CN110124347B - Water-saving energy-saving type flue gas purifying device and method - Google Patents
Water-saving energy-saving type flue gas purifying device and method Download PDFInfo
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- CN110124347B CN110124347B CN201910519215.7A CN201910519215A CN110124347B CN 110124347 B CN110124347 B CN 110124347B CN 201910519215 A CN201910519215 A CN 201910519215A CN 110124347 B CN110124347 B CN 110124347B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 118
- 239000003546 flue gas Substances 0.000 title claims abstract description 106
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000005406 washing Methods 0.000 claims abstract description 102
- 239000002002 slurry Substances 0.000 claims abstract description 81
- 239000007921 spray Substances 0.000 claims abstract description 43
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 238000009833 condensation Methods 0.000 claims abstract description 34
- 230000005494 condensation Effects 0.000 claims abstract description 34
- 238000001816 cooling Methods 0.000 claims abstract description 34
- 238000000746 purification Methods 0.000 claims abstract description 23
- 239000003245 coal Substances 0.000 claims abstract description 17
- 238000010248 power generation Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 177
- 238000005507 spraying Methods 0.000 claims description 60
- 239000003570 air Substances 0.000 claims description 42
- 238000000605 extraction Methods 0.000 claims description 16
- 239000002184 metal Substances 0.000 claims description 12
- 238000009990 desizing Methods 0.000 claims description 11
- 238000001035 drying Methods 0.000 claims description 7
- 239000003344 environmental pollutant Substances 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 7
- 231100000719 pollutant Toxicity 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 6
- 239000012080 ambient air Substances 0.000 claims description 6
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 239000000428 dust Substances 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 3
- 238000007254 oxidation reaction Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 230000000149 penetrating effect Effects 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 2
- 238000004140 cleaning Methods 0.000 claims 1
- 239000002918 waste heat Substances 0.000 abstract description 12
- 238000001704 evaporation Methods 0.000 abstract description 3
- 230000008020 evaporation Effects 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 239000000110 cooling liquid Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 238000007792 addition Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—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
-
- 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
- B01D53/26—Drying gases or vapours
- B01D53/28—Selection of materials for use as drying agents
-
- 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
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- 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
- B01D53/73—After-treatment of removed components
-
- 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
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
- F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- 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
- 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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The invention discloses a water-saving and energy-saving type flue gas purifying device and a method, wherein the device comprises a washing tower, a washing pump, a condensing pump, a condensate clarifying tank and an air cooling pipe grid; the heat of the washing slurry and the high-temperature flue gas is recovered through an indirect condensation mode, so that the evaporation capacity of water in the washing process is reduced; and recovering heat and gaseous moisture in the saturated flue gas in a direct spray condensing mode, and using the recovered heat to raise the inlet air temperature of a hearth of the coal-fired boiler. By adopting the water-saving and energy-saving type flue gas purification method, the water consumption of the flue gas purification device can be greatly reduced while the full utilization of the flue gas waste heat can be realized, and the coal consumption of the unit power generation of the generator set can be reduced.
Description
Technical Field
The invention relates to the field of resource and environmental protection, in particular to a water-saving and energy-saving type flue gas purifying device and method.
Background
A large amount of dust particles and SO are produced in the industrial and electric coal burning process X 、NO X 、CO X Pollutants such as HF, HCl and the like are discharged along with high-temperature tail gas, a large amount of heat is wasted, and serious environmental pollution is caused to the environment, so that the heat of coal-fired tail gas is recovered, the heat loss is reduced, and the pollutants in the flue gas are treated and discharged up to the standard.
In the aspect of flue gas waste heat recovery, boiler efficiency is an important index of economic operation of the unit in the thermal power generation unit, and in various boiler heat loss, the smoke exhaust heat loss accounts for more than half of the total heat loss of the boiler. The higher exhaust gas temperature can lead to the reduction of boiler efficiency, the rise of annual average coal consumption of the unit, and the increase of smoke pollutant discharge amount, and the influence on the economic operation and pollutant discharge index of the unit. The research results show that: every 30 ℃ of the exhaust gas temperature is increased, the boiler efficiency is reduced by 1%, and the unit standard coal consumption is increased by 3 g/(kW.h).
