CN210485778U - Water-saving and energy-saving type flue gas purification device - Google Patents
Water-saving and energy-saving type flue gas purification device Download PDFInfo
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- CN210485778U CN210485778U CN201920904053.4U CN201920904053U CN210485778U CN 210485778 U CN210485778 U CN 210485778U CN 201920904053 U CN201920904053 U CN 201920904053U CN 210485778 U CN210485778 U CN 210485778U
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Abstract
The utility model discloses a water-saving and energy-saving flue gas purification device, which comprises a washing tower, a washing pump, a condensate clarification tank and an air cooling pipe grid; the heat of the washing slurry and the high-temperature flue gas is recovered in an indirect condensation mode, so that the water evaporation amount in the washing process is reduced; the heat and the gaseous moisture in the saturated flue gas are recovered in a direct spraying and condensing mode, and the recovered heat is used for improving the inlet air temperature of the hearth of the coal-fired boiler. Adopt the utility model discloses energy-saving and water-saving flue gas purification device reduces flue gas purification device water consumption by a wide margin when can realize the make full use of flue gas waste heat, can also reduce generating set unit generating power's coal consumption.
Description
Technical Field
The utility model relates to a resource and environmental protection field especially relate to a water conservation and energy saving type flue gas purification device.
Background
China is a country rich in coal, water and gas, the global coal yield is nearly half from China, the yield of coal in 2016 is 34.11 hundred million tons of raw coal in China, the coal is the first in the world, and the occupation ratio is up to 45.7%. Meanwhile, China is also a country with high coal consumption, coal is dominant in an energy consumption structure, the coal consumption accounts for more than 70% of the total primary energy consumption, industrial and electric coal is mainly used, the total coal consumption rate is over 90%, and civil coal is used as an auxiliary material. A large amount of dust particles and SO are generated in the industrial and electric coal burning processX、NOX、COXPollutants such as HF and HCl are discharged along with high-temperature tail gas, so that a large amount of heat is wasted, the environment is also seriously polluted, the heat of the coal-burning tail gas is recycled, 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, in a thermal power generating unit, the boiler efficiency is an important index for economic operation of the unit, and in heat loss of various boilers, the heat loss of flue gas accounts for more than half of the total heat loss of the boiler. The higher exhaust gas temperature can cause the reduction of boiler efficiency, the annual average coal consumption of the unit is increased, the emission of smoke and dust pollutants is increased, and the economic operation and pollutant emission indexes of the unit are influenced. The research result shows that: when the exhaust gas temperature rises by 30 ℃, the boiler efficiency is reduced by 1 percent, and the unit coal consumption is increased by 3 g/(kWh).
At present, the mode of realizing flue gas waste heat recovery mainly has: the waste heat of the flue gas heats condensed water of a regenerative system of the unit, heats heat supply network water, and heats primary air and secondary air of a boiler. The corresponding flue gas waste heat recovery technology comprises the following steps: the system comprises a low-temperature economizer technology, a low-temperature flue gas treatment technology, a front-mounted liquid-phase medium air preheater and low-temperature economizer combined technology and a novel power station boiler waste heat utilization comprehensive optimization technology. Through the combination of various flue gas waste heat recovery technologies, the design value of the exhaust gas temperature of an active unit is about 130 ℃, but due to the problems of coal burning conditions, the operation level of a power plant and the like, the actual value of the exhaust gas temperature is generally about 150 ℃, and the heat emission loss of the flue gas is still at a high level.
Therefore, how to effectively recycle the waste heat in the secondary high-temperature flue gas with the exhaust gas temperature of less than 150 ℃ becomes a problem to be solved urgently for each thermal power generator set at present.
