CN109395540B - Raw flue gas sensible heat deep utilization regeneration system - Google Patents
Raw flue gas sensible heat deep utilization regeneration system Download PDFInfo
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- CN109395540B CN109395540B CN201811513571.XA CN201811513571A CN109395540B CN 109395540 B CN109395540 B CN 109395540B CN 201811513571 A CN201811513571 A CN 201811513571A CN 109395540 B CN109395540 B CN 109395540B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 136
- 239000003546 flue gas Substances 0.000 title claims abstract description 136
- 230000008929 regeneration Effects 0.000 title claims abstract description 37
- 238000011069 regeneration method Methods 0.000 title claims abstract description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 137
- 238000010521 absorption reaction Methods 0.000 claims abstract description 96
- 239000007788 liquid Substances 0.000 claims abstract description 67
- 239000000779 smoke Substances 0.000 claims abstract description 52
- 238000000034 method Methods 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims abstract description 13
- 238000005507 spraying Methods 0.000 claims description 61
- 230000003009 desulfurizing effect Effects 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 15
- 239000000428 dust Substances 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 11
- 230000001502 supplementing effect Effects 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 7
- 239000003245 coal Substances 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims 4
- 230000001174 ascending effect Effects 0.000 claims 1
- 230000008859 change Effects 0.000 abstract description 6
- 239000000243 solution Substances 0.000 description 115
- 238000010438 heat treatment Methods 0.000 description 17
- 238000012856 packing Methods 0.000 description 14
- 230000000694 effects Effects 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 239000012266 salt solution Substances 0.000 description 8
- 230000005494 condensation Effects 0.000 description 7
- 239000006096 absorbing agent Substances 0.000 description 6
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000023556 desulfurization Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000004134 energy conservation Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram 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
- 238000005086 pumping Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000012546 transfer Methods 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
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010248 power generation Methods 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
- 239000008400 supply water Substances 0.000 description 1
- 238000005496 tempering 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
- B01D53/1456—Removing acid components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/10—Combinations of devices covered by groups B01D45/00, B01D46/00 and B01D47/00
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
- F22D1/32—Feed-water heaters, i.e. economisers or like preheaters arranged to be heated by steam, e.g. bled from turbines
- F22D1/34—Feed-water heaters, i.e. economisers or like preheaters arranged to be heated by steam, e.g. bled from turbines and returning condensate to boiler with main feed supply
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
Abstract
The application discloses a regeneration system for deep utilization of sensible heat of raw flue gas. The regeneration system 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 and is 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 application belongs to the technical field of environmental protection, and particularly relates to a raw flue gas sensible heat deep utilization regeneration system.
Background
At present, the mainstream dehumidification smoke plume technology is that a flue gas condenser, a spray tower or a slurry cooler is added on a slurry circulating slurry pipe behind a desulfurizing tower to cool and separate out water from flue gas at an outlet of the desulfurizing tower, and the flue gas is heated by using waste heat of raw flue gas, so that the technology cannot deeply recover a large amount of latent heat of water vapor of the flue gas, and waste sensible heat of the raw flue gas.
And meanwhile, the flue gas is condensed and water is separated out, so that an external refrigerant is needed, and the great energy waste is caused. In order to take away the latent heat of clean flue gas and need a large amount of cooling circulating water, the cold source is the problem that must face of current mainstream technology, especially to the region that prescribes the export flue gas temperature and moisture content of desulfurizing tower, not only need condensation in winter, even also need flue gas condensation in summer, and the cooling tower of power plant often is full load operation in summer, can't provide effective cold source, if newly built cooling tower needs to increase the investment, can cause simultaneously to change waste water with good water, can not play the water conservation effect. 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 application is that the existing technical route for recovering the flue gas waste heat 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 original flue gas sensible heat deep utilization and regeneration system is provided.
Therefore, the application adopts the technical proposal that,
the original flue gas sensible heat deep utilization regeneration system comprises a dust removing device, a desulfurizing device and an absorbing device which are sequentially communicated, 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;
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 coal economizer is arranged between the dust removing device and the desulfurizing device;
and the eighth heat exchanger is arranged between the lower part of the absorption device and the economizer, is respectively connected with the lower part of the absorption device and the economizer, and is used for conveying the solution in the first flue gas treatment area into the eighth heat exchanger to exchange heat with a heat exchange medium, and conveying the heat exchange medium after heat exchange into the economizer to exchange heat with flue gas passing through the economizer.
