CN109569199B - Flue gas treatment device - Google Patents
Flue gas treatment device Download PDFInfo
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- CN109569199B CN109569199B CN201811141341.5A CN201811141341A CN109569199B CN 109569199 B CN109569199 B CN 109569199B CN 201811141341 A CN201811141341 A CN 201811141341A CN 109569199 B CN109569199 B CN 109569199B
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- heat exchanger
- heat
- smoke
- flue gas
- absorption device
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 239000003546 flue gas Substances 0.000 title claims abstract description 114
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 107
- 238000010521 absorption reaction Methods 0.000 claims abstract description 99
- 239000000779 smoke Substances 0.000 claims abstract description 66
- 239000007788 liquid Substances 0.000 claims abstract description 57
- 238000000034 method Methods 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 12
- 238000005507 spraying Methods 0.000 claims description 60
- 230000008929 regeneration Effects 0.000 claims description 22
- 238000011069 regeneration method Methods 0.000 claims description 22
- 238000001914 filtration Methods 0.000 claims description 19
- 230000003750 conditioning effect Effects 0.000 claims description 17
- 239000007921 spray Substances 0.000 claims description 16
- 238000009833 condensation Methods 0.000 claims description 12
- 230000001502 supplementing effect Effects 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 4
- 230000000630 rising effect Effects 0.000 claims description 3
- 230000008859 change Effects 0.000 abstract description 5
- 239000000243 solution Substances 0.000 description 107
- 238000010438 heat treatment Methods 0.000 description 26
- 238000001816 cooling Methods 0.000 description 12
- 230000003009 desulfurizing effect Effects 0.000 description 12
- 230000005494 condensation Effects 0.000 description 10
- 238000006477 desulfuration reaction Methods 0.000 description 10
- 230000023556 desulfurization Effects 0.000 description 10
- 239000012266 salt solution Substances 0.000 description 10
- 230000000694 effects Effects 0.000 description 9
- 229920006395 saturated elastomer Polymers 0.000 description 9
- 239000000428 dust Substances 0.000 description 8
- 238000005265 energy consumption Methods 0.000 description 5
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 239000000498 cooling water Substances 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000004891 communication Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 238000005399 mechanical ventilation Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000002699 waste material Substances 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
- 239000006096 absorbing agent Substances 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
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction 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
- 239000012535 impurity Substances 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
- 239000002245 particle Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000005496 tempering Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a flue gas treatment device. The device is characterized in that a liquid storage unit is arranged in an absorption device, an inner cavity is divided into a first smoke treatment area and a second smoke treatment area by the liquid storage unit, smoke enters from the bottom of the absorption device to be in countercurrent contact with concentrated solution sprayed on the top of the absorption device, the concentrated solution in the second smoke treatment area absorbs water in the smoke to be diluted, latent heat released in the water phase change process is separated out, and the smoke and the concentrated solution are heated to 55-65 ℃; the heated concentrated solution is led out through the liquid storage unit and enters the first heat exchanger to exchange heat with a heat exchange medium (such as heat supply network water), the heat exchange medium can be heated to 3-10 ℃, the concentrated solution is cooled to be approximately consistent with the inlet temperature of the solution at the top of the second smoke treatment area and then enters the first smoke treatment area, moisture in smoke is continuously absorbed, step heat exchange is adopted for the first time, the heat exchange quality can be effectively improved, and sensible heat of raw smoke and latent heat of clean smoke steam are deeply recovered and utilized.
Description
Technical Field
The invention belongs to the technical field of environmental protection, and particularly relates to a flue gas treatment device.
Background
With the development of economy in China, the method is used for actively responding to the technical requirements (trial) of gypsum rain and colored smoke plume test of a coal-fired power plant in Shanghai city, the emission standard of atmospheric pollutants of a coal-fired power plant in Zhejiang (solicited manuscript), the notification of the work related to further strengthening the deep treatment of atmospheric pollution in important industries such as thermal power and steel in China in Tianjin city and the specification of colored smoke plume elimination in the areas such as Tangshan, zhangjia and the like in Hebei. Various technical routes for recovering the flue gas waste heat are developed, and common technical routes are that a flue gas condenser and a spray tower are arranged behind a desulfurizing tower or a slurry cooler is added on a slurry circulating slurry pipe to cool flue gas at an outlet of the desulfurizing tower to separate out water, and then the MGGH system is used for heating dehydrated clean flue gas by using the original flue gas waste heat.
The sensible heat of the raw flue gas and a large amount of latent heat of water vapor in the clean flue gas cannot be deeply utilized by the flue gas condensation or flue gas condensation regeneration technical route. Meanwhile, in order to cool and dehydrate the flue gas, the technology needs to take away the condensation latent heat of the flue gas by using an external refrigerant, and then heats the clean flue gas by using the sensible heat of the original flue gas to improve the unsaturation degree and climbing capacity, so that the mode causes great waste of energy. Meanwhile, the flue gas is condensed to release latent heat, a large amount of cooling circulating water is needed for taking away the latent heat, the cold source is a problem which needs to be faced by each technical route at present, particularly, for the region which prescribes the temperature and moisture content of flue gas at the outlet of a desulfurizing tower, the flue gas is required to be condensed in winter, even in summer, the cooling tower of a power plant is often operated at full load in summer, an effective cold source cannot be provided, if the cooling tower is newly built, tens of millions of investment is needed, and meanwhile, the water of the cooling tower is evaporated to be replaced by waste water in the flue gas, so that the water-saving effect cannot be achieved. If a mechanical ventilation cooling tower is newly built, the construction cost is extremely high, and the mechanical ventilation cooling tower cannot bear a power plant.