In the aspect of flue gas pollutant treatment, at present, the installation rate of dust removal, desulfurization and denitration devices of coal-fired units in China is close to 100%, and more than 90% of the installation rate adopts a wet scrubbing flue gas desulfurization technology. Coal fired boiler wet flue gas desulfurization device is at the operation in-process, and high temperature flue gas and spray liquid contact, and moisture evaporation water vapor gets into the flue gas in the washing liquid, forms high temperature saturation wet flue gas and discharges to ambient air in, also discharged a large amount of moisture to ambient air simultaneously, and to the example of 300MW unit, 120m water consumption of desulfurization system3H, including the moisture of the raw smoke of 71.8m3Perh, 40m of water supplement of desulfurization system3And h, the annual running time is 8000 hours, and the annual water consumption of one 300MW unit is 100 ten thousand tons. 10000Nm of flue gas discharged according to burning ton coal3T, the moisture content of the wet smoke is 112g/Nm3It is estimated that the moisture content of the wet flue gas is about 1 ton per 1 ton of coal burned, and the wet flue gas mainly comprises original water content in the coal and desulphurization make-up water. 34-37 billion tons of coal are consumed nationwide in 2014-2017, the moisture discharged into the atmosphere by the flue gas desulfurization device of the coal-fired boiler is as high as thirty billion tons every year, and the amount of the water vapor discharged into the environment by a wet desulfurization system is far larger than that of the water vapor discharged into the environment by a coal-fired power plantWater consumption of the wet desulphurization system of the plant.
Therefore, how to save water for the wet desulphurization device is a difficult problem for treating the coal-fired flue gas pollutants.
SUMMERY OF THE UTILITY MODEL
The utility model provides a water conservation and energy saving type flue gas purification device for coal fired power plant's gas cleaning reduces the gas cleaning device water consumption by a wide margin when realizing flue gas waste heat make full use of, can also reduce generating set unit generating power's coal consumption.
The specific technical scheme is as follows:
a water-saving and energy-saving flue gas purification device comprises a washing tower, a washing pump, a condensate clarifying tank and an air cooling pipe grid;
a washing slurry tank, a slurry tank heat-taking layer, a spraying heat-taking 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 arranged on the tower wall between the slurry pool heat taking layer and the spraying heat taking layer, and a flue gas outlet is arranged at the tower top;
the washing spraying layer is communicated with the washing slurry tank through an inlet and outlet pipeline of the washing pump;
the slurry pool heat taking layer liquid inlet, the spraying heat taking layer liquid inlet and the condensation spraying layer liquid inlet are respectively communicated with the outlet of the condensation pump through pipelines; the slurry pool heat taking layer liquid outlet, the spraying heat taking layer liquid outlet and the liquid receiving layer liquid outlet are respectively communicated with the air cooling pipe grid liquid inlet through pipelines;
the liquid outlet of the air cooling tube grid is communicated with the liquid inlet of the condensate clarifying pool through a pipeline; the liquid outlet of the condensate settling pond is communicated with the inlet of the condensate pump through a pipeline.
Preferably, the air-cooling pipe grid is arranged at an air inlet of a primary fan of a boiler hearth.
Preferably, valves are arranged on respective connecting pipelines of the liquid inlet of the heat taking layer of the slurry tank, the liquid inlet of the spraying heat taking layer and the liquid inlet of the condensing spraying layer and used for opening, closing and adjusting the flow of the condensed liquid.
The utility model discloses based on energy-saving flue gas purification device's energy-saving flue gas purification method of economizing on water, including following step:
(1) by removing dust and NOXThe high-temperature flue gas enters the washing tower from a flue gas inlet, enters the washing spraying layer after being rectified and heat exchanged by a heat taking pipe of the spraying heat taking layer, further exchanges heat with the washing liquid, and is cooled to reach a saturated state, and meanwhile, gaseous pollutants in the flue gas are removed; the saturated flue gas enters a desizing layer for desizing;
the high-temperature washing liquid which completes the washing heat exchange falls into the washing slurry tank;
(2) clean saturated flue gas which is heated, washed and desized passes through the liquid receiving layer to enter the condensation spraying layer, and continuously exchanges heat with low-temperature condensation spraying liquid to cool, the saturated flue gas is cooled to a supersaturated state, a large amount of water vapor in the flue gas is condensed into liquid condensate, the condensate falls into the liquid receiving layer along with the condensation spraying liquid, and is discharged out of the washing tower through the liquid receiving layer;
the flue gas after condensation and temperature reduction is subjected to demisting and drying to remove fine liquid drops and then is discharged from a flue gas outlet;
(3) the high-temperature washing liquid falling into the washing slurry tank and the low-temperature liquid in the heat taking pipe of the heat taking layer of the slurry tank exchange heat rapidly, the temperature of the high-temperature washing liquid is reduced, and meanwhile, the heat taking pipe of the heat taking layer of the slurry tank is used for carrying out layered oxidation on the slurry in the slurry tank;
(4) the high-temperature condensate which finishes heat taking is sent to an air cooling pipe grid through a slurry pool heat taking layer liquid outlet, a spraying heat taking layer liquid outlet and a liquid collecting layer liquid outlet through pipelines, under the action of air flow of 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;
the primary air which completes heat exchange and temperature rise enters a hearth to complete combustion with coal, so that the coal consumption for power generation is reduced;
(5) and the low-temperature condensate after condensation and temperature reduction enters a condensate clarifying tank from a liquid outlet of the air cooling pipe grid through a pipeline for sedimentation and clarification, a small amount of particulate matters are removed, and then the low-temperature condensate is sent to a slurry tank heat taking layer by a condensing pump, is sprayed to the heat taking layer and is further subjected to heat exchange with high-temperature flue gas through a condensation spraying layer, and is recycled.