At present, the mode for realizing the recycling of the waste heat of the flue gas mainly comprises the following steps: the flue gas waste heat heats the condensation water of the heat recovery system of the unit, heats the water of the heat supply network and heats the primary air and the secondary air of the boiler. The corresponding flue gas waste heat recovery technology comprises the following steps: a low-temperature economizer technology, a low-temperature flue gas treatment technology, a combination technology of a prepositive liquid-phase medium air preheater and the low-temperature economizer, and a novel comprehensive optimization technology for the waste heat utilization of a power station boiler. By combining multiple flue gas waste heat recovery technologies, the design value of the flue gas temperature of the active unit is about 130 ℃, but the actual value of the flue gas temperature is generally about 150 ℃ due to the problems of coal burning conditions, power plant operation level and the like, and the flue gas heat emission loss is still at a higher level.
Therefore, how to effectively recycle the waste heat in the secondary high-temperature flue gas with the flue gas temperature less than 150 ℃ becomes the problem to be solved urgently for each thermal generator set at present.
In the operation process of the wet desulfurization device of the coal-fired boiler, high-temperature flue gas contacts with spray liquid, water in washing liquid is evaporated into steam to enter the flue gas, high-temperature saturated wet flue gas is formed to be discharged into the ambient air, a large amount of water is discharged into the ambient air, and a 300MW unit is taken as an example, and the desulfurization system consumes 120m of water 3 And/h, including that the raw flue gas contains 71.8m of water 3 Water supplementing 40m for/h and desulfurizing system 3 And/h, when the annual running time is 8000 hours, the annual water consumption of one 300MW unit is 100 ten thousand tons. 10000Nm of flue gas is discharged according to ton of coal combustion 3 Moisture content of wet flue gas of 112g/Nm per t 3 It is estimated that, per 1 ton of coal burned, the wet flue gas takes about 1 ton of water, mainly including the raw water and desulphurized make-up water in the coal.
Therefore, how to save water for the wet desulfurization device is a difficult problem for treating the pollutants of the coal-fired flue gas.
Disclosure of Invention
The invention provides a water-saving energy-saving type flue gas purification device and a method, which are used for flue gas purification of a coal-fired power plant, and can greatly reduce the water consumption of the flue gas purification device and the coal consumption of the unit power generation of a generator set while realizing full utilization of flue gas waste heat.
The specific technical scheme is as follows:
a water-saving and energy-saving type flue gas purification device comprises a washing tower, a washing pump, a condensing pump, a condensate clarifying tank and an air cooling pipe grid;
a washing slurry tank, a slurry tank heat-collecting layer, a spraying heat-collecting layer, a washing spraying layer, a desizing layer, a liquid collecting layer, a condensing spraying layer and a demisting drying layer are sequentially arranged in the washing tower from bottom to top;
a flue gas inlet is formed in the tower wall between the slurry pool heat-taking layer and the spraying heat-taking layer, and a flue gas outlet is formed in the tower top;
the washing spray layer is communicated with the washing slurry tank through a washing pump inlet and outlet pipeline;
the liquid inlet of the heat taking layer of the slurry pond and the liquid inlet of the spraying heat taking layer are respectively communicated with the liquid inlet of the condensing spraying layer through pipelines; the liquid outlet of the heat-taking layer of the slurry pond and the liquid outlet of the spraying heat-taking layer are respectively communicated with the liquid inlet of the air cooling pipe grid through pipelines;
the liquid outlet of the air cooling pipe grid is communicated with the liquid inlet of the condensate clarifying tank through a pipeline; and a liquid outlet of the condensate clarifying tank is communicated with an inlet of the condensing pump through a pipeline.
Preferably, the air cooling pipe grating is arranged at an air inlet of a primary fan of the boiler hearth.
Preferably, valves are arranged on the connecting pipelines of the heat-taking layer liquid inlet of the slurry tank, the spraying heat-taking layer liquid inlet and the condensing spraying layer liquid inlet respectively and are used for opening, closing and adjusting the flow of condensate.
