CN109569199A - A kind of flue gas processing device - Google Patents
A kind of flue gas processing device Download PDFInfo
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- CN109569199A CN109569199A CN201811141341.5A CN201811141341A CN109569199A CN 109569199 A CN109569199 A CN 109569199A CN 201811141341 A CN201811141341 A CN 201811141341A CN 109569199 A CN109569199 A CN 109569199A
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- heat exchanger
- heat
- flue gas
- solution
- absorption plant
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 81
- 239000003546 flue gas Substances 0.000 title claims abstract description 79
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 92
- 238000010521 absorption reaction Methods 0.000 claims abstract description 84
- 239000007921 spray Substances 0.000 claims abstract description 72
- 239000003517 fume Substances 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims description 25
- 239000007788 liquid Substances 0.000 claims description 20
- 230000001172 regenerating effect Effects 0.000 claims description 17
- 239000000779 smoke Substances 0.000 claims description 16
- 238000005496 tempering Methods 0.000 claims description 15
- 238000009833 condensation Methods 0.000 claims description 13
- 230000005494 condensation Effects 0.000 claims description 13
- 238000001914 filtration Methods 0.000 claims description 12
- 238000005086 pumping Methods 0.000 claims description 7
- 235000019504 cigarettes Nutrition 0.000 claims description 4
- 230000002441 reversible effect Effects 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 239000013589 supplement Substances 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 abstract description 33
- 238000000034 method Methods 0.000 abstract description 12
- 230000008569 process Effects 0.000 abstract description 4
- 230000007704 transition Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 102
- 238000001816 cooling Methods 0.000 description 12
- 230000003009 desulfurizing effect Effects 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 238000004064 recycling Methods 0.000 description 7
- 229920006395 saturated elastomer Polymers 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 238000000605 extraction Methods 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 239000003595 mist Substances 0.000 description 5
- 230000036961 partial effect Effects 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000007701 flash-distillation Methods 0.000 description 3
- 230000002633 protecting effect Effects 0.000 description 3
- 230000002829 reductive effect Effects 0.000 description 3
- 239000012266 salt solution Substances 0.000 description 3
- 238000009938 salting Methods 0.000 description 3
- 238000010025 steaming Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 230000009897 systematic effect Effects 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 230000009194 climbing Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- MXWHMTNPTTVWDM-NXOFHUPFSA-N mitoguazone Chemical compound NC(N)=N\N=C(/C)\C=N\N=C(N)N MXWHMTNPTTVWDM-NXOFHUPFSA-N 0.000 description 1
- 230000003020 moisturizing effect Effects 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 210000002966 serum Anatomy 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000005619 thermoelectricity Effects 0.000 description 1
- 239000002351 wastewater Substances 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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D53/14—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 absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D53/26—Drying gases or vapours
- B01D53/263—Drying gases or vapours by absorption
-
- 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
-
- 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
- B01D53/75—Multi-step processes
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- 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
- F23J15/006—Layout of treatment plant
-
- 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
- F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
-
- 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
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0014—Recuperative heat exchangers the heat being recuperated from waste air or from vapors
-
- 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 processing devices.Reservoir unit is arranged in the device in absorption plant, inner cavity is divided into the first fume treatment area and the second fume treatment area using it, flue gas enters the concentrated solution counter current contacting with absorption plant top spray from the bottom of absorption plant, it is thinning that the concentrated solution in the second fume treatment area absorbs moisture in flue gas, the latent heat discharged in moisture phase transition process is precipitated, heats flue gas and concentrated solution to 55 DEG C -65 DEG C；Concentrated solution after heating draws to enter in First Heat Exchanger by reservoir unit to exchange heat with heat transferring medium (such as hot net water), heat transferring medium can be warmed 3-10 DEG C, concentrated solution is cooled to substantially uniform later into the first fume treatment area with solution inlet port temperature at the top of the second fume treatment area, continue to absorb moisture in flue gas, it is exchanged heat for the first time using step, the quality that heat is changed can be effectively promoted, depth recycles and the sensible heat of former flue gas and the latent heat of neat stress water vapour is utilized.
Description
Technical field
The invention belongs to environmental technology fields, and in particular to a kind of flue gas processing device.
Background technique
It is at present active response " Shanghai City coal-burning power plant gypsum rain and the test of coloured plume with China's expanding economy
Technical requirements (tentative) ", Zhejiang " Emission standards of air pollutants for coal-fired " (solicit meaning original text), Tianjin is " about further
Reinforce notice of the key industrys atmosphere pollution deep treatment such as city's thermoelectricity, steel in relation to work " and Tangshan, Zhang Jia
Mouthful, coloured plume specification is eliminated on the ground such as Handan.The technology path of various Mist heat recoverings is developed, common technology road
Line is to arrange flue gas condenser, spray column after desulfurizing tower or increase slurries cooler on serum recycle slurry pipe to make
Moisture is precipitated in the cooling of desulfurizing tower exiting flue gas, recycles neat stress of the MGGH system after former fume afterheat thermal dehydration.