Disclosure of Invention
Therefore, the technical problem to be solved by the invention is that the existing technical route for recovering the waste heat of the flue gas has the defects that the sensible heat of the original flue gas and a great amount of latent heat of water vapor in the clean flue gas cannot be deeply utilized, meanwhile, the energy and water resources are wasted, the investment cost is high, and the colored smoke plume is only invested and has no benefit, so that the flue gas treatment device is provided.
For this reason, the technical proposal adopted by the application is that,
a flue gas treatment device, which comprises an absorption device and also comprises,
the liquid storage unit is arranged in the absorption device and divides the inner cavity of the liquid storage unit into a first smoke treatment area and a second smoke treatment area, and smoke is suitable for entering the second smoke treatment area from the first smoke treatment area through the liquid storage unit;
and the liquid inlet end of the first heat exchanger is communicated with the liquid storage unit, the liquid outlet end of the first heat exchanger is communicated with the first smoke treatment area close to the liquid storage unit, so that the solution in the liquid storage unit enters the first heat exchanger for heat exchange, and the heat exchanged solution is sent into the first smoke treatment area to contact smoke.
Further, a regeneration system is also included, the regeneration system including,
the flash tank is provided with a dilute solution inlet and a steam outlet at the upper part and a concentrated solution outlet at the lower part;
the lower part of the absorption device, the sixth heat exchanger and the dilute solution inlet are sequentially communicated;
the steam outlet, the compressor, the saturator and the sixth heat exchanger are sequentially communicated, so that the dilute solution and the secondary steam enter the flash tank after heat exchange occurs in the sixth heat exchanger.
Further, the device also comprises a first spraying unit, wherein the first spraying unit is arranged in the absorption device near the middle upper part of the absorption device and is positioned above the liquid storage unit, and the concentrated solution outlet, the fifth heat exchanger and the first spraying unit are sequentially communicated, so that the concentrated solution after heat exchange is sprayed on the rising flue gas through the first spraying unit;
the second spraying unit is close to the liquid storage unit and arranged below the liquid storage unit in the absorption device, and the liquid storage unit, the first heat exchanger and the second spraying unit are sequentially communicated and arranged so as to exchange heat with the solution contacted with the flue gas and then spray the solution on the clean flue gas so as to reversely convect with the clean flue gas.
Further, the lower part of the absorption device, the fifth heat exchanger, the sixth heat exchanger and the dilute solution inlet are sequentially communicated, so that heat exchange is performed between the fifth heat exchanger and the concentrated solution from the concentrated solution outlet of the flash tank, and the concentrated solution is finally sent to the flash tank after heat exchange by the sixth heat exchanger.
Further, the device also comprises a second heat exchanger, wherein the lower part of the absorption device, the second heat exchanger and the second spraying unit are sequentially communicated, so that the dilute solution is sent to the second spraying unit after heat exchange;
the lower part of the absorption device, the solution filtering and conditioning system, the second heat exchanger and the second spraying unit are sequentially communicated, so that dilute solution is fed into the second spraying unit after filtering and conditioning and heat exchange.
Further, the heat exchange device further comprises a third heat exchanger and a fourth heat exchanger, wherein the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger are sequentially communicated, so that heat supply network incoming water or low condensation water sequentially passes through the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger and exchanges heat with substances entering the corresponding heat exchangers.
Further, the sixth heat exchanger is respectively communicated with the third heat exchanger and the fourth heat exchanger, so that the air-extracted condensed water of the sixth heat exchanger is fed into the third heat exchanger for heat exchange, then fed into the boiler for water supply, and the secondary steam condensed water of the sixth heat exchanger is fed into the fourth heat exchanger for heat exchange and then used as process supplementing water;
the steam outlet is also communicated with the fourth heat exchanger so as to send the secondary steam into the fourth heat exchanger for heat exchange.
Further, the lower part of the absorption device is provided with a smoke inlet, the upper part of the absorption device is provided with a smoke outlet, and the first spraying unit, the liquid storage unit and the second spraying unit are all positioned between the smoke inlet and the smoke outlet.
Further, a first pump is arranged between the lower part of the absorption device and the second heat exchanger or between the second heat exchanger and the second spraying unit;
a second pump is arranged between the lower part of the absorption device and the solution filtering and conditioning system, or between the solution filtering and conditioning system and the second heat exchanger, or between the second heat exchanger and the second spraying unit;
a third pump is arranged between the lower part of the absorption device and the fifth heat exchanger, or between the fifth heat exchanger and the sixth heat exchanger, or between the sixth heat exchanger and the flash tank;
and a fourth pump is arranged between the concentrated solution outlet and the fifth heat exchanger or between the fifth heat exchanger and the first spraying unit.