Further, the flue gas absorbing device further comprises a first packing layer and a second packing layer, wherein the first packing layer is arranged in the absorbing device between the first spraying unit and the liquid storage unit, and the second packing layer is arranged in the absorbing device between the second spraying unit and the flue gas inlet.
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;
and the lower part of the absorption device, the sixth heat exchanger and the dilute solution inlet are sequentially communicated.
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 liquid storage unit, the first heat exchanger and the second spraying unit are sequentially communicated, so that the solution in the liquid storage unit is sent into the second spraying unit after heat exchange;
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 system also 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 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; or alternatively, the first and second heat exchangers may be,
the first heat exchanger, the second heat exchanger, the fourth heat exchanger and the third heat exchanger are sequentially communicated, so that the heat supply network incoming water or the low-condensation water sequentially passes through the first heat exchanger, the second heat exchanger, the fourth heat exchanger and the third heat exchanger and exchanges heat with substances entering the corresponding heat exchangers.
Further, the sixth heat exchanger is communicated with the third heat exchanger so as to send the air-extracted condensed water of the sixth heat exchanger into the third heat exchanger for heat exchange, and then return to the boiler for water supply; the steam outlet is communicated with the fourth heat exchanger so as to send the secondary steam into the fourth heat exchanger for heat exchange, and the secondary steam is used as process supplementing water after heat exchange; or alternatively, the first and second heat exchangers may be,
the sixth heat exchanger is communicated with the fourth heat exchanger so as to send the air-extracted condensed water of the sixth heat exchanger into the fourth heat exchanger for heat exchange, and then return to the boiler for water supply; the steam outlet is communicated with the third heat exchanger so as to send the secondary steam into the third heat exchanger for heat exchange, and the secondary steam is used as process supplementing water after heat exchange.
Further, a smoke inlet is formed in the lower portion of the absorption device, a smoke outlet is formed in the upper portion of the absorption device, the smoke outlet is communicated with the chimney, and the first spraying unit, the liquid storage unit and the second spraying unit are all located between the smoke inlet and the smoke outlet;
the demister is arranged in the absorption device and is positioned between the first spraying unit and the flue gas 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 application has the following advantages:
1. according to the system for deeply utilizing sensible heat of raw flue gas, provided by the application, a liquid storage unit is arranged in an absorption device, an inner cavity is divided into a first flue gas treatment area and a second flue gas treatment area by utilizing the liquid storage unit, flue gas enters from the bottom of the absorption device and is in countercurrent contact with concentrated solution (such as concentrated salt solution) sprayed on the top 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 inlet temperature of the solution at the top of the second smoke treatment area and then enters the first smoke treatment area, water in smoke is continuously absorbed, and the gradient heat exchange is adopted for the first time, so that the heat exchange quality can be effectively improved. Meanwhile, an economizer is arranged between the dust removing device and the desulfurizing device, the lower part of the absorbing device is connected with the economizer so as to send the solution in the first flue gas treatment area into the economizer, an eighth heat exchanger is arranged between the lower part of the absorbing device and the economizer, the sensible heat of the flue gas is fully recovered, the sensible heat of the raw flue gas and the latent heat of water vapor of the clean flue gas are finally deeply recovered and utilized through the means, a large amount of cold sources are needed for cooling and condensing the flue gas 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 original flue gas sensible heat deep utilization regeneration system provided by the application, 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 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 regenerated into concentrated solution after being treated by the third heat exchanger and the flash tower, and then the concentrated solution is sent to the absorption device, the secondary steam generated by the flash tower enters the fourth heat exchanger to exchange heat with the heat supply network water, the heat supply network water is lifted to 85-90 ℃ for heating or low-adding condensed water, and the cooled condensed water can be used for demister flushing water of the 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 original flue gas sensible heat deep utilization regeneration system provided by the application, steam is pumped by adopting the steam turbine in a heating season, and pumped condensate water is returned to the boiler for water supply after heat exchange of the third heat exchanger or the fourth heat exchanger. 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 basically unaffected. 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 income are solved in the above mode, sensible heat of raw flue gas and latent heat of water vapor of clean flue gas after a desulfurization device are further recovered through an economizer, an eighth heat exchanger, a fifth heat exchanger, a sixth heat exchanger and a flash tank, 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 original flue gas sensible heat deep utilization regeneration system provided by the application not only can use the original flue gas sensible heat for heating heat supply network water or low-condensation water, but also can recover a great amount of latent heat of water vapor in flue gas, and deeply recover 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 more than one third, saves the running cost and has good environmental protection and energy saving effects because the system equipment is simple.