Above-mentioned flue gas condensing or flue gas condensing regeneration techniques route, can not deep exploitation original flue gas sensible heat and neat stress
A large amount of latent heat of middle water vapour.Meanwhile it is latent need to take away flue gas condensing in order to be dehydrated flue gas cool-down with extraneous refrigerant for above-mentioned technology
Heat, later again with former obvious heat of smoke heating neat stress to promote degree of unsaturation and climbing ability, this mode causes pole to the energy
Big waste.Flue gas condensing discharges latent heat simultaneously, and takes away this part latent heat and need a large amount of cooling circulating water, which is mesh
Preceding every kind of technology path requires the problem of facing, especially for the area of regulation desulfurizing tower outlet smoke temperature and water capacity, no
But winter needs to condense or even summer is also required to flue gas condensing, and cooling tower is often oepration at full load when power plant's summer, can not
Effective cold source is provided, if newly-built cooling tower, needs to increase several ten million investments, while the moisture for evaporating cooling tower gains flue gas
In waste water, do not have water-saving result.If newly-built induced cooling tower, construction cost is high, unbearable to power plant.
Summary of the invention
Therefore, existing the technical problem to be solved by the present invention is to the technology path of existing Mist heat recovering can not depth benefit
With a large amount of latent heat of water vapour in the sensible heat and neat stress of former flue gas, while the energy and water resource waste, cost of investment are big, eliminate
Coloured plume only has the defect for investing not income, to propose a kind of flue gas processing device.
For this purpose, the technical solution that the application takes is,
A kind of flue gas processing device, including absorption plant further include,
Reservoir unit is set in the absorption plant, and its inner cavity is divided into the first fume treatment area and the second flue gas
Treatment region, flue gas are suitable for entering second fume treatment area from first fume treatment area by the reservoir unit；
First Heat Exchanger, liquid feeding end are connected to the reservoir unit, and outlet end is close to the reservoir unit and described the
One fume treatment area connection, so that the solution in the reservoir unit enters heat exchange in the First Heat Exchanger, and will be after heat exchange
Solution be sent into first fume treatment area and smoke contacts.
It further, further include regenerative system, the regenerative system includes,
Dilute solution inlet and steam (vapor) outlet is arranged in flash tank, upper part, and lower part is arranged concentrated solution and exports；
6th heat exchanger, the lower part of the absorption plant, the 6th heat exchanger and dilute solution inlet are sequentially communicated；
Compressor and saturator, the steam (vapor) outlet, compressor, saturator and the 6th heat exchanger are sequentially communicated, so that dilute
After solution and secondary steam exchange heat in the 6th heat exchanger, into the flash tank.
Further, further include the first spray unit, in the inner close to the setting of the middle and upper part of the absorption plant, and be located at
The top of the reservoir unit, concentrated solution outlet, the 5th heat exchanger and the first spray unit are sequentially communicated setting, after exchanging heat
Concentrated solution by first spray unit spray on the flue gas of rising；
Second spray unit is set in the absorption plant, the storage close to the reservoir unit and being disposed below
Liquid unit, First Heat Exchanger and the second spray unit are sequentially communicated setting, after exchanging heat with the solution after smoke contacts, then spray
Drench on neat stress, with neat stress reverse convection.
Further, the lower part of the absorption plant, the 5th heat exchanger, the 6th heat exchanger and dilute solution inlet successively connect
It is logical, to exchange heat in the concentrated solution in the 5th heat exchanger with the concentrated solution outlet from flash tank, then through the 6th heat exchange
After device heat exchange, it is finally sent into the flash tank.
It further, further include the second heat exchanger, the lower part of the absorption plant, the second heat exchanger and the second spray unit
It is sequentially communicated setting, weak solution is sent into second spray unit after exchanging heat；
Solution filters tempering system, and the lower part of the absorption plant, solution filter tempering system, the second heat exchanger and second
Spray unit is sequentially communicated setting, is sent into second spray unit after weak solution is filtered quenched and heat exchange.
It further, further include third heat exchanger and the 4th heat exchanger, the First Heat Exchanger, the second heat exchanger, third
Heat exchanger and the 4th heat exchanger are sequentially communicated, so that heat supply network water or low pressure condensation water pass sequentially through the First Heat Exchanger,
Two heat exchangers, third heat exchanger and the 4th heat exchanger, and exchange heat to the substance entered in corresponding heat exchanger.
Further, the 6th heat exchanger is connected to the third heat exchanger and the 4th heat exchanger respectively, will be described
After the pumping condensed water of 6th heat exchanger is sent into the third heat exchanger heat exchange, back boiler water supply, by the 6th heat exchanger
After secondary steam condensed water is sent into the 4th heat exchanger heat exchange, water is supplemented as technique；
The steam (vapor) outlet is also connected to the 4th heat exchanger, by secondary steam be sent into the 4th heat exchanger into
Row heat exchange.
Further, gas inlet is arranged in the lower part of the absorption plant, and exhanst gas outlet, first spray is arranged in top
Unit, the reservoir unit and second spray unit are respectively positioned between the gas inlet and exhanst gas outlet.
Further, the absorption plant lower part and second heat exchanger or second heat exchanger and the second spray
The first pump of setting between unit；
The absorption plant lower part and solution filtering tempering system or solution filtering tempering system and described the
The second pump of setting between two heat exchangers or second heat exchanger and second spray unit；
The absorption plant lower part and the 5th heat exchanger or the 5th heat exchanger and the 6th heat exchanger, or
Third is arranged between 6th heat exchanger and the flash tank to pump；
The concentrated solution outlet and setting the 4th between the 5th heat exchanger or the 5th heat exchanger and the first spray unit
Pump.