The invention also discloses a water-saving and energy-saving type flue gas purification method based on the water-saving and energy-saving type flue gas purification device, which comprises the following steps:
(1) Through dust removal and NO removal X The high-temperature flue gas enters a washing tower from a flue gas inlet, is rectified by a spray heat-taking layer heat-taking pipe, enters a washing spray layer after heat exchange, and is further subjected to heat exchange with washing liquid, so that the flue gas is cooled to reach a saturated state, and gaseous pollutants in the flue gas are removed; saturated flue gas enters a desizing layer for desizing;
the high-temperature washing liquid which completes washing heat exchange falls into a washing slurry tank;
(2) The clean saturated flue gas which is subjected to heat taking, washing and desizing passes through the liquid collecting layer to enter the condensation spraying layer, and is subjected to heat exchange and cooling with the low-temperature condensation spraying liquid, the saturated flue gas is cooled to a supersaturated state, a large amount of water vapor in the flue gas is condensed and liquefied into liquid condensation water, the condensation water falls into the liquid collecting layer along with the condensation spraying liquid, and the condensation water is discharged out of the washing tower through the liquid collecting layer;
the flue gas after condensation cooling is discharged from a flue gas outlet after fine liquid drops are removed through a demisting and drying layer;
(3) The high-temperature washing liquid falling into the washing slurry tank exchanges heat with the low-temperature liquid in the heat-collecting pipe of the slurry tank heat-collecting layer rapidly, the temperature of the high-temperature washing liquid is reduced, and the slurry in the slurry tank is subjected to layered oxidation by using the heat-collecting pipe of the slurry tank heat-collecting layer;
(4) The high-temperature condensate after heat extraction is sent to an air cooling pipe grid through a liquid outlet of a heat extraction layer of a slurry tank, a liquid outlet of a spray heat extraction layer and a liquid outlet of a liquid receiving layer through pipelines, and under the action of air flow at an air inlet of a primary fan of a boiler hearth, low-temperature ambient air rapidly exchanges heat with the high-temperature condensate through the air cooling pipe grid, and the temperature of the condensate rapidly drops to form low-temperature condensate;
primary air which completes heat exchange and temperature rise enters a hearth to complete combustion with coal, so that the power generation and coal consumption are reduced;
(5) The low-temperature condensate after condensation cooling enters a condensate clarifying tank from a liquid outlet of an air cooling pipe grid through a pipeline to be precipitated and clarified, a small amount of particles are removed, and then the condensate is pumped to a slurry tank heat-taking layer, a spraying heat-taking layer and a condensation spraying layer to continuously exchange heat with high-temperature flue gas for recycling.
A plurality of pulp tank heat-taking modules are arranged in the pulp tank heat-taking layer, and the pulp tank heat-taking modules are distributed on the section of the washing tower; and a plurality of spray heat-taking modules are arranged in the spray heat-taking layer, and the spray heat-taking modules are distributed on the section of the washing tower.
Preferably, the height of the pulp pool heat-taking module is 0.3 m-0.5 m, the pulp pool heat-taking module is immersed under the washing pulp, and the top end of the pulp pool heat-taking module is 0.5 m-0.8 m away from the liquid level of the washing pulp pool.
Preferably, the height of the spraying heat-taking module is 0.3 m-0.7 m, the bottom end of the spraying heat-taking module is 0.3 m-1.5 m away from the flue gas inlet, and the top end of the spraying heat-taking module is 0.5 m-2.0 m away from the washing spraying layer.
The slurry tank heat-taking module and the spraying heat-taking module have the same structure and are horizontally arranged in the washing tower.
Each heating module consists of two pipe boxes and a plurality of heating pipes communicated between the two pipe boxes.
In each heat taking module, one end of the pipe box is communicated up and down, and the other end of the pipe box is divided into an upper cavity and a lower cavity which are not communicated by a liquid separating plate; the upper cavity is a liquid inlet cavity and is communicated with a liquid inlet of the heat taking module; the lower cavity is a liquid outlet cavity and is communicated with a liquid outlet of the heating module.
Preferably, the liquid inlet cavity is vertically provided with liquid homogenizing plates, and each liquid homogenizing plate is provided with a liquid homogenizing hole which horizontally penetrates through the liquid homogenizing plate.
The liquid homogenizing holes are used for homogenizing a liquid flow field in the liquid inlet cavity.
Further, the aperture of the liquid-homogenizing hole is 5mm-20mm, and the aperture ratio of the liquid-homogenizing plate is 10% -25%.
Preferably, the heat collecting pipes are communicated between the two pipe boxes in a layered and equidistant mode; further, the heat-collecting pipes are divided into even layers, and each heat-collecting pipe is located right above the middle point of two adjacent heat-collecting pipes below the heat-collecting pipe and right below the middle point of two adjacent heat-collecting pipes above the heat-collecting pipe.
The upper half heat-taking pipe is communicated with the liquid inlet cavity and the pipe box at the other end, and the lower half heat-taking pipe is communicated with the liquid outlet cavity and the pipe box at the other end.
The low-temperature condensate enters the liquid inlet cavity from the liquid inlet of the heat extraction layer, flows uniformly through the liquid separation plate, enters the other end pipe box from the upper part of the heat extraction pipe, enters the lower part of the heat extraction pipe from the lower part of the other end pipe box, flows into the liquid outlet cavity, and is finally discharged through the liquid outlet of the heat extraction layer.