The technical scheme of the invention has the following advantages:
1. according to the flue gas treatment device provided by the invention, the liquid storage unit is arranged in the absorption device, the inner cavity is divided into the first flue gas treatment area and the second flue gas treatment area by utilizing the liquid storage unit, flue gas enters into countercurrent contact with concentrated solution (such as concentrated salt solution) sprayed on the top of the absorption device from the bottom of the absorption device, the concentrated solution in the second flue gas treatment area absorbs water in the flue gas to be diluted, latent heat released in the water phase change process is separated out, and the flue gas and the concentrated solution are heated to 55-65 ℃; the heated concentrated solution is led out through the liquid storage unit and enters the first heat exchanger to exchange heat with a heat exchange medium (such as heat supply network water), the heat exchange medium can be heated to 3-10 ℃, the concentrated solution is cooled to be approximately consistent with the temperature of the solution inlet at the top of the second smoke treatment area and then enters the first smoke treatment area, moisture in smoke is continuously absorbed, step heat exchange is adopted for the first time, the heat exchange quality can be effectively improved, the sensible heat of raw smoke and the latent heat of water vapor of clean smoke are finally deeply recovered and utilized through the means, a large amount of cold sources are needed for cooling and condensing smoke in the prior art, and water resources are greatly saved. Meanwhile, the water in the clean flue gas is recovered, the running cost of the system is reduced, the problem that a coal-fired power plant or other industries eliminate colored smoke plumes and a deep water lifting system is only put into a system without income is solved, the environment-friendly effects of high efficiency, energy conservation, emission reduction and the like are achieved, and the system has good social and economic effects.
2. According to the flue gas treatment device provided by the invention, firstly, the water content of the clean flue gas is greatly reduced by utilizing the absorption device, and the dryness and the temperature of the clean flue gas are improved due to the latent heat released by phase change in the process of absorbing steam by the concentrated solution, so that the effects of eliminating colored smoke plumes, deeply extracting water, reducing the dust content of the clean flue gas and recovering the low-quality latent heat of water vapor in the clean flue gas can be simultaneously achieved; then the concentrated solution after absorbing the water vapor in the absorption device is changed into a dilute solution, a part of the dilute solution is cooled by a fifth heat exchanger, then the original concentration is recovered by a regeneration system, and finally the dilute solution is returned to the second flue gas treatment area; the other part of the flue gas is heated by a second heat exchanger to heat a heat exchange medium (such as heat supply network water) and then returned to the first flue gas treatment area, the two flow rates are adjusted according to specific requirements, and the water absorption capacity of the unit mass concentrated solution can be changed by adjusting the ratio of the two flow rates; in addition, the dilute solution sent to the regeneration system is subjected to heat exchange with saturated steam generated by the regeneration system and enters a flash tank for flash evaporation and regeneration to become concentrated solution, and then the concentrated solution is sent to an absorption device, the regeneration process utilizes saturated steam generated after secondary steam compression at the top of the regeneration system, the saturated steam releasing latent heat is changed into secondary steam condensate water, the secondary steam condensate water enters a fourth heat exchanger again to exchange heat with heat supply network water, and the cooled condensate water can be used as demister flushing water of a desulfurization device or used as process supplementing water and the like, so that the cost and the energy consumption are reduced. The regeneration of power plant steam is avoided, and the steam consumption can be effectively reduced.
3. According to the flue gas treatment device provided by the invention, the steam is pumped by adopting the steam turbine in the heating season of the regeneration system, and the pumped condensate water is returned to the boiler for water supply after heat exchange of the third heat exchanger; the non-heating season adopts secondary steam of a compressor, a saturator and a flash tower, saturated steam generated after compression is used for water supplementing of the desulfurization device process. After the heat exchange and temperature rise of the heat supply network water or the low condensation water pass through the first heat exchanger and the second heat exchanger of the absorption device, the heat exchange is carried out between the heat supply network water or the low condensation water and the third heat exchanger and the fourth heat exchanger of the regeneration system, the heating season reaches the requirement of the temperature of the heat supply network water, and the heat supply is carried out on the heat supply network in the heating season; the low-adding-removing or low-temperature-saving economizer heat exchanging is performed in the non-heating season, and the low-adding-removing method can be used for heating low-adding condensed water, so that the power generation capacity of the non-heating season unit is not affected. The problems that a coal-fired power plant or other industries remove wet smoke plume and a deep water lifting system is only put into practice and has no benefit are solved in the above mode, the latent heat of the water vapor of the clean flue gas after the desulfurization device is further recovered through the compressor, the saturator and the flash tower system, the moisture in the clean flue gas is recovered, the running cost of the system is reduced, and the environment-friendly effects of high efficiency, energy conservation, emission reduction and the like are achieved.