Technical solution of the present invention has the advantages that
1, reservoir unit is arranged in absorption plant, is divided into inner cavity using it for flue gas processing device provided by the invention
First fume treatment area and the second fume treatment area, flue gas enter dense with absorption plant top spray from the bottom of absorption plant
Solution (such as dense saline solution) counter current contacting, it is thinning that the concentrated solution in the second fume treatment area absorbs moisture in flue gas, and moisture phase is precipitated
The latent heat discharged during becoming heats flue gas and concentrated solution to 55 DEG C -65 DEG C；Concentrated solution after heating is drawn by reservoir unit
It exchanges heat into First Heat Exchanger with heat transferring medium (such as hot net water), heat transferring medium can be warmed 3-10 DEG C, and concentrated solution is cooled to
It is substantially uniform later into the first fume treatment area with solution inlet port temperature at the top of the second fume treatment area, continue to absorb in flue gas
Moisture is exchanged heat using step for the first time, can effectively be promoted the quality that heat is changed, be recycled eventually by above-mentioned means depth and original is utilized
The sensible heat of flue gas and the latent heat of neat stress water vapour avoid the condensation of prior art flue gas cool-down from needing a large amount of cold sources, greatly save
Water resource.Moisture in neat stress has been recycled simultaneously, systematic running cost has been reduced and uses, and solves coal-burning power plant or other industry is eliminated
Coloured plume, depth water pumping system is only put into does not have the problem of income, reaches the environment protectings such as efficient energy-saving and emission-reducing, is had fine
Social and economic effect.
2, the aqueous of neat stress is greatly lowered first with absorption plant for flue gas processing device provided by the invention
Rate, steam in by concentrated solution absorption process since phase transformation discharges latent heat, can so that the mass dryness fraction and temperature of neat stress are improved
Reach simultaneously and eliminates that coloured plume, depth water lift, water vapour is low-quality latent in the dustiness for reducing neat stress and recycling neat stress
The effect of heat；Then the concentrated solution after absorbing vapor in absorption plant becomes weak solution, and a part passes through the in weak solution
The cooling of five heat exchangers, then restored by regenerative system to original content, it finally returns to the second fume treatment area；Another part passes through
Second heat exchanger heats heat transferring medium (such as hot net water), returns again to the first fume treatment area, two strands of uninterrupteds are according to specific
It is required that adjustment, the water absorbing capacity of unit mass concentrated solution can be changed by adjusting two-way flow-rate ratio；In addition, it is sent to regenerative system
In weak solution become concentrated solution by the way that flash regeneration in flash tank is exchanged heat and entered with the saturated vapor that regenerative system generates, then
It being transported in absorption plant, the saturated vapor generated after the compression of the secondary steam at the top of regenerative system is utilized in regenerative process,
The saturated vapor of release latent heat becomes secondary steam condensed water, which is again introduced into the 4th heat exchanger and heat supply network
Water heat exchange, the condensed water after cooling can be used for desulfurizer mist eliminator flushing water or as technique supplement water etc., reduce into
Sheet and energy consumption.It avoids regeneration using power plant steam, can effectively reduce steam consumption.
3, flue gas processing device provided by the invention, regenerative system heating season are evacuated come steam pumping using steam turbine, are evacuated cold
Condensate is after the heat exchange of third heat exchanger, back boiler water supply；Non- heating season uses compressor+secondary steaming of saturator+flash column
Vapour, the saturated vapor generated after compression, condensed water are used for the moisturizing of desulfurizer technique.Hot net water or low pressure condensation water pass through absorption
The First Heat Exchanger of device and the second heat exchanger heat exchange heating and then third heat exchanger and the 4th heat exchanger with regenerative system
Heat exchange, heating season reach hot net water temperature requirement, heating season backheat net；Non- heating season go it is low plus or go low-level (stack-gas) economizer exchange heat after
Go again it is low plus, can be used for heating low pressure condensation water, keep non-heating season unit generation ability unaffected.It solves in the above manner
Coal-burning power plant or other industry eliminate that wet plume, depth water pumping system is only put into does not have the problem of income, pass through compressor+saturation
Device+flash distillation Tower System further recycles the latent heat of neat stress water vapour after desulfurizer, recycles moisture in neat stress, reduces system
System operating cost, reaches the environment protectings such as efficient energy-saving and emission-reduction.
4, former obvious heat of smoke not only can be used to heat hot net water or low plus solidifying by flue gas processing device provided by the invention
It bears water, a large amount of latent heat of water vapour in acceptable recovered flue gas simultaneously, depth Mist heat recovering, due to cigarette during recycling latent heat
Temperature degree raises simultaneously, and can reduce flue gas moisture content simultaneously and improve flue-gas temperature, reaches recycling latent heat collaboration and eliminates coloured cigarette
Plumage and reduction dust content effect.The device recycles saving water resource by depth water lift, since system equipment is simple,
System operation pressure drop about one third can be reduced compared with presently relevant technology, save operating cost, there is environmental protection section well
It can effect.