The low-temperature condensate in the heat-collecting pipe of the slurry pond heat-collecting layer exchanges heat with the high-temperature slurry, the low-temperature condensate in the heat-collecting pipe of the spray heat-collecting layer exchanges heat with the high-temperature flue gas, and meanwhile, the heat-collecting pipe of the spray heat-collecting layer can also rectify the high-temperature flue gas, so that the uniformity of the flue gas in a flow field in a washing tower is enhanced, the utilization rate of washing spray liquid is greatly improved, and the efficient purification of the flue gas is realized.
The heat-collecting pipe is a metal thin pipe; the diameter of a heat-collecting pipe in the slurry tank heat-collecting module is 20-50 mm, and the clearance distance of the heat-collecting pipe is 30-60 mm; the diameter of the heat-collecting pipe in the spray heat-collecting module is 30-80 mm, and the gap distance of the heat-collecting pipe is 50-100 mm.
A plurality of atomizing nozzles are arranged in the condensation spray layer; preferably, the condensate spray liquid-gas ratio of the condensate spray layer is 0.5L/Nm 3 ～3.0L/Nm 3 。
The air cooling pipe grating comprises a plurality of metal fin pipes; the residence time of the liquid in the metal finned tube is 10 s-50 s, and the flow rate of the liquid in the metal finned tube is 0.5 m/s-2.5 m/s; the ratio of the surface area of the fin to the surface area of the outer wall of the tube is 10-50:1.
Compared with the prior art, the invention has the beneficial effects that:
(1) The invention provides a solution for efficiently recovering flue gas waste heat, which comprises the following steps: a slurry heat-taking layer is arranged in the washing slurry tank, and the heat in the high-temperature slurry is recovered; a spray heat-collecting layer is arranged in a high-temperature flue gas area at a flue gas inlet of the washing tower, and waste heat in flue gas is largely recovered; combining spray heat exchange, slurry heat extraction of a slurry tank and high-temperature flue gas heat extraction, and carrying out step-by-step deep heat extraction through three-stage different temperature areas to recover heat in the high-temperature flue gas to the maximum extent;
(2) The invention provides a solution for reducing the coal consumption of a generator set by using the waste heat of flue gas, which comprises the following steps: sending the high-temperature condensate after heat extraction to an air inlet of a primary fan arranged in a boiler hearth, transferring heat to air at an inlet of the fan by using a finned tube, improving the temperature of air entering a coal-fired hearth, and reducing the coal consumption of a generator set under unit power generation;
(3) The invention provides a solution for reducing water consumption of a flue gas purification device, which comprises the following steps: the temperature of the washing liquid is reduced through the heat-taking layer of the slurry tank, and the temperature of the flue gas is reduced through spraying the heat-taking layer, so that the evaporation capacity of water in the flue gas washing process is greatly reduced; the purified flue gas is condensed and cooled by utilizing condensation spray washing, and water vapor in the saturated flue gas is converted into liquid water and recycled, so that the water consumption of the purification device is greatly reduced;
(4) The invention provides a solution for improving the purification efficiency of a flue gas purification device, which comprises the following steps: the inlet flue gas is rectified by the heat collecting pipe in the heat collecting module, so that the uniformity of a flow field of the flue gas in the washing tower is enhanced, the utilization rate of washing spray liquid is greatly improved, and the efficient purification of the flue gas is realized.
Drawings
FIG. 1 is a schematic diagram of a water-saving and energy-saving flue gas purifying device;
FIG. 2 is a schematic diagram of a heating module;
fig. 3 is a schematic cross-sectional structure of fig. 2.
Detailed Description
The invention will be described in further detail below with reference to the drawings and examples, it being noted that the examples described below are intended to facilitate an understanding of the invention and are not intended to limit the invention in any way.
As shown in figure 1, the water-saving and energy-saving flue gas purification device comprises a washing tower 1, a washing pump 2, a condensing pump 3, a condensate clarifying tank 4 and an air cooling pipe grid 5.
The bottom of the washing tower is provided with a washing slurry tank, a slurry tank heat-collecting layer 1-1 is arranged in the washing slurry tank, and a spray heat-collecting layer 1-2, a washing spray layer 1-3, a desizing layer 1-4, a liquid collecting layer 1-5, a condensation spray layer 1-6 and a demisting drying layer 1-7 are sequentially arranged above the washing slurry tank. A flue gas inlet is arranged on the tower wall between the slurry pool heat-taking layer 1-1 and the spraying heat-taking layer 1-2, and a flue gas outlet is arranged on the tower top.
The washing spraying layer 1-3 is communicated with the washing slurry pool through an inlet pipeline and an outlet pipeline of the washing pump 2, the washing pump 2 is used for conveying washing slurry to the washing spraying layer 1-3, and the washing slurry is uniformly sprayed out of the washing spraying layer 1-3 to wash the flue gas.