4. The flue gas treatment device provided by the invention not only can use the sensible heat of the original flue gas for heating the heat supply network water or adding the condensation water at a low temperature, but also can recover a great amount of latent heat of the water vapor in the flue gas, and deeply recover the flue gas waste heat. The device recovers water-saving resources by deep water lifting, and compared with the prior related technology, the device can reduce the pressure drop of the system by about one third due to simple system equipment, saves the operation cost and has good environmental protection and energy saving effects.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present invention, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
FIG. 1 is a layout of a flue gas treatment device in an embodiment of the invention;
FIG. 2 is a layout of a flue gas treatment system in an embodiment of the invention;
FIG. 3 is a system diagram of a flue gas treatment system in an embodiment of the present invention;
FIG. 4 is a schematic view of the structure of an absorber device in an embodiment of the present invention;
FIG. 5 is a schematic diagram of a regeneration system according to an embodiment of the present invention;
wherein the reference numerals are expressed as:
1-a dust removal device; 2-a desulfurizing device; 3-an absorption device; 3-1-a first spray unit; 3-2-a second spray unit; 3-3-reservoir unit; 3-4-smoke inlet; 3-5-fume outlet; 3-6-demister; 4-an economizer; 5-a first pump; 6-a second pump; 7-a solution filtering tempering system; 8-a first heat exchanger; 9-a second heat exchanger; 10-a third heat exchanger; 11-fourth heat exchanger; 12-a third pump; 13-a fifth heat exchanger; 14-fourth pump; 15-a compressor; a 16-saturator; 17-sixth heat exchanger; 18-a flash tank; 19-chimney; 20-seventh heat exchanger; 21-a solution replenishment tank; 22-fifth pump.
Detailed Description
The following description of the present invention will be made clearly and fully, and it is apparent that the embodiments described are some, but not all, of the embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In the description of the present invention, it should be noted that the directions or positional relationships indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
In addition, the technical features of the different embodiments of the present invention described below may be combined with each other as long as they do not collide with each other.
Example 1
The embodiment provides a flue gas treatment device, as shown in fig. 1, which comprises an absorption device 3, wherein the absorption device 3 can be an absorption tower, a flue gas inlet 3-4 is arranged at the lower part of the absorption device 3, a flue gas outlet 3-5 is arranged at the upper part of the absorption device, and the flue gas treatment device further comprises a liquid storage unit 3-3, for example, the liquid storage unit 3-3 can be a liquid receiving disc, as shown in fig. 4, the liquid receiving disc is provided with a disc which is matched with the inner cavity of the desulfurization tower, a through hole is formed in the disc, the through hole is provided with an extension section which extends towards the top of the desulfurization tower along the axial direction of the desulfurization tower, a liquid storage space is arranged between adjacent extension sections, the extension section is arranged in the absorption device 3, the inner cavity of the absorption device is divided into a first flue gas treatment area and a second flue gas treatment area, and flue gas is suitable for passing through the liquid storage unit 3-3 from the first flue gas treatment area to the second flue gas treatment area; specifically, the liquid storage unit 3-3 may be disposed in the middle of the desulfurizing tower;
the liquid inlet end of the first heat exchanger 8 is communicated with the liquid storage unit 3-3, and the liquid outlet end is communicated with the first smoke treatment area close to the liquid storage unit 3-3, so that the solution of the liquid storage unit 3-3 enters the first heat exchanger 8 for heat exchange, and the heat exchanged solution is sent into the first smoke treatment area to contact with smoke.
In addition, the application provides a flue gas treatment system comprising the flue gas treatment device, as shown in fig. 2 and 3, the flue gas treatment system comprises a dust removing device 1, a desulfurizing device 2 and an absorbing device 3 which are sequentially communicated, wherein the dust removing device 1 can be an electric dust collector, and the desulfurizing device 2 can be a desulfurizing tower.
In the flue gas treatment device, a liquid storage unit 3-3 is arranged in an absorption device 3, an inner cavity is divided into a first flue gas treatment area and a second flue gas treatment area by using the liquid storage unit, flue gas enters from the bottom of the absorption device 3 and is in countercurrent contact with concentrated solution (such as concentrated salt solution) sprayed on the top of the absorption device 3, the concentrated solution in the second flue gas treatment area absorbs water in the flue gas to be diluted, latent heat released in the water phase change process is separated out, and the flue gas and the concentrated solution are heated to 55-65 ℃; the heated concentrated solution is led out into the first heat exchanger through the liquid storage unit 3-3 to exchange heat with a heat exchange medium (such as heat supply network water), the heat exchange medium can be heated to 3-10 ℃, the concentrated solution is cooled to be approximately consistent with the inlet temperature of the solution at the top of the second smoke treatment area and then enters the first smoke treatment area, moisture in smoke is continuously absorbed, step heat exchange is adopted for the first time, the heat exchange quality can be effectively improved, finally, sensible heat of original smoke and latent heat of water vapor of clean smoke are deeply recycled and utilized through the means, a large amount of cold sources are needed for cooling and condensing smoke in the prior art, and water resources are greatly saved. Meanwhile, the water in the clean flue gas is recovered, the running cost of the system is reduced, the problem that a coal-fired power plant or other industries eliminate colored smoke plumes and a deep water lifting system is only put into a system without income is solved, the environment-friendly effects of high efficiency, energy conservation, emission reduction and the like are achieved, and the system has good social and economic effects.