Detailed description of the invention
It, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical solution in the prior art
Embodiment or attached drawing needed to be used in the description of the prior art be briefly described, it should be apparent that, it is described below
Attached drawing is some embodiments of the present invention, for those of ordinary skill in the art, before not making the creative labor
It puts, is also possible to obtain other drawings based on these drawings.
Fig. 1 is the layout drawing of flue gas processing device in the embodiment of the present invention；
Fig. 2 is the layout drawing of smoke processing system in the embodiment of the present invention；
Fig. 3 is the system diagram of smoke processing system in the embodiment of the present invention；
Fig. 4 is the structural schematic diagram of absorption plant in the embodiment of the present invention；
Fig. 5 is the structural schematic diagram of regenerative system in the embodiment of the present invention；
Wherein appended drawing reference indicates are as follows:
1- dust-extraction unit；2- desulfurizer；3- absorption plant；The first spray unit of 3-1-；The second spray unit of 3-2-；3-
3- reservoir unit；3-4- gas inlet；3-5- exhanst gas outlet；3-6- demister；4- economizer；5- first is pumped；6- second is pumped；7-
Solution filters tempering system；8- First Heat Exchanger；The second heat exchanger of 9-；10- third heat exchanger；The 4th heat exchanger of 11-；12-
Three pumps；The 5th heat exchanger of 13-；14- the 4th is pumped；15- compressor；16- saturator；The 6th heat exchanger of 17-；18- flash tank；19-
Chimney；The 7th heat exchanger of 20-；21- solution supplements tank；22- the 5th is pumped.
Specific embodiment
Technical solution of the present invention is clearly and completely described below, it is clear that described embodiment is the present invention
A part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art are not having
Every other embodiment obtained under the premise of creative work is made, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that term " center ", "upper", "lower", "left", "right", "vertical",
The orientation or positional relationship of the instructions such as "horizontal", "inner", "outside" be based on the orientation or positional relationship shown in the drawings, merely to
Convenient for description the present invention and simplify description, rather than the device or element of indication or suggestion meaning must have a particular orientation,
It is constructed and operated in a specific orientation, therefore is not considered as limiting the invention.In addition, term " first ", " second ",
" third " is used for descriptive purposes only and cannot be understood as indicating or suggesting relative importance.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " installation ", " phase
Even ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or be integrally connected；It can
To be mechanical connection, it is also possible to be electrically connected；It can be directly connected, can also can be indirectly connected through an intermediary
Connection inside two elements.For the ordinary skill in the art, above-mentioned term can be understood at this with concrete condition
Concrete meaning in invention.
As long as in addition, the non-structure each other of technical characteristic involved in invention described below different embodiments
It can be combined with each other at conflict.
Embodiment 1
A kind of flue gas processing device is present embodiments provided, as shown in Figure 1, including absorption plant 3, as absorption plant 3 can
For absorption tower, gas inlet 3-4 is arranged in the lower part of absorption plant 3, and it further includes reservoir unit 3- that exhanst gas outlet 3-5, which is arranged, in top
3, such as reservoir unit 3-3 can be liquid dish, as shown in figure 4, liquid dish has the disk being adapted with desulfurizing tower inner cavity, disk
On open up through-hole, along the axial direction of desulfurizing tower, through-hole has the extended segment that extends to desulfurization column overhead, is between adjacent extended segment
Reservoir space is set in absorption plant 3, and its inner cavity is divided into the first fume treatment area and the second fume treatment area, flue gas
Suitable for entering the second fume treatment area from the first fume treatment area by reservoir unit 3-3；Specifically, reservoir unit 3-3 can be set
It is placed in the middle part of desulfurizing tower；
First Heat Exchanger 8, liquid feeding end are connected to reservoir unit 3-3, and outlet end is close to reservoir unit 3-3 and the first flue gas
Treatment region connection so that the solution of 3-3 enters heat exchange in First Heat Exchanger 8 in reservoir unit, and the solution after heat exchange is sent into
First fume treatment area and smoke contacts.
In addition, this application provides the smoke processing systems including above-mentioned flue gas processing device, and as shown in Figures 2 and 3, the cigarette
Gas processing system includes the dust-extraction unit 1, desulfurizer 2 and absorption plant 3 for being sequentially communicated setting, if dust-extraction unit 1 can be electricity
Deduster, desulfurizer 2 can be desulfurizing tower.
In above-mentioned flue gas processing device, reservoir unit 3-3 is set in absorption plant 3, inner cavity is divided into first using it
Fume treatment area and the second fume treatment area, flue gas enter dense molten with 3 top spray of absorption plant from the bottom of absorption plant 3
Liquid (such as dense saline solution) counter current contacting, it is thinning that the concentrated solution in the second fume treatment area absorbs moisture in flue gas, and moisture phase transformation is precipitated
The latent heat discharged in the process heats flue gas and concentrated solution to 55 DEG C -65 DEG C；Concentrated solution after heating is drawn by reservoir unit 3-3
Enter in First Heat Exchanger out and exchange heat with heat transferring medium (such as hot net water), heat transferring medium can be warmed 3-10 DEG C, concentrated solution cooling
It is extremely substantially uniform later into the first fume treatment area with solution inlet port temperature at the top of the second fume treatment area, continue to absorb flue gas
Middle moisture is exchanged heat using step for the first time, can effectively be promoted the quality that heat is changed, be recycled and be utilized eventually by above-mentioned means depth
The sensible heat of former flue gas and the latent heat of neat stress water vapour avoid the condensation of prior art flue gas cool-down from needing a large amount of cold sources, save significantly
About water resource.Moisture in neat stress has been recycled simultaneously, is reduced systematic running cost and is used, solves coal-burning power plant or other industry disappears
Except coloured plume, depth water pumping system is only put into does not have the problem of income, reaches the environment protectings such as efficient energy-saving and emission-reducing, is had very
Good social and economic effect.