Drawings
In order to more clearly illustrate the embodiments of the present application 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 application, 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 diagram of an original flue gas sensible heat depth utilization regeneration system in an embodiment of the application;
FIG. 2 is a system diagram of a regeneration system for sensible heat depth utilization of raw flue gas in an embodiment of the application;
FIG. 3 is a schematic view of the structure of an absorber device in an embodiment of the present application;
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-eighth heat exchanger; 16-heat supply network incoming water or low-adding condensed water; 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 application 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 application. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.
In the description of the present application, 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 application 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 application. 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 application, 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 application 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 application described below may be combined with each other as long as they do not collide with each other.
Example 1
The embodiment provides a regeneration system for sensible heat deep utilization of raw flue gas, as shown in fig. 1 and 2, which 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 remover, the desulfurizing device 2 can be a desulfurizing tower, the absorbing device 3 can be an absorbing tower, more particularly a spray tower or a packed tower, a flue gas inlet 3-4 is arranged at the lower part of the absorbing device 3, a flue gas outlet 3-5 is arranged at the upper part of the absorbing device, and a liquid storage unit 3-3 is also included, for example, the liquid storage unit 3-3 can be a liquid receiving disc, as shown in fig. 3, the liquid receiving disc is provided with a disc which is matched with the inner cavity of the desulfurizing tower, a through hole is formed in the disc, the through hole is provided with an extending section extending towards the top of the desulfurizing tower along the axial direction of the desulfurizing tower, a liquid storage space is formed between adjacent extending sections, the absorbing device 3 is arranged in the absorbing device, the inner cavity of the absorbing device is divided into a first flue gas treatment area and a second flue gas treatment area, and the flue gas treatment area is suitable for passing through the liquid storage unit 3-3; 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;
the economizer 4 is arranged between the dust removing device 1 and the desulfurizing device 2; specifically, the economizer 4 may be a low-temperature economizer, and by using the low-temperature economizer, the temperature of the flue gas is reduced to about 90 ℃ by using the heat medium circulating water, and the absorbed heat heats the dilute solution by the heat medium circulating water;
an eighth heat exchanger 15 disposed between the lower portion of the absorption device 3 and the economizer 4 and connected to the lower portion of the absorption device 3 and the economizer 4, respectively, to transfer the solution in the first flue gas treatment zone into the eighth heat exchanger 15 to exchange heat with a heat exchange medium, and transfer the heat exchange medium after heat exchange into the economizer 4 to exchange heat with flue gas passing through the economizer 4; specifically, the eighth heat exchanger 15 is a plate heat exchanger, the heat exchange medium can be heat medium circulating water, and the low-temperature economizer and the eighth heat exchanger 15 are adopted to heat the dilute solution, so that the problem of improvement of heat exchanger materials caused by the partition wall type direct heating of the dilute solution of the flue gas can be avoided, and the investment cost is reduced.
In the regeneration system for deeply utilizing sensible heat of raw flue gas, 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 through the liquid storage unit 3-3 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, water in smoke is continuously absorbed, and the gradient heat exchange is adopted for the first time, so that the heat exchange quality can be effectively improved. Meanwhile, an economizer is arranged between the dust removing device and the desulfurizing device, the lower part of the absorbing device is connected with the economizer so as to send the solution in the first flue gas treatment area into the economizer, an eighth heat exchanger is arranged between the lower part of the absorbing device and the economizer, the sensible heat of the flue gas is fully recovered, the sensible heat of the raw flue gas and the latent heat of water vapor of the clean flue gas are finally deeply recovered and utilized through the means, a large amount of cold sources are needed for cooling and condensing the flue gas 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, the flue gas treatment device also comprises a first packing layer and a second packing layer, wherein the first packing layer is arranged in the absorption device 3 between the first spraying unit 3-1 and the liquid storage unit 3-3, and the second packing layer is arranged in the absorption device 3 between the second spraying unit 3-2 and the flue gas inlet 3-4; in particular, the packing in the first packing layer and the second packing layer may be structured packing or random packing.