The liquid inlet of the heat taking layer 1-1 of the slurry pond, the liquid inlet of the spraying heat taking layer 1-2 and the liquid inlet of the condensation spraying layer 1-6 are respectively communicated with the outlet of the condensation pump 3 through pipelines; the liquid outlet of the slurry pool heat-taking layer 1-1, the liquid outlet of the spraying heat-taking layer 1-2 and the liquid outlet of the liquid collecting layer 1-5 are respectively communicated with the liquid inlet of the air cooling pipe grid 5 through pipelines; the liquid outlet of the air-cooling pipe grid 5 is communicated with the liquid inlet of the condensate clarifying tank 4 through a pipeline; the liquid outlet of the condensate clarifying tank 4 is communicated with the inlet of the condensing pump 3 through a pipeline.
Valves are arranged on the connecting pipelines of the liquid inlet of the heat taking layer 1-1 of the slurry pond, the liquid inlet of the spraying heat taking layer 1-2 of the slurry pond and the liquid inlet of the condensing spraying layer 1-6 of the slurry pond respectively and are used for opening, closing and adjusting the flow of condensate.
The slurry tank heat-taking layer 1-1 and the spraying heat-taking layer 1-2 are respectively internally provided with a plurality of heat-taking modules which are distributed on the section of the washing tower. The height of the slurry pool heat-taking module is 0.3 m-0.5 m, the slurry pool heat-taking module is immersed in the washing slurry, and the top end of the slurry pool heat-taking module is 0.5 m-0.8 m away from the liquid level of the slurry pool; the height of the spraying heat-taking module is 0.3 m-0.7 m, the distance between the bottom end of the spraying heat-taking module and the top end of the inlet flue is 0.3 m-1.5 m, and the distance between the top end of the spraying heat-taking module and the washing spraying layer is 0.5 m-2.0 m.
As shown in fig. 2 and 3, the slurry tank heat-taking module and the spraying heat-taking module have the same structure and are horizontally arranged in the washing tower, each heat-taking module consists of a pipe box and heat-taking pipes, two pipe boxes are respectively arranged at two ends of the heat-taking module, and the two pipe boxes at two ends are communicated and connected by a plurality of layers of heat-taking pipes distributed at equal intervals.
The middle part of the pipe box at one end of each heat taking module is divided into two cavities which are not communicated with each other by a liquid separating plate 1-2-3, the upper cavity is a liquid inlet cavity 1-2-1 and is communicated and connected with a liquid inlet of the heat taking module, and the lower cavity is a liquid outlet cavity 1-2-4 and is communicated and connected with a liquid outlet of the heat taking module.
The middle part in each liquid inlet cavity 1-2-1 is vertically provided with a liquid homogenizing plate 1-2-2, and each liquid homogenizing plate 1-2-2 is provided with a plurality of liquid homogenizing holes penetrating through the liquid homogenizing plate 1-2-2 horizontally for homogenizing the liquid flow field in the liquid inlet cavity 1-2-1. The aperture of the liquid-homogenizing hole is 5mm-20mm, and the aperture ratio of the liquid-homogenizing plate 1-2-2 is 10% -25%.
And liquid through holes which are distributed at equal intervals and are communicated with the heat taking pipes are formed in the vertical side plates at the inner sides of the pipe boxes at the two ends of the heat taking module.
The heat-collecting pipes are metal thin pipes with two ends penetrating through the inside, and the two ends of each heat-collecting pipe are welded and communicated with the corresponding liquid through holes of the pipe boxes at the two ends respectively. The heat-collecting pipes are arranged in an even number and distributed at equal intervals, and each heat-collecting pipe is positioned right above the middle point of two adjacent heat-collecting pipes below and right below the middle point of two adjacent heat-collecting pipes above.
The end heat-collecting pipes above the liquid-separating plate 1-2-3 are the upper heat-collecting pipes 1-2-5, the heat-collecting pipes below the liquid-separating plate 1-2-3 are the lower heat-collecting pipes 1-2-6, and the liquid of the upper heat-collecting pipes and the liquid of the lower heat-collecting pipes reversely flow.
The diameter of a heat-collecting pipe in the slurry tank heat-collecting module is 20-50 mm, and the clearance distance of the heat-collecting pipe is 30-60 mm; the diameter of the heat-collecting pipe in the spray heat-collecting module is 30-80 mm, and the gap distance of the heat-collecting pipe is 50-100 mm.