Further, as shown in figure 5, further including regenerative system, regenerative system includes flash tank 18, and upper part setting is dilute molten
Liquid import and steam (vapor) outlet, lower part are arranged concentrated solution and export；6th heat exchanger 17, the lower part of absorption plant 3, the 6th heat exchanger 17
It is sequentially communicated with dilute solution inlet；Compressor 15 and saturator 16, steam (vapor) outlet, compressor 15, saturator 16 and the 6th heat exchange
Device 17 is sequentially communicated, so that after weak solution and secondary steam exchange heat in the 6th heat exchanger 17, into flash tank 18.
In addition, the driving heat source heating season of regenerative system is machine assembly air-exhausting；Non- heating season uses compressor+saturator+sudden strain of a muscle
The saturated vapor that the secondary steam of tower generates is steamed, compressor+saturator+flash distillation Tower System can make non-heating season unit generation ability
It is unaffected.Not equality of temperature is heated to by heat supply network heat exchanger in Various Seasonal hot net water or circulation heat medium water or low pressure condensation water
Degree.
It in the present embodiment, further include the first spray unit 3-1, in the inner close to the setting of the middle and upper part of absorption plant 3, and
Positioned at the top of reservoir unit 3-3, concentrated solution outlet, the 5th heat exchanger 13 and the first spray unit 3-1 are sequentially communicated setting, with
Concentrated solution after heat exchange is sprayed by the first spray unit 3-1 on the flue gas of rising；Second spray unit 3-2, close to storage
Liquid unit 3-3 and being disposed below is set in absorption plant 3, reservoir unit 3-3, First Heat Exchanger 8 and the second spray unit
3-2 is sequentially communicated setting, by with after the solution heat exchange after smoke contacts, then sprays on neat stress, with reverse with neat stress
Convection current；Specifically, the first spray unit 3-1 and the second spray unit 3-2 includes the spray for spraying conduit and being arranged on interval
Mouth is drenched, and the first spray unit 3-1 and the second spray unit 3-2 are close to the exhanst gas outlet 3-5 of absorption plant 3 and are located under it
Side, in this way extension counter current contacting distance, can heat in effective recovered flue gas.
Specifically, the lower part of absorption plant 3, the 5th heat exchanger 13, the 6th heat exchanger 17 and dilute solution inlet are sequentially communicated,
Absorbing tower bottom solution to be exchanged heat in the concentrated solution in the 5th heat exchanger 13 with the concentrated solution outlet from flash tank, then through the
After the heat exchange of six heat exchangers 17, it is finally sent into flash tank 18；5th heat exchanger 13 can be plate heat exchanger；
In addition, also setting up the 7th heat exchanger 20, the concentrated solution come out out of the 5th heat exchanger 13 can enter the 7th heat exchanger
20, with after hot net water or the heat exchange of low plus condensed water, enter back into absorption plant.
Embodiment 2
A kind of flue gas processing device is present embodiments provided, on the basis of above-described embodiment 1, in order to improve heat exchange effect
Fruit, sufficiently recycles the latent heat of the sensible heat and neat stress water vapour in former flue gas, and waste liquid is sufficiently regenerated, and further includes the second heat exchange
Device 9, the lower part of absorption plant 3, the second heat exchanger 9 and the second spray unit 3-2 are sequentially communicated setting, by weak solution through exchanging heat
After be sent into the second spray unit 3-2；Meanwhile in order to which the concentrated solution in absorption plant as absorbing liquid is filtered and is modulated,
It further include solution filtering tempering system 7, lower part, solution filtering tempering system 7, the second heat exchanger 9 and the second spray of absorption plant 3
Leaching unit 3-2 is sequentially communicated setting, is sent into the second spray unit 3-2 after weak solution is filtered quenched and heat exchange；Specifically,
As shown in figure 3, solution filtering tempering system 7 be made of the cyclone+filter being sequentially communicated, while setting be sequentially communicated it is molten
Liquid supplements tank 21 and the 5th pump 22, and the 5th pump 22 is connected to solution filtering tempering system 7, with make-up solution into it.