Further, as shown in fig. 5, the regeneration system further comprises a flash tank 18, wherein the upper part of the regeneration system is provided with a dilute solution inlet and a steam outlet, and the lower part of the regeneration system is provided with a concentrated solution outlet; the lower part of the absorption device 3, the sixth heat exchanger 17 and the dilute solution inlet are sequentially communicated; the compressor 15 and the saturator 16, the steam outlet, the compressor 15, the saturator 16 and the sixth heat exchanger 17 are sequentially connected, so that the dilute solution and the secondary steam exchange heat in the sixth heat exchanger 17 and then enter the flash tank 18.
In addition, the driving heat source of the regeneration system heats the season and pumps air for the unit; the saturated steam generated by the secondary steam of the compressor, the saturator and the flash tower is adopted in the non-heating season, and the compressor, the saturator and the flash tower system can prevent the power generation capacity of the non-heating season unit from being affected. And heating the heat supply network water or the circulating heat medium water or the low-condensation water to different temperatures through the heat supply network heat exchanger in different seasons.
In this embodiment, the device further includes a first spraying unit 3-1, which is disposed in the absorption device 3 near the middle upper portion thereof and above the liquid storage unit 3-3, and the concentrated solution outlet, the fifth heat exchanger 13 and the first spraying unit 3-1 are sequentially connected to each other, so as to spray the concentrated solution after heat exchange onto the rising flue gas through the first spraying unit 3-1; the second spraying unit 3-2 is arranged in the absorption device 3 near the liquid storage unit 3-3 and below the liquid storage unit 3-3, and the liquid storage unit 3-3, the first heat exchanger 8 and the second spraying unit 3-2 are sequentially communicated and arranged so as to exchange heat with the solution contacted with the flue gas and then spray the solution on the clean flue gas so as to reversely convect with the clean flue gas; specifically, the first spraying unit 3-1 and the second spraying unit 3-2 comprise spraying pipes and spraying nozzles arranged on the spraying pipes at intervals, and the first spraying unit 3-1 and the second spraying unit 3-2 are close to the flue gas outlet 3-5 of the absorption device 3 and are positioned below the flue gas outlet 3-5, so that the countercurrent contact path is prolonged, and heat in flue gas can be effectively recovered.
Specifically, the lower part of the absorption device 3, the fifth heat exchanger 13, the sixth heat exchanger 17 and the dilute solution inlet are sequentially communicated, so that the bottom solution of the absorption tower exchanges heat with the concentrated solution from the concentrated solution outlet of the flash tank in the fifth heat exchanger 13, exchanges heat through the sixth heat exchanger 17, and is finally sent to the flash tank 18; the fifth heat exchanger 13 may be a plate heat exchanger;
in addition, a seventh heat exchanger 20 is also arranged, and the concentrated solution coming out of the fifth heat exchanger 13 can enter the seventh heat exchanger 20 to exchange heat with heat supply network water or low-adding condensed water and then enter the absorption device.
Example 2
The embodiment provides a flue gas treatment device, in order to improve the heat exchange effect on the basis of the embodiment 1, fully recover sensible heat in raw flue gas and latent heat of purified flue gas steam and fully regenerate waste liquid, and further comprises a second heat exchanger 9, wherein the lower part of the absorption device 3, the second heat exchanger 9 and the second spraying unit 3-2 are sequentially communicated, so that dilute solution is sent into the second spraying unit 3-2 after heat exchange; meanwhile, in order to filter and modulate the concentrated solution used as the absorption liquid in the absorption device, the device also comprises a solution filtering and conditioning system 7, wherein the lower part of the absorption device 3, the solution filtering and conditioning system 7, a second heat exchanger 9 and a second spraying unit 3-2 are sequentially communicated, so that the dilute solution is sent to the second spraying unit 3-2 after filtering and conditioning and heat exchanging; specifically, as shown in fig. 3, the solution filtration conditioning system 7 is composed of a cyclone + filter which are sequentially communicated, while a solution replenishing tank 21 and a fifth pump 22 which are sequentially communicated are provided, and the fifth pump 22 is communicated with the solution filtration conditioning system 7 to replenish the solution therein.