Further, a regeneration system is also included, the regeneration system includes a flash tank 18, wherein the upper part is provided with a dilute solution inlet and a steam outlet respectively, and the lower part is provided with a concentrated solution outlet; specifically, a dilute solution inlet is arranged at the middle part of the device, and a steam outlet is arranged at the upper part of the device; the lower part of the absorption device 3, the sixth heat exchanger 17 and the dilute solution inlet are sequentially communicated; in particular, the sixth heat exchanger 17 may be a plate heat exchanger.
In addition, the heat source is driven by the regeneration system to heat the air for the unit in heating season, and the heat supply network water or the circulating heat medium water or the low condensation water in different seasons is heated to different temperatures through the heat supply network heat exchanger.
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 liquid storage unit 3-3, the first heat exchanger 8 and the second spraying unit 3-2 are sequentially communicated, so that the solution in the liquid storage unit 3-3 is sent into the second spraying unit after heat exchange;
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 3.
Example 2
The embodiment provides a system for deeply utilizing sensible heat of raw flue gas, which is based on the embodiment 1, in order to improve the heat exchange effect, fully recover sensible heat in raw flue gas and latent heat of water vapor of clean flue gas 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 spray unit 3-2 are sequentially communicated, so that dilute solution is sent into the second spray 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. 2, 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 embodiment provides a regeneration system for sensible heat deep utilization of raw flue gas, which is based on the embodiment 1 or 2, and further comprises a third heat exchanger 10 and a fourth heat exchanger 11, wherein the first heat exchanger 8, the second heat exchanger 9, the third heat exchanger 10 and the fourth heat exchanger 11 are sequentially communicated, so that heat supply water or low condensation water of a heat supply network 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;
as a variant embodiment, the positions of the third heat exchanger 10 and the fourth heat exchanger 11 are interchangeable according to the temperature of the primary steam condensate and the secondary steam temperature, specifically, the first heat exchanger 8, the second heat exchanger 9, the fourth heat exchanger 11 and the third heat exchanger 10 are sequentially communicated, so that the heat supply network incoming water or the low-adding condensate water sequentially passes through the first heat exchanger 8, the second heat exchanger 9, the fourth heat exchanger 11 and the third heat exchanger 10 and exchanges heat with the substances entering the corresponding heat exchangers.
Further, the sixth heat exchanger 17 is communicated with the third heat exchanger 10, so that the air-extracted condensed water of the sixth heat exchanger 17 is sent to the third heat exchanger 10 for heat exchange, and then returned to the boiler for water supply; the steam outlet is communicated with the fourth heat exchanger 11, secondary steam condensate water of the sixth heat exchanger 17 is sent into the fourth heat exchanger 10, and after heat exchange, the secondary steam condensate water is used as process supplementing water, and heat supply network water or low-adding condensate water passing through the first heat exchanger 8, the second heat exchanger 9, the third heat exchanger 10 and the fourth heat exchanger 11 is used as heat supply network backwater or low-adding system, namely, heat supply network water or low-adding condensate water 16;
as a modified embodiment, the sixth heat exchanger 17 is communicated with the fourth heat exchanger 11, so that the pumping condensate water of the sixth heat exchanger 17 is sent to the fourth heat exchanger 11 for heat exchange, and then returned to the boiler for water supply; the steam outlet is communicated with the third heat exchanger 10 to send the secondary steam condensate water of the sixth heat exchanger 17 into the third heat exchanger 10, and after heat exchange, the secondary steam condensate water is used as process supplementing water, and the heat supply network water or low-adding condensate water passing through the first heat exchanger 8, the second heat exchanger 9, the third heat exchanger 10 and the fourth heat exchanger 11 is used as heat supply network backwater or low-adding system, namely the heat supply network water or low-adding condensate water 16;
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 18 enters the third heat exchanger 10 or the fourth heat exchanger 11 to raise the heat supply network water to 85-90 ℃ for heating or low condensed water.