Embodiment 3
A kind of flue gas processing device is present embodiments provided, further includes that third is changed on the basis of above-described embodiment 1 or 2
Hot device 10 and the 4th heat exchanger 11, First Heat Exchanger 8, the second heat exchanger 9, third heat exchanger 10 and the 4th heat exchanger 11 successively connect
It is logical, so that heat supply network water or low pressure condensation water pass sequentially through First Heat Exchanger 8, the second heat exchanger 9, third heat exchanger 10 and the 4th
Heat exchanger 11, and exchange heat to the substance entered in corresponding heat exchanger；
Further, the 6th heat exchanger 17 is connected to third heat exchanger 10 and the 4th heat exchanger 11 respectively, and the 6th is changed
After the pumping condensed water of hot device 17 is sent into the heat exchange of third heat exchanger 10, back boiler water supply, by the secondary steam of the 6th heat exchanger 17
After condensed water is sent into the heat exchange of the 4th heat exchanger 10, water is supplemented as technique；Steam (vapor) outlet is also connected to the 4th heat exchanger 11, will
Secondary steam is sent into the 4th heat exchanger 11 and exchanges heat；
In order to realize the flowing of liquid, 3 lower part of absorption plant and the second heat exchanger 9 or the second heat exchanger 9 and the second spray
The first pump 5 of setting between unit 3-2；3 lower part of absorption plant and solution filtering tempering system 7 or solution filtering tempering system 7 with
The second pump 6 of setting between second heat exchanger 9 or the second heat exchanger 9 and the second spray unit 3-2；3 lower part of absorption plant and the 5th
Third is arranged between heat exchanger 13 or the 5th heat exchanger 13 and the 6th heat exchanger 17 or the 6th heat exchanger 17 and flash tank 17 to pump
12；Concentrated solution outlet and the 4th pump 14 of setting between the 5th heat exchanger 13 or the 5th heat exchanger 13 and the first spray unit 3-1.
It is used to supply in addition, hot net water is promoted to 85 DEG C or so into the 4th heat exchanger by the secondary steam of flash drum overhead
It is warm；The heating of secondary steam compression+saturation steam is entered plate-type heat-exchange using compressor+saturator+flash column by non-heating season
Hot net water (low pressure condensation water) can be heated to 60 DEG C or so by the weak solution of device, condensed water, for heating low pressure condensation water, be led to
Crossing such method of operation can make non-heating season air exhaust energy consumption cancel out each other with recycling energy consumption, not generate negatively to unit generation ability
It influences.The concentrated solution of flash tank bottom in the 5th heat exchanger 13 (dilute concentrated solution heat exchanger) with weak solution exchange heat, then again with
Absorption tower top is back to after 7th heat exchanger (heat exchange of concentrated solution heat exchanger).Non- heating season secondary steam is arranged from regenerator overhead
Enter compressor out, becomes superheated steam through heating, become saturated vapor by spray, as regenerator driving heat source,
Become condensed water after release latent heat, which exchanges heat with third heat exchanger again.
Embodiment 4
A kind of flue gas processing device is present embodiments provided, on the basis of above-described embodiment 1,2 or 3, as shown in Fig. 2,
Smoke processing system including the flue gas processing device in the present embodiment further includes economizer 3-6, be set to dust-extraction unit 1 with
Between desulfurizer 2 or between air preheater and dust-extraction unit 1, the 4th heat exchanger 11 is connected to economizer 3-6, by condensed water
It exchanges heat in economizer 3-6 with the flue gas from dust-extraction unit 1, and the flue gas after heat exchange is sent into desulfurizer 2.
Further, gas inlet 3-4 is arranged in the lower part of absorption plant 3, and exhanst gas outlet 3-5, exhanst gas outlet is arranged in top
3-5 is connected to chimney 19, and the first spray unit 3-1, reservoir unit 3-3 and the second spray unit 3-2 are respectively positioned on gas inlet 3-4
Between exhanst gas outlet 3-5；Demister 3-6 is set in absorption plant 3, and is located at the first spray unit 3-1 and exhanst gas outlet
Between 3-5.
If desired smoke temperature is promoted to higher temperature, can be arranged on flue behind the exhanst gas outlet 3-4 of absorption plant 3
Heat exchanger or the inner-heating tube at the top of 3 upper section of absorption plant again, by the temperature that smoke temperature is heated to environmental protection or owner needs.
Embodiment 5
A kind of flue gas processing device is present embodiments provided, on the basis of above-described embodiment 1,2,3 and 4, in order to adapt to
Non- heating season, absorption plant can spray flue gas using recirculated cooling water as traditional spray column in absorption plant, can
Make system flexible modulation smoke processing system, energy saving, the fume treatment system including the flue gas processing device in the present embodiment
System, spray column are directly connected to the exhanst gas outlet of desulfurizer 2, can be cold using salting liquid or circulation as needed in the course of work
But switch spray between water, when switching to recirculated cooling water spray, system becomes spray system, by the upper of absorption plant
Lower section sprays low-temperature cooling water, saturated flue gas and shower water heat and mass, flue-gas temperature summer is down to 48 DEG C, winter is down to 45
DEG C, shower water and the heat exchange of low plus condensed water of tower bottom are sprayed, reduces machine assembly air-exhausting, the shower water after exchanging heat is back to spray again
It drenches in tower；Or the shower water of spray tower bottom is sent to cold water tower cooler, recycling after cooling.