Example 3
The present embodiment provides a flue gas treatment device, which further includes a third heat exchanger 10 and a fourth heat exchanger 11 on the basis of the above embodiment 1 or 2, where the first heat exchanger 8, the second heat exchanger 9, the third heat exchanger 10 and the fourth heat exchanger 11 are sequentially connected, so that the heat supply network incoming water or the low condensation water sequentially passes through the first heat exchanger 8, the second heat exchanger 9, the third heat exchanger 10 and the fourth heat exchanger 11, and exchanges heat with substances entering the corresponding heat exchangers;
further, the sixth heat exchanger 17 is respectively communicated with the third heat exchanger 10 and the fourth heat exchanger 11, so that the extracted condensate water of the sixth heat exchanger 17 is fed into the third heat exchanger 10 for heat exchange, then fed into the boiler, and the secondary steam condensate water of the sixth heat exchanger 17 is fed into the fourth heat exchanger 10 for heat exchange and then used as process supplementing water; the steam outlet is also communicated with the fourth heat exchanger 11 so as to send the secondary steam into the fourth heat exchanger 11 for heat exchange;
in order to realize the flow of the liquid, a first pump 5 is arranged between the lower part of the absorption device 3 and the second heat exchanger 9 or between the second heat exchanger 9 and the second spraying unit 3-2; a second pump 6 is arranged between the lower part of the absorption device 3 and the solution filtering and conditioning system 7, or between the solution filtering and conditioning system 7 and the second heat exchanger 9, or between the second heat exchanger 9 and the second spraying unit 3-2; a third pump 12 is arranged between the lower part of the absorption device 3 and the fifth heat exchanger 13, or between the fifth heat exchanger 13 and the sixth heat exchanger 17, or between the sixth heat exchanger 17 and the flash tank 17; a fourth pump 14 is arranged between the concentrated solution outlet and the fifth heat exchanger 13, or between the fifth heat exchanger 13 and the first spray unit 3-1.
In addition, the secondary steam at the top of the flash tank enters a fourth heat exchanger to lift the heat supply network water to about 85 ℃ for heating; the compressor, the saturator and the flash tower are utilized to heat secondary vapor compression and saturated vapor into the dilute solution of the plate heat exchanger in non-heating seasons, condensed water can heat supply network water (low-added condensed water) to about 60 ℃ for heating the low-added condensed water, and the operation mode can offset the pumping energy consumption and the recovery energy consumption in the non-heating seasons, so that the generating capacity of a unit is not negatively influenced. The concentrated solution at the bottom of the flash tank exchanges heat with the dilute solution in a fifth heat exchanger 13 (dilute concentrated solution heat exchanger), and then returns to the top of the absorption tower after exchanging heat with a seventh heat exchanger (concentrated solution heat exchanger). The secondary steam in the non-heating season is discharged from the top of the regenerator and enters the compressor, is changed into superheated steam through pressurization and temperature increase, is changed into saturated steam through spraying, is used as a driving heat source of the regenerator, is changed into condensation water after latent heat is released, and the condensation water exchanges heat with the third heat exchanger again.
Example 4
The present embodiment provides a flue gas treatment device, on the basis of the above embodiments 1, 2 or 3, as shown in fig. 2, the flue gas treatment system including the flue gas treatment device in this embodiment further includes an economizer 3-6 disposed between the dust removing device 1 and the desulfurizing device 2 or between the air preheater and the dust removing device 1, and a fourth heat exchanger 11 is in communication with the economizer 3-6 to exchange heat between condensed water and flue gas from the dust removing device 1 in the economizer 3-6 and send the flue gas after heat exchange into the desulfurizing device 2.
Further, a smoke inlet 3-4 is arranged at the lower part of the absorption device 3, a smoke outlet 3-5 is arranged at the upper part of the absorption device, the smoke outlet 3-5 is communicated with a chimney 19, and the first spraying unit 3-1, the liquid storage unit 3-3 and the second spraying unit 3-2 are all positioned between the smoke inlet 3-4 and the smoke outlet 3-5; the demister 3-6 is arranged in the absorption device 3 and is positioned between the first spraying unit 3-1 and the flue gas outlet 3-5.
If the smoke temperature needs to be raised to a higher temperature, a reheat heat exchanger can be arranged on a rear flue of the smoke outlet 3-4 of the absorption device 3 or a heat pipe can be replaced in the top of the upper section of the absorption device 3 to heat the smoke temperature to the temperature required by environmental protection or owners.
Example 5
The embodiment provides a flue gas treatment device, on the basis of the embodiments 1, 2, 3 and 4, in order to adapt to non-heating seasons, the absorption device can be used as a traditional spray tower, the circulating cooling water is utilized to spray the flue gas in the absorption device, so that a system can flexibly regulate and control a flue gas treatment system, energy sources are saved, the flue gas treatment system comprising the flue gas treatment device in the embodiment is directly communicated with a flue gas outlet of a desulfurization device 2, spraying can be switched between salt solution or circulating cooling water according to requirements in the working process, when the spraying is switched to the circulating cooling water, the system becomes a spray system, saturated flue gas and spraying water transfer heat and mass, the flue gas temperature is reduced to 48 ℃ in summer and reduced to 45 ℃ in winter, the spraying water at the bottom of the spray tower exchanges heat with low-adding condensed water, the unit is reduced, and the spraying water after heat exchange returns to the spray tower; or the spray water at the bottom of the spray tower is sent to a cooling tower for cooling, and the spray water is recycled after being cooled.