The condensing spray layer 1-6 is positioned above the liquid collecting layer 1-5 and below the demisting and drying layer 1-7, and a plurality of atomizing nozzles are arranged in the condensing spray/1-6. The condensate spraying liquid-gas ratio of the condensate spraying layer is 0.5L/Nm 3 ～3.0L/Nm 3 。
The air cooling pipe grid 5 is arranged at the air inlet of a primary air supply fan room of the power plant boiler; the air-cooling tube grating 5 consists of a liquid inlet, a liquid outlet and a plurality of metal finned tubes communicated with the liquid inlet and the liquid outlet. The residence time of the liquid in the metal finned tube is 10 s-50 s, the flow rate of the liquid in the metal finned tube is 0.5 m/s-2.5 m/s, and the ratio of the surface area of the fin to the surface area of the outer wall of the tube is 10-50:1.
The process flow for realizing water and energy saving in the flue gas purification process by adopting the device comprises the following steps:
complete dust removal and NO removal X The high-temperature flue gas enters the washing tower 1 from a flue gas inlet, sequentially passes through the spray heat-collecting layer 1-2 and the washing spray layer 1-3, rapidly exchanges heat with low-temperature liquid in the heat-collecting pipes 1-2-5 and 1-2-6 of the spray heat-collecting layer 1-3, and enters the washing spray layer 1-3 after being uniformly rectified by the heat-collecting pipes 1-2-5 and 1-2-6 of the spray heat-collecting layer 1-2. The washing spray liquid is sent to the washing spray layer 1-3 by the washing pump 2 to further exchange heat with the rising flue gas, part of water in the washing liquid evaporates in the heat exchange process, the flue gas is cooled to reach a saturated state, and SO in the flue gas is removed at the same time X Gaseous contaminants such as HF and HCl. The high-temperature washing liquid which completes washing heat exchange falls into the slurry tank under the action of gravity. The saturated flue gas after washing and purification enters the desizing layer 1-4 to remove residual washing liquid drops in the flue gas. And the clean saturated flue gas after heat taking, washing and desizing passes through the liquid collecting layer 1-5, enters the condensation spraying layer 1-6, continuously exchanges heat with the low-temperature condensation spraying liquid, cools the saturated flue gas to supersaturation, condenses and liquefies a large amount of water vapor in the flue gas into liquid condensed water, and the condensed water falls into the liquid collecting layer 1-5 along with the condensation spraying liquid under the action of gravity, and is discharged out of the washing tower through the liquid collecting layer 1-5. And the flue gas after condensation cooling is discharged from the outlet of the washing tower after fine liquid drops are removed by the demisting and drying layers 1-7. The high-temperature washing liquid falling into the slurry tank exchanges heat with the low-temperature liquid in the slurry tank heat-taking layer 1-1 rapidly, the slurry temperature of the slurry tank is reduced, and the slurry tank is subjected to layered oxidation by utilizing the heat-taking pipe of the slurry tank heat-taking layer. The flue gas is cooled by the spraying heat-taking layer 1-3, and the washing liquid is cooled by the slurry tank heat-taking layer 1-1, so that the reaction temperature of the flue gas in the washing process can be greatly reduced, the water evaporation amount in the heat exchange process is reduced, and the water consumption in the flue gas purification process is reduced.
The low-temperature condensate is respectively sent to liquid inlets of the slurry tank heat-taking layer 1-1, the spraying heat-taking layer 1-2 and the condensation spraying layer 1-6 by a condensing pump 3 through pipelines, and a plurality of heat-taking modules which are distributed on the horizontal section of the washing tower 1 are arranged in the slurry tank heat-taking layer 1-1 and the spraying heat-taking layer 1-2. Under the pressure of the condensing pump 3, low-temperature condensate enters the liquid inlet cavity 1-2-1 above the liquid separating plate 1-2-3 from the liquid inlet of the heat taking module, flows uniformly through the liquid homogenizing plate 1-2-2 orifice plate in the liquid inlet cavity 1-2-1, enters the liquid inlet of the upper heat taking pipe 1-2-5 at the same flow speed, flows horizontally, exchanges heat with high-temperature flue gas or high-temperature washing liquid, flows out of the condensate through the liquid outlet of the upper heat taking pipe 1-2-5 through the pipe box, enters through the liquid inlet of the lower heat taking pipe 1-2-6 corresponding to the liquid outlet of the upper heat taking pipe 1-2-5, flows reversely along the liquid inlet of the upper heat taking pipe 1-2-5, and continuously exchanges heat with the high-temperature flue gas or the high-temperature washing liquid. The high-temperature condensate after heat exchange enters the liquid outlet cavity 1-2-4 from the liquid outlet of the lower heat extraction pipe 1-2-6, and is discharged out of the tower through the liquid outlet of the heat extraction module. A plurality of atomizing nozzles are arranged in the condensation spraying layer 1-7, low-temperature condensate is atomized into fog drops through the atomizing nozzles, exchanges heat with saturated flue gas, falls into the liquid collecting layer 1-6 with condensed water drops under the action of gravity, and is discharged out of the washing tower 1 through the liquid collecting layer 1-6.