In addition, the specific working principle of above-mentioned apparatus is as follows:
As illustrated in fig. 1 and 2, flue gas enters and the dense saline solution of absorption tower top spray adverse current, absorption from absorb the bottom of the tower
Moisture is thinning in dense saline solution absorption flue gas at the top of tower upper section, is precipitated in moisture phase transition process and discharges latent heat, heats flue gas and salt
Solution is to 55 DEG C -65 DEG C.Solution after heating is drawn by upper section bottom liquid dish enters First Heat Exchanger (heat supply network level-one heat exchange
Device) exchange heat with hot net water, hot net water can be warmed 3-10 DEG C, salting liquid be cooled to it is consistent with solution inlet port temperature at the top of upper section it
Enter at the top of the lower section of absorption tower afterwards, continues to absorb moisture in flue gas, absorption tower lower section bottom weak solution is respectively by first pump (dilute salt
Solution pump) it is sent to the second heat exchanger (heat supply network secondary heat exchanger) and the 5th heat exchanger (dilute concentrated solution heat exchanger), the first heat exchange out
The hot net water of device (heat supply network first-class heat exchanger) and the weak solution for entering the second heat exchanger (heat supply network secondary heat exchanger) exchange heat, by lower section
It is consistent that bottom weak solution is cooled to First Heat Exchanger taphole temperature, and exports with First Heat Exchanger (heat supply network first-class heat exchanger)
Solution is mixed into absorption tower lower section top spray, and hot net water is heated to 50-60 DEG C；Into the 5th heat exchanger (dilute concentrated solution
Heat exchanger) weak solution with from regenerative system come concentrated solution heat exchange after enter regenerative system.It is dilute after being heated through concentrated solution
Solution enter the 6th heat exchanger (plate heat exchanger) be continuously heating to 120 DEG C -140 DEG C (heat source be heating season using pump group steaming
Vapour, non-heating season pass through compressor+saturator+flash column secondary steam), then carry out flash tank flash distillation.When heating season, take out
Air cooling condensate enters third heat exchanger 10 (heat supply network three-level heat exchanger) and exchanges heat with hot net water, the secondary steam of flash drum overhead
Hot net water 85 DEG C or so are promoted into the 4th heat exchanger 11 (heat supply network level Four heat exchanger) to be used to heat；Non- heating season utilizes pressure
The heating of secondary steam compression+saturation steam is entered the dilute of the 6th heat exchanger (plate heat exchanger) by contracting machine+saturator+flash column
Solution, flash vessel top secondary steam temperature is about 95 DEG C -110 DEG C, is determined by concentration of salt solution used and water absorption, secondary steaming
Vapour enters the superheated steam of compressor compresses to 300 DEG C or so from flash drum overhead, becomes temperature about 130 by spray saturation
DEG C -150 DEG C of saturated vapor, hot net water (low pressure condensation water) can be heated to 57 DEG C -70 DEG C or so by condensed water, for heating
Low pressure condensation water, or it is connected with low low-level (stack-gas) economizer, its temperature is continued to lift up to 65 DEG C -85 DEG C.Condensation after cooling
Water can be used for desulfurizer mist eliminator flushing water etc..Beginning sorption type heat pump system COP can be made to be promoted to 3- by such method of operation
4, non-heating season air exhaust energy consumption can be made to cancel out each other with recycling energy consumption, do not had a negative impact to unit generation ability.Flash tank
The concentrated solution of bottom exchanges heat in the 5th heat exchanger (dilute concentrated solution heat exchanger) with weak solution, then passes through concentrated solution cooling heat exchanger
It is cooled to 30 DEG C -50 DEG C and is back to recycling at the top of the upper section of absorption tower.
Specifically, desulfurizing tower lower section bottom solution is divided into three parts: first part returns after exchanging heat with heat supply network secondary heat exchanger
It returns and forms partial circulating at the top of the lower section of absorption tower；Second part enters regenerative system after being sent to dilute concentrated solution heat exchanger heating；
On the one hand Part III, which enters the quenched unit of solution filtering, can pass through rotation in the quenched unit of absorption tower lower section bottom ancillary filter
Flow crystal salt (sulfate, carbonate that device+filter device removes the solution solid particulate matter accumulated in absorption tower and generation
Deng) etc. substances, the pollutant for making absorption tower solution and Control of Impurities are to a certain degree；On the other hand calcium base salt is added, adjusts molten
The pH of liquid, keeps the absorbability of solution, while reducing the corrosivity of solution.Absorbing liquid enters at the top of absorption tower, by equal
Even spray and the neat stress reverse convection entered from absorb the bottom of the tower, water vapour is absorbed by concentrated solution in neat stress, upper section and under
The respective settable spare level of spraying layer of section, to improve the reliability on absorption tower.By adjusting absorption tower lower section partial circulating solution
The water absorbing capacity for measuring controllable unit mass salting liquid, arranges absorption tower, since absorb the bottom of the tower flue gas contains after desulfurizing tower
Water rate is high, and most of water suction occurs in this section, partial circulating is arranged in absorb the bottom of the tower, by reducing the control of partial circulating solution temperature
Lower section equilibrium temperature in absorption tower processed, to improve the water absorbing capacity of unit mass solution, the weak solution concentration after absorption is relatively dense
The ratio of solution reduction 1%-10%, partial circulating internal circulating load and regeneration cycle amount can be in 1:1-10:1.Desulfurizing tower in original system
It is not required to do any transformation, it includes single column Two-way Cycle and double tower binary cycle system which, which is suitable for desulfurization Tower System,.
