；On the other hand, turbulator
Surface area it is very big, surface is all that the surface area of liquid film and smoke contacts is also very big, to improve heat of solution absorbing reaction
Efficiency, so that flue gas is sufficiently achieved cooling, the harmful substance in flue gas made fully to be taken away by liquid, contain in temperature-fall period Central Plains
Due to being cooled down, the strain of water vapour liquid phase is removed the flue gas of saturated vapor at water, is finally all flowed under the influence of gravity into
The lower resistance water collector of bottom, then the flow ipe from lower resistance water collector annular groove, be discharged into condensing soln circulating tank after
It is continuous to recycle.
Due to the process also absorption with solution to sulfur dioxide cooled down to flue gas, in condensate water circulatory after gradually concentrating
Bottom has a small amount of ammonium sulfate precipitation object in storage tank 8, and partly precipitated object is sent to film separation system 12 by pumping.
The preferred embodiment of the present invention has been described in detail above.It should be appreciated that the ordinary skill of this field is without wound
The property made labour, which according to the present invention can conceive, makes many modifications and variations.Therefore, all technician in the art
Pass through the available technology of logical analysis, reasoning, or a limited experiment on the basis of existing technology under this invention's idea
Scheme, all should be in the protection domain being defined in the patent claims.
Claims (10)
1. a kind of flue gas depth takes off white minimum discharge device, which is characterized in that including desulfurizing tower, heat exchange of heat pipe A, air-introduced machine and
Take off white device；
The desulfurizing tower includes that desulfurizing tower carries effect tower tray, and desulfurizing tower spraying layer restrains rapid ball condensing unit, demister and desulfurization
Tower exports；
The heat exchange of heat pipe A is connect by the air-introduced machine with the desulfurizing tower；In the inside of the desulfurizing tower, from bottom to top
It has been sequentially arranged the desulfurizing tower and has put forward effect tower tray, the desulfurizing tower spraying layer, the rapid ball condensing unit of the tube bank and the demisting
Device；Between the demister and desulfurizing tower outlet, the desulfurizing tower is circumscribed with the de- white device, including drop
Separator, heat exchange of heat pipe B take off white temperature raising wind turbine and the first electric control valve；The liquid drop separator and the heat pipe heat exchanging
One end of device B connects, and the other end of the heat exchange of heat pipe B is connected with the de- white temperature raising wind turbine, described to take off white temperature raising wind turbine
It is connected with first electric control valve again, it is described after de- white temperature raising flue gas is adjusted in first electric control valve
It takes off white temperature raising flue gas to export into the desulfurizing tower, be discharged after being mixed with main flue gas.
2. flue gas depth as described in claim 1 takes off white minimum discharge device, which is characterized in that the heat exchange of heat pipe A with
The heat exchange of heat pipe B is close together；The heat exchange of heat pipe A is high temperature heat pipe heat exchanger, is cooled down to flue gas；The heat
Heat exchange of heat pipe B is low temperature heat pipe heat exchanger, is heated to flue gas.
3. flue gas depth as described in claim 1 takes off white minimum discharge device, which is characterized in that the heat exchange of heat pipe A's
Flue gas circulation is 37 ten thousand steres/hour, and the flue gas circulation of the heat exchange of heat pipe B is 12 ten thousand steres/hour.
4. flue gas depth as described in claim 1 takes off white minimum discharge device, which is characterized in that outside the desulfurizing tower spraying layer
It is connected to main desulfurization pump and doctor solution plate heat exchanger；The doctor solution of the main desulfurization pump discharge passes through the doctor solution plate-type heat-exchange
After device cooling, the doctor solution enters the desulfurizing tower spraying layer inside the desulfurizing tower, with heat smoke haptoreaction.
5. flue gas depth as described in claim 1 takes off white minimum discharge device, which is characterized in that the rapid ball condensation dress of the tube bank
It sets and is connected to condensate water circulatory storage tank successively, condensate pump, condensate liquid plate heat exchanger is attached by pipeline each other,
Form a set of circulation condensation device；The condensed water generated later is being condensed to flue gas by the liter gas inside the desulfurizing tower
Flue gas condensing water is flow to the condensate water circulatory storage tank by the pipeline and stored by water collector, the condensate water circulatory
After condensed water in storage tank carries out cooling using condensate pump pressurization and the condensate liquid plate heat exchanger, by the pipe
Road enters the rapid ball condensing unit of the tube bank and continues cooled flue gas.
6. flue gas depth as claimed in claim 5 takes off white minimum discharge device, which is characterized in that the condensate water circulatory storage tank
Will produce partly precipitated object after recycling for a long time, through pump pressurization by the condensate water circulatory storage tank condensed water and
Sediment is sent to sediment piece-rate system, and extra condensed water is handled by being pumped to advanced treatment of wastewater using film separation system
The extra condensed water is used as system circulating water moisturizing circulation afterwards；Water in the condensate water circulatory storage tank is mended by technique
Water is supplemented, and the technique moisturizing comes from technique water tank.
7. flue gas depth as described in claim 1 takes off white minimum discharge device, which is characterized in that described to take off white temperature raising wind turbine pair
Flue gas pressurizes, and the air quantity for taking off white temperature raising wind turbine is 12 ten thousand steres/hour.
8. flue gas depth as described in claim 1 takes off white minimum discharge device, which is characterized in that described to take off white temperature raising wind turbine
It is connect with the second electric control valve, second electric control valve enters kiln to described take off after white temperature raising flue gas is adjusted
Former chimney is hot standby；The flue gas circulation of first electric control valve is 5-6 ten thousand steres/hour, second motorized adjustment
The flue gas circulation of valve is 6-7 ten thousand steres/hour.
9. flue gas depth as described in claim 1 takes off white minimum discharge device, which is characterized in that the height of the desulfurizing tower is
70 meters.
10. a kind of method that flue gas depth takes off white minimum discharge, which is characterized in that the described method comprises the following steps：
Step 1, main flue gas exchanged heat into the heat exchange of heat pipe A after by the air-introduced machine enter the desulfurizing tower, institute
It is the flue gas after boiler or kiln dedusting to state main flue gas, is 150 DEG C -180 DEG C in the temperature for entering the heat exchange of heat pipe A, institute
It states temperature of the main flue gas into the desulfurizing tower after heat exchange and is reduced to 100 DEG C -140 DEG C；
Step 2, the main flue gas pass sequentially through the desulfurizing tower and carry effect tower tray from bottom to top after entering in the desulfurizing tower
With the desulfurizing tower spraying layer, the temperature of the main flue gas will drop to 55 DEG C -65 DEG C after by the desulfurizing tower spraying layer；
Step 3, main flue gas continuation pass sequentially through the rapid ball condensing unit of the tube bank and the demister from below to up, into
Row condensation desulfurization and dedusting demisting dehydration, condensed discharge flue-gas temperature is≤45 DEG C -47 DEG C, dust content<10mg/Nm3；
25% to 35% discharge flue gas carries out de- white processing by the de- white device in step 4, the step 3, first passes through
The liquid drop separator enters back into the heat exchange of heat pipe B, between the discharge flue gas is warming up to 130 DEG C -160 DEG C, then
It is divided into two-way under the de- white temperature raising fan action, wherein it is connected with first electric control valve all the way, first electricity
After the de- white temperature raising flue gas is adjusted in dynamic regulating valve, the de- white temperature raising flue gas is exported into the desulfurizing tower, with
65% to the 75% discharge flue gas is discharged after being mixed in step 3, and mixed flue-gas temperature is 68 DEG C -75
℃。
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