The high-temperature cooling liquid discharged from the liquid outlets of the slurry pool heat-taking layer 1-1, the spray heat-taking layer 1-2 and the liquid collecting layer 1-6 carries absorbed heat to the liquid inlet of the air cooling pipe grid 5 at the air inlet of the primary fan of the boiler through a pipeline, and when the absorbed heat flows through the finned pipes in the air cooling pipe grid 5, low-temperature ambient air vertically passes through the finned pipes in the air cooling pipe grid 5 under the action of negative pressure at the air inlet of the primary fan and exchanges heat with the high-temperature cooling liquid in the pipe rapidly. The ambient air which completes heat exchange and temperature rise enters the boiler hearth to complete combustion reaction with coal, and the temperature of the air entering the hearth is increased, so that the heat required by air preheating is reduced, and the coal consumption in the combustion process is reduced. The low-temperature condensate which completes heat exchange and cooling in the fin tubes of the air cooling tube grating 5 enters the liquid inlet of the condensate clarifying tank 4 through the liquid outlet of the air cooling tube grating, small fine particle dust trapped in the condensation washing process is removed by precipitation, and the low-temperature condensate which completes precipitation clarification is respectively sent to the liquid inlets of the pulp tank heat-taking layer 1-1, the spraying heat-taking layer 1-2 and the condensation spraying layer 1-6 by the condensation pump 3 and is recycled as condensate.
The foregoing embodiments have described the technical solutions and advantages of the present invention in detail, and it should be understood that the foregoing embodiments are merely illustrative of the present invention and are not intended to limit the invention, and any modifications, additions, substitutions and the like that fall within the principles of the present invention should be included in the scope of the invention.
Claims (10)
1. The water-saving and energy-saving type flue gas purification device is characterized by comprising a washing tower, a washing pump, a condensing pump, a condensate clarifying tank and an air cooling pipe grid;
a washing slurry tank, a slurry tank heat-collecting layer, a spraying heat-collecting layer, a washing spraying layer, a desizing layer, a liquid collecting layer, a condensing spraying layer and a demisting drying layer are sequentially arranged in the washing tower from bottom to top;
a plurality of slurry tank heat-taking modules are arranged in the slurry tank heat-taking layer, and the slurry tank heat-taking modules are immersed under the washing slurry; a flue gas inlet is formed in the tower wall between the slurry pool heat-taking layer and the spraying heat-taking layer, and a flue gas outlet is formed in the tower top;
the washing spray layer is communicated with the washing slurry tank through a washing pump inlet and outlet pipeline;
the liquid inlet of the heat taking layer of the slurry pond and the liquid inlet of the spraying heat taking layer are respectively communicated with the liquid inlet of the condensing spraying layer through pipelines; the liquid outlet of the heat-taking layer of the slurry pond and the liquid outlet of the spraying heat-taking layer are respectively communicated with the liquid inlet of the air cooling pipe grid through pipelines;
the liquid outlet of the air cooling pipe grid is communicated with the liquid inlet of the condensate clarifying tank through a pipeline; and a liquid outlet of the condensate clarifying tank is communicated with an inlet of the condensing pump through a pipeline.
2. The water-saving and energy-saving type flue gas purification device according to claim 1, wherein the height of the slurry tank heat-taking module is 0.3 m-0.5 m, and the height of the top end of the slurry tank heat-taking module is 0.5 m-0.8 m from the liquid level of the washing slurry tank.
3. The water-saving and energy-saving type flue gas purification device according to claim 1, wherein the height of the spray heat-taking module is 0.3 m-0.7 m, the bottom end of the spray heat-taking module is 0.3 m-1.5 m from the flue gas inlet, and the top end of the spray heat-taking module is 0.5 m-2.0 m from the washing spray layer.
4. The water and energy saving type flue gas purifying device according to claim 1, wherein the slurry tank heat taking module and the spraying heat taking module have the same structure; each heating module consists of two pipe boxes and a plurality of heating pipes communicated between the two pipe boxes.