In addition, the specific working principle of the device is as follows:
as shown in fig. 1 and 2, the flue gas enters from the bottom of the absorption tower and flows in countercurrent with the concentrated salt solution sprayed from the top of the absorption tower, the water in the flue gas is absorbed by the concentrated salt solution at the top of the upper section of the absorption tower to be diluted, latent heat is released in the water phase change process, and the flue gas and the salt solution are heated to 55-65 ℃. The heated solution is led out through a liquid receiving disc at the bottom of the upper section and enters a first heat exchanger (a first heat exchanger of a heat supply network) to exchange heat with heat supply network water, the heat supply network water can be heated to 3-10 ℃, salt solution is cooled to be consistent with the inlet temperature of the solution at the top of the upper section and then enters the top of the lower section of the absorption tower, moisture in the flue gas is continuously absorbed, the dilute solution at the bottom of the lower section of the absorption tower is respectively sent to a second heat exchanger (a second heat exchanger of the heat supply network) and a fifth heat exchanger (a dilute concentrated solution heat exchanger) by a first pump (a dilute salt solution pump), the heat supply network water exiting the first heat exchanger (the first heat exchanger of the heat supply network) exchanges heat with the dilute solution entering the second heat exchanger (the second heat exchanger of the heat supply network), the dilute solution at the bottom of the lower section is cooled to be consistent with the outlet temperature of the first heat exchanger (the first heat exchanger of the heat supply network), and is mixed with the outlet solution at the top of the bottom of the lower section of the absorption tower to be sprayed, and the heat supply network water is heated to 50-60 ℃; the dilute solution entering the fifth heat exchanger (dilute concentrated solution heat exchanger) exchanges heat with the concentrated solution from the regeneration system and then enters the regeneration system. The diluted solution heated by the concentrated solution enters a sixth heat exchanger (plate heat exchanger) to continuously heat to 120-140 ℃ (the heat source is the steam of a pumping unit used in heating season, and the secondary steam of a compressor, a saturator and a flash tower is used in non-heating season), and then flash evaporation is carried out in a flash tank. In heating season, the air-extracting condensed water enters a third heat exchanger 10 (a heat supply network three-stage heat exchanger) to exchange heat with heat supply network water, and the secondary steam at the top of the flash tank enters a fourth heat exchanger 11 (a heat supply network four-stage heat exchanger) to raise the heat supply network water to about 85 ℃ for heating; in the non-heating season, the secondary steam compression and saturation steam is heated by a compressor, a saturator and a flash tower to enter a dilute solution of a sixth heat exchanger (a plate heat exchanger), the temperature of the secondary steam at the top of the flash evaporator is about 95-110 ℃, the secondary steam is determined by the concentration and the water absorption of the salt solution, the secondary steam enters the compressor from the top of the flash tank to be compressed to about 300 ℃, the superheated steam is saturated by spraying and becomes saturated steam with the temperature of about 130-150 ℃, and the condensed water can heat supply network water (low-pressure condensed water) to about 57-70 ℃ for heating the low-pressure condensed water or is connected with a low-temperature economizer in series to continuously raise the temperature to 65-85 ℃. The condensed water after cooling can be used for demister flushing water of the desulfurizing tower, etc. Through the operation mode, the COP of the absorption starting heat pump system can be improved to 3-4, the pumping energy consumption and the recovery energy consumption in the non-heating season can be mutually offset, and the generating capacity of the unit is not negatively influenced. The concentrated solution at the bottom of the flash tank exchanges heat with the dilute solution in a fifth heat exchanger (dilute concentrated solution heat exchanger), and is cooled to 30-50 ℃ by a concentrated solution cooling heat exchanger and returned to the top of the upper section of the absorption tower for recycling.
Specifically, the bottom solution at the lower section of the desulfurizing tower is divided into three parts: the first part exchanges heat with a heat supply network secondary heat exchanger and returns to the top of the lower section of the absorption tower to form small circulation; the second part is sent to a dilute and concentrated solution heat exchanger for heating and then enters a regeneration system; the third part enters a solution filtering and conditioning unit, and the bottom of the lower section of the absorption tower is matched with the filtering and conditioning unit, so that on one hand, solid particles accumulated in the absorption tower and substances such as generated crystal salts (sulfate, carbonate and the like) and the like of the solution can be removed through a cyclone and a filtering device, and the pollutants and impurities of the solution in the absorption tower are controlled to a certain degree; on the other hand, calcium-based salt is added, the pH value of the solution is adjusted, the absorption capacity of the solution is maintained, and meanwhile, the corrosiveness of the solution is reduced. The absorption liquid enters from the top of the absorption tower, and flows reversely with the purified flue gas entering from the bottom of the absorption tower through uniform spraying, the water vapor in the purified flue gas is absorbed by the concentrated solution, and the spraying layers of the upper section and the lower section can be provided with standby layers so as to improve the reliability of the absorption tower. The water absorption capacity of the salt solution in unit mass can be controlled by adjusting the small circulating solution amount at the lower section of the absorption tower, the absorption tower is arranged behind the desulfurization tower, most of water absorption occurs at the part due to high water content of flue gas at the bottom of the absorption tower, small circulation is arranged at the bottom of the absorption tower, the equilibrium temperature at the lower section of the absorption tower is controlled by reducing the temperature of the small circulation solution, so that the water absorption capacity of the solution in unit mass is improved, the concentration of the absorbed dilute solution is reduced by 1% -10% compared with that of the concentrated solution, and the ratio of the small circulation amount to the regeneration circulation amount can be 1:1-10:1. The desulfurization tower in the original system does not need to be modified, and the invention is applicable to desulfurization tower systems including single-tower double-circulation systems and double-tower double-circulation systems.