Example 4
The embodiment provides a regeneration system for sensible heat deep utilization of raw flue gas, on the basis of the embodiment 1, 2 or 3, the lower part of an absorption device 3 is provided with a flue gas inlet 3-4, the upper part is provided with a flue gas outlet 3-5, the flue gas outlet 3-5 is communicated with a chimney 19, and a first spraying unit 3-1, a liquid storage unit 3-3 and a second spraying unit 3-2 are all positioned between the flue gas inlet 3-4 and the flue gas 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.
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, 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 or the low-added condensed water is heated to 50-60 ℃; the technology considers the temperature gradient of the absorber from the top to the bottom, and the cascade heat exchange is carried out through the primary heat exchanger and the secondary heat exchanger of the absorber, so that the quality of hot water can be effectively improved; 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.
And the absorption liquid at the lower section of the absorber is sent to an eighth heat exchanger 15 (a plate-type intermediate heat exchanger), exchanges heat with the heating medium water from the economizer 4, is mixed with the dilute solution heated by the concentrated solution after the heat exchange, heats the heating medium water by utilizing the sensible heat of the original flue gas, and then enters a sixth heat exchanger (a steam heater) to continuously heat to 120-140 ℃ (a heat source adopts pump set steam), and is subjected to flash evaporation in a flash tank. The flue heat exchanger adopts a low-temperature economizer, the temperature of the flue gas is reduced to about 90 ℃ by using heat medium circulating water, and the absorbed heat heats the dilute solution by using the heat medium circulating water. The air-extracted condensed water enters a third heat exchanger (a third heat exchanger of a heat supply network) or a fourth heat exchanger (a fourth heat exchanger of the heat supply network) to exchange heat with heat supply network water, secondary steam at the top of the flash tank enters the fourth heat exchanger (the fourth heat exchanger of the heat supply network) or the third heat exchanger (the third heat exchanger of the heat supply network) to lift the heat supply network water or the low-added condensed water to about 95 ℃, concentrated solution at the bottom of the flash tank exchanges heat with the dilute solution in a fifth heat exchanger (a dilute concentrated solution heat exchanger), and then is cooled to 30-50 ℃ through a seventh heat exchanger (a concentrated solution cooling heat exchanger) and returned to the top of the upper section of the absorber for recycling.
In addition, the temperature of the flue gas outlet of the low-temperature economizer generally needs not to be lower than 90 ℃, the flue gas can be reduced to 90 ℃ by circulating heat medium water, so that the temperature of the raw flue gas at the inlet of the desulfurizing tower can be fully absorbed, the evaporation water quantity of the desulfurizing tower can be reduced, and the process water supplementing quantity of the desulfurizing tower can be reduced. In order to prevent low-temperature corrosion, the water outlet temperature of low-temperature heating medium water is generally above 70 ℃, the temperature of a dilute solution coming out of the bottom of an absorber is about 70 ℃, the heat of raw flue gas can be fully recovered by utilizing the small heat exchange temperature end difference of a plate heat exchanger, when the temperature of the raw flue gas is 140 ℃, the heat of the raw flue gas can basically and completely meet the regeneration heat, the steam quantity of a regeneration system can be reduced by utilizing the sensible heat of the raw flue gas, regeneration can be realized in non-heating seasons even without steam, when the sensible heat of the flue gas cannot completely meet the regeneration heat, the dilute solution is sent into a steam heater to continuously heat (the heat source is the steam of a pumping unit), and finally flash tank flash evaporation is carried out. The air-extracted condensed water enters a third-level heat exchanger of the heat supply network to exchange heat with the heat supply network water, and the secondary steam at the top of the flash tank enters a fourth-level heater of the heat supply network to lift the heat supply network water to 85-90 ℃ for heating or low-adding the condensed water. The concentrated solution at the bottom of the flash tank is returned to the top of the absorption tower after heat exchange with the dilute solution in the dilute concentrated solution heat exchanger.