5. The water-saving and energy-saving type flue gas purification device according to claim 4, wherein in each heat taking module, one end pipe box is communicated up and down, and the other end pipe box is divided into an upper cavity and a lower cavity which are not communicated by a liquid separation plate; the upper cavity is a liquid inlet cavity and is communicated with a liquid inlet of the heat taking module; the lower cavity is a liquid outlet cavity and is communicated with a liquid outlet of the heating module.
6. The water-saving and energy-saving type flue gas purification device according to claim 5, wherein the liquid inlet cavity is vertically provided with liquid homogenizing plates, and each liquid homogenizing plate is provided with liquid homogenizing holes horizontally penetrating through the liquid homogenizing plate.
7. The water-saving and energy-saving type flue gas purifying device according to claim 5, wherein the aperture of the liquid-homogenizing holes is 5mm-20mm, and the aperture ratio of the liquid-homogenizing plate is 10% -25%.
8. The water and energy saving type flue gas purifying apparatus according to claim 4, wherein the heat collecting pipe is a metal thin pipe; the diameter of a heat-collecting pipe in the slurry tank heat-collecting module is 20-50 mm, and the clearance distance of the heat-collecting pipe is 30-60 mm; the diameter of the heat-collecting pipe in the spray heat-collecting module is 30-80 mm, and the gap distance of the heat-collecting pipe is 50-100 mm.
9. The water and energy saving flue gas cleaning device according to claim 1, wherein the air cooling grid comprises a plurality of metal finned tubes; the residence time of the liquid in the metal finned tube is 10 s-50 s, and the flow rate of the liquid in the metal finned tube is 0.5 m/s-2.5 m/s; the ratio of the surface area of the fins to the surface area of the outer wall of the tube is 10-50:1.
10. A method for purifying flue gas based on the water-saving and energy-saving type flue gas purifying device according to any one of claims 4 to 8, comprising the steps of:
(1) Through dust removal and NO removal X The high-temperature flue gas enters a washing tower from a flue gas inlet, is rectified by a spray heat-taking layer heat-taking pipe, enters a washing spray layer after heat exchange, and is further subjected to heat exchange with washing liquid, so that the flue gas is cooled to reach a saturated state, and gaseous pollutants in the flue gas are removed; saturated flue gas enters a desizing layer for desizing;
the high-temperature washing liquid which completes washing heat exchange falls into a washing slurry tank;
(2) The clean saturated flue gas which is subjected to heat taking, washing and desizing passes through the liquid collecting layer to enter the condensation spraying layer, and is subjected to heat exchange and cooling with the low-temperature condensation spraying liquid, the saturated flue gas is cooled to a supersaturated state, a large amount of water vapor in the flue gas is condensed and liquefied into liquid condensation water, the condensation water falls into the liquid collecting layer along with the condensation spraying liquid, and the condensation water is discharged out of the washing tower through the liquid collecting layer;
the flue gas after condensation cooling is discharged from a flue gas outlet after fine liquid drops are removed through a demisting and drying layer;
(3) The high-temperature washing liquid falling into the washing slurry tank exchanges heat with the low-temperature liquid in the heat-collecting pipe of the slurry tank heat-collecting layer rapidly, the temperature of the high-temperature washing liquid is reduced, and the slurry in the slurry tank is subjected to layered oxidation by using the heat-collecting pipe of the slurry tank heat-collecting layer;
(4) The high-temperature condensate after heat extraction is sent to an air cooling pipe grid through a liquid outlet of a heat extraction layer of a slurry tank, a liquid outlet of a spray heat extraction layer and a liquid outlet of a liquid receiving layer through pipelines, and under the action of air flow at an air inlet of a primary fan of a boiler hearth, low-temperature ambient air rapidly exchanges heat with the high-temperature condensate through the air cooling pipe grid, and the temperature of the condensate rapidly drops to form low-temperature condensate;
primary air which completes heat exchange and temperature rise enters a hearth to complete combustion with coal, so that the power generation and coal consumption are reduced;
(5) The low-temperature condensate after condensation cooling enters a condensate clarifying tank from a liquid outlet of an air cooling pipe grid through a pipeline to be precipitated and clarified, a small amount of particles are removed, and then the condensate is pumped to a slurry tank heat-taking layer, a spraying heat-taking layer and a condensation spraying layer to continuously exchange heat with high-temperature flue gas for recycling.
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| CN111558294B (en) * | 2020-05-27 | 2022-04-22 | 杭州蕴泽环境科技有限公司 | Wet flue gas purification system and method with energy-saving function |
| CN111589290B (en) * | 2020-05-27 | 2024-02-20 | 新疆天富环保科技有限公司 | Energy-saving type boiler tail gas purification system and method |
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