Obviously, the above embodiments are merely examples for clarifying the description, and does not limit the embodiments.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of variation or
It changes.There is no necessity and possibility to exhaust all the enbodiments.And it is extended from this it is obvious variation or
It changes still within the protection scope of the invention.
Claims (10)
1. a kind of flue gas processing device, including absorption plant, which is characterized in that further include,
Reservoir unit is set in the absorption plant, and its inner cavity is divided into the first fume treatment area and the second fume treatment
Area, flue gas are suitable for entering second fume treatment area from first fume treatment area by the reservoir unit；
First Heat Exchanger, liquid feeding end are connected to the reservoir unit, and outlet end is close to the reservoir unit and first cigarette
Gas disposal area connection, so that the solution in the reservoir unit enters heat exchange in the First Heat Exchanger, and will be molten after heat exchange
Liquid is sent into first fume treatment area and smoke contacts.
2. flue gas processing device according to claim 1, which is characterized in that it further include regenerative system, the regenerative system
Including,
Dilute solution inlet and steam (vapor) outlet is arranged in flash tank, upper part, and lower part is arranged concentrated solution and exports；
6th heat exchanger, the lower part of the absorption plant, the 6th heat exchanger and dilute solution inlet are sequentially communicated；
Compressor and saturator, the steam (vapor) outlet, compressor, saturator and the 6th heat exchanger are sequentially communicated, so that weak solution
After exchanging heat in the 6th heat exchanger with secondary steam, into the flash tank.
3. flue gas processing device according to claim 2, which is characterized in that further include,
First spray unit in the inner close to the setting of the middle and upper part of the absorption plant, and is located at the top of the reservoir unit,
Concentrated solution outlet, the 5th heat exchanger and the first spray unit are sequentially communicated setting, and the concentrated solution after exchanging heat passes through described the
One spray unit is sprayed on the flue gas of rising；
Second spray unit is set in the absorption plant, the reservoir list close to the reservoir unit and being disposed below
Member, First Heat Exchanger and the second spray unit are sequentially communicated setting, after exchanging heat with the solution after smoke contacts, then spray in
On neat stress, with neat stress reverse convection.
4. flue gas processing device according to claim 3, which is characterized in that the lower part of the absorption plant, the 5th heat exchange
Device, the 6th heat exchanger and dilute solution inlet are sequentially communicated, to go out in the 5th heat exchanger with the concentrated solution from flash tank
The concentrated solution heat exchange of mouth, then after the 6th heat exchanger heat exchange, finally it is sent into the flash tank.
5. flue gas processing device according to claim 3 or 4, which is characterized in that further include,
Second heat exchanger, the lower part of the absorption plant, the second heat exchanger and the second spray unit are sequentially communicated setting, will be dilute
Solution is sent into second spray unit after exchanging heat；
Solution filters tempering system, lower part, solution filtering tempering system, the second heat exchanger and the second spray of the absorption plant
Unit is sequentially communicated setting, is sent into second spray unit after weak solution is filtered quenched and heat exchange.
6. flue gas processing device according to claim 5, which is characterized in that further include,
Third heat exchanger and the 4th heat exchanger, the First Heat Exchanger, the second heat exchanger, third heat exchanger and the 4th heat exchanger according to
Secondary connection so that heat supply network water or low pressure condensation water pass sequentially through the First Heat Exchanger, the second heat exchanger, third heat exchanger and
4th heat exchanger, and exchange heat to the substance entered in corresponding heat exchanger.
7. flue gas processing device according to claim 6, which is characterized in that the 6th heat exchanger respectively with the third
Heat exchanger and the connection of the 4th heat exchanger, send the pumping condensed water of the 6th heat exchanger into the third heat exchanger and exchange heat
Afterwards, back boiler water supply, after the secondary steam condensed water of the 6th heat exchanger is sent into the 4th heat exchanger heat exchange, as work
Skill supplements water；
The steam (vapor) outlet is also connected to the 4th heat exchanger, and secondary steam is sent into the 4th heat exchanger and is changed
Heat.
8. the flue gas processing device according to any one of claim 3-7, which is characterized in that the lower part of the absorption plant
Gas inlet is set, and exhanst gas outlet, first spray unit, the reservoir unit and second spray unit is arranged in top
It is respectively positioned between the gas inlet and exhanst gas outlet.
9. the flue gas processing device according to any one of claim 3-7, which is characterized in that the absorption plant lower part with
The first pump of setting between second heat exchanger or second heat exchanger and the second spray unit；
The absorption plant lower part and solution filtering tempering system or solution filtering tempering system are changed with described second
The second pump of setting between hot device or second heat exchanger and second spray unit.
10. flue gas processing device according to claim 9, which is characterized in that the absorption plant lower part and the described 5th
Heat exchanger or the 5th heat exchanger and it is arranged between the 6th heat exchanger or the 6th heat exchanger and the flash tank
Third pump；
The concentrated solution outlet and the 4th pump of setting between the 5th heat exchanger or the 5th heat exchanger and the first spray unit.
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| CN113899026A (en) * | 2021-09-24 | 2022-01-07 | 安徽聪旗智能科技有限公司 | High-cycle-energy-efficiency lithium chloride dehumidification system and lithium chloride solution circulation method |
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| CN109569199B (en) | 2024-02-20 |
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