Specifically, the bottom solution at the lower section of the desulfurizing tower is divided into four parts:
the first part exchanges heat with the heat network secondary heat exchanger and returns to the top of the lower section of the absorption tower to form small circulation. The second portion is sent to the dilute rich solution heat exchanger for heating and then enters the 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. And the fourth part enters the economizer to exchange heat with the flue gas.
The absorption liquid enters from the top of the absorption tower, and through uniform spraying or dripping and reverse convection of the purified flue gas entering from the bottom of the absorption tower, the water vapor in the purified flue gas of the packing layer is absorbed by the concentrated solution, and the spraying layer or dripping layer of the upper section and the lower section can be provided with a standby layer 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 application 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 application.
Claims (4)
1. The original flue gas sensible heat deep utilization regeneration system comprises a dust removing device, a desulfurizing device and an absorbing device which are sequentially communicated, and is characterized by further 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 coal economizer is arranged between the dust removing device and the desulfurizing device;
the eighth heat exchanger is arranged between the lower part of the absorption device and the economizer, and is respectively connected with the lower part of the absorption device and the economizer so as to send the solution in the first flue gas treatment area into the eighth heat exchanger to exchange heat with a heat exchange medium, and send the heat exchange medium after heat exchange into the economizer to exchange heat with flue gas passing through the economizer;
the regeneration system comprises a flash tank, wherein the upper part of the flash tank is provided with a dilute solution inlet and a steam outlet respectively, 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 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 and arranged so as to spray the concentrated solution subjected to heat exchange on the ascending smoke 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;
the liquid storage unit, the first heat exchanger and the second spraying unit are sequentially communicated, so that the solution in the liquid storage unit is sent into the second spraying unit after heat exchange;
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 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 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; or the first heat exchanger, the second heat exchanger, the fourth heat exchanger and the third heat exchanger are sequentially communicated, so that the heat supply network incoming water or the low-condensation water sequentially passes through the first heat exchanger, the second heat exchanger, the fourth heat exchanger and the third heat exchanger and exchanges heat with substances entering the corresponding heat exchangers;
the sixth heat exchanger is communicated with the third heat exchanger so as to send the air-extracted condensed water of the sixth heat exchanger into the third heat exchanger for heat exchange, and then return to the boiler for water supply; the steam outlet is communicated with the fourth heat exchanger so as to send the secondary steam into the fourth heat exchanger for heat exchange, and the secondary steam is used as process supplementing water after heat exchange; or the sixth heat exchanger is communicated with the fourth heat exchanger so as to send the air-extracted condensed water of the sixth heat exchanger into the fourth heat exchanger for heat exchange, and then return the water to the boiler; the steam outlet is communicated with the third heat exchanger so as to send the secondary steam into the third heat exchanger for heat exchange, and the secondary steam is used as process supplementing water after heat exchange.
2. The raw flue gas sensible heat deep utilization regeneration system according to claim 1, further comprising a first filler layer and a second filler layer, wherein the first filler layer is disposed in the absorption device between the first spray unit and the liquid storage unit, and the second filler layer is disposed in the absorption device between the second spray unit and the flue gas inlet.
3. The system for deep utilization of sensible heat of raw flue gas according to claim 2, wherein a flue gas inlet is arranged at the lower part of the absorption device, a flue gas outlet is arranged at the upper part of the absorption device, the flue gas outlet is communicated with a chimney, and the first spraying unit, the liquid storage unit and the second spraying unit are all positioned between the flue gas inlet and the flue gas outlet;
the demister is arranged in the absorption device and is positioned between the first spraying unit and the flue gas outlet.
4. A raw flue gas sensible heat deep utilization regeneration system according to claim 3, wherein 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 spray 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.
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| CN109806751B (en) * | 2019-03-25 | 2021-08-24 | 周岩 | Low-energy-consumption coal-fired boiler flue gas whitening system |
| CN110183024A (en) * | 2019-06-24 | 2019-08-30 | 中国华电科工集团有限公司 | A kind of device using low-grade flue gas concentration waste water |
| CN110372142A (en) * | 2019-07-10 | 2019-10-25 | 中国华电科工集团有限公司 | A kind of device using low-grade flue gas processing waste water |
| CN110394031A (en) * | 2019-07-10 | 2019-11-01 | 中国华电科工集团有限公司 | A kind of waste heat recycles the device for the white joint Waste water concentrating that disappears |
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