It is apparent that the above examples are given by way of illustration only and are not limiting of the embodiments. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary here nor is it exhaustive of all embodiments. While still being apparent from variations or modifications that may be made by those skilled in the art are within the scope of the invention.
Claims (3)
1. A flue gas treatment device comprises an absorption device and is characterized by also comprising,
the liquid storage unit is arranged in the absorption device and divides the inner cavity of the liquid storage unit into a first smoke treatment area and a second smoke treatment area, and smoke is suitable for entering the second smoke treatment area from the first smoke treatment area through the liquid storage unit;
the liquid inlet end of the first heat exchanger is communicated with the liquid storage unit, the liquid outlet end of the first heat exchanger is communicated with the first smoke treatment area close to the liquid storage unit, so that the solution in the liquid storage unit enters the first heat exchanger for heat exchange, and the heat exchanged solution is sent into the first smoke treatment area to contact smoke; the absorption device is internally provided with a first spraying unit and a second spraying unit, the lower part of the absorption device is provided with a smoke inlet, the upper part of the absorption device is provided with a smoke outlet, and the first spraying unit, the liquid storage unit and the second spraying unit are all positioned between the smoke inlet and the smoke outlet;
the lower part of the absorption device, the second heat exchanger and the second spraying unit are sequentially communicated, so that the dilute solution is sent to the second spraying unit after heat exchange;
the lower part of the absorption device, the solution filtering and conditioning system, the second heat exchanger and the second spraying unit are sequentially communicated, so that dilute solution is fed into the second spraying unit after filtering and conditioning and heat exchange;
the regeneration system comprises a flash tank, a sixth heat exchanger, a compressor and a saturator, wherein the upper part of the flash tank is provided with a dilute solution inlet and a steam outlet, and the lower part of the flash tank is provided with a concentrated solution outlet; the lower part of the absorption device, the sixth heat exchanger and the dilute solution inlet are sequentially communicated; the steam outlet, the compressor, the saturator and the sixth heat exchanger are sequentially communicated, so that the dilute solution and the secondary steam enter the flash tank after heat exchange occurs in the sixth heat exchanger;
the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger are sequentially communicated, so that the heat supply network incoming water or low-condensation water sequentially passes through the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger and exchanges heat with substances entering the corresponding heat exchangers;
the first spraying unit is arranged in the absorption device close to the middle upper part of the absorption device and is positioned above the liquid storage unit, and the concentrated solution outlet, the fifth heat exchanger and the first spraying unit are sequentially communicated, so that the concentrated solution after heat exchange is sprayed on the rising flue gas through the first spraying unit;
the second spraying unit is close to the liquid storage unit and is arranged below the liquid storage unit in the absorption device, and the liquid storage unit, the first heat exchanger and the second spraying unit are sequentially communicated, so that after heat exchange is carried out on a solution contacted with the flue gas, the solution is sprayed on the clean flue gas so as to reversely convect with the clean flue gas;
the lower part of the absorption device, a fifth heat exchanger, a sixth heat exchanger and a dilute solution inlet are sequentially communicated, so that heat exchange is performed between the fifth heat exchanger and the concentrated solution from the concentrated solution outlet of the flash tank, and the concentrated solution is finally sent to the flash tank after heat exchange by the sixth heat exchanger;
the sixth heat exchanger is respectively communicated with the third heat exchanger and the fourth heat exchanger, so that the extracted condensate water of the sixth heat exchanger is fed into the third heat exchanger for heat exchange, then fed into the boiler for water supply, and the secondary steam condensate water of the sixth heat exchanger is fed into the fourth heat exchanger for heat exchange and then used as process supplementing water;
the steam outlet is also communicated with the fourth heat exchanger so as to send the secondary steam into the fourth heat exchanger for heat exchange.
2. The flue gas treatment device according to claim 1, wherein a first pump is provided between the lower part of the absorption device and the second heat exchanger, or between the second heat exchanger and the second spray unit;
and a second pump is arranged between the lower part of the absorption device and the solution filtering and conditioning system, or between the solution filtering and conditioning system and the second heat exchanger, or between the second heat exchanger and the second spraying unit.
3. The flue gas treatment device according to claim 2, wherein a third pump is provided between the lower part of the absorption device and the fifth heat exchanger, or the fifth heat exchanger and the sixth heat exchanger, or the sixth heat exchanger and the flash tank;
and a fourth pump is arranged between the concentrated solution outlet and the fifth heat exchanger or between the fifth heat exchanger and the first spraying 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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