A plurality of pulp tank heat-taking modules are arranged in the pulp tank heat-taking layer and are fully distributed on the cross section of the washing tower; and a plurality of spraying heat-taking modules are arranged in the spraying heat-taking layer and are fully distributed on the cross section of the washing tower.
Preferably, the height of the slurry tank heat-taking module is 0.3-0.5 m, the slurry tank heat-taking module is immersed under the washing slurry, and the distance from the top end of the slurry tank heat-taking module to the liquid level of the washing slurry tank is 0.5-0.8 m.
Preferably, the height of the spraying heat-taking module is 0.3-0.7 m, the distance between the bottom end of the spraying heat-taking module and the flue gas inlet is 0.3-1.5 m, and the distance between the top end of the spraying heat-taking module and the washing spraying layer is 0.5-2.0 m.
The slurry pool 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 two pipe boxes and a plurality of heat taking pipes communicated between the two pipe boxes.
In each heat taking module, a pipe box at one end is communicated up and down, and a pipe box at the other end 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 heat taking module.
Preferably, the liquid inlet cavity is vertically provided with a liquid equalizing plate, and each liquid equalizing plate is provided with a liquid equalizing hole which is horizontally communicated with the liquid equalizing plate.
The liquid equalizing hole is used for uniformly feeding a liquid flow field in the liquid cavity.
Furthermore, 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 extraction pipes are communicated between the two pipe boxes at equal intervals in a layered mode; furthermore, the heat taking pipes are divided into even layers, and each heat taking pipe is positioned right above the middle point of two adjacent heat taking pipes below the heat taking pipe and is positioned right below the middle point of two adjacent heat taking pipes above the heat taking pipe.
The upper half part of the heat-taking pipe is communicated with the liquid inlet cavity and the pipe box at the other end, and the lower half part of the 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-taking layer, flows through the liquid-dividing plate uniformly, enters the pipe box at the other end from the upper half heat-taking pipe, enters the lower half heat-taking pipe from the lower part of the pipe box at the other end, flows into the liquid outlet cavity from the lower half heat-taking pipe, and is finally discharged from the liquid outlet of the heat-taking layer.
The low-temperature condensate in the heat taking pipe of the heat taking layer of the slurry tank exchanges heat with high-temperature slurry, the low-temperature condensate in the heat taking pipe of the heat taking layer is sprayed to exchange heat with high-temperature flue gas, and meanwhile, the heat taking pipe of the heat taking layer is sprayed to rectify the high-temperature flue gas, 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 high-efficiency purification of the flue gas is realized.
The heat taking pipe is a thin metal pipe; the diameter of a heat taking pipe in the slurry pool heat taking module is 20 mm-50 mm, and the gap distance of the heat taking pipe is 30 mm-60 mm; the diameter of the heat taking pipe in the spraying heat taking module is 30-80 mm, and the gap distance of the heat taking pipe is 50-100 mm.
A plurality of atomizing nozzles are arranged in the condensation spraying layer; preferably, the condensate spraying liquid-gas ratio of the condensate spraying layer is 0.5L/Nm3～3.0L/Nm3。
The air cooling pipe grid comprises a plurality of metal finned pipes; the residence time of the liquid in the metal fin tubes is 10-50 s, and the flow velocity of the liquid in the metal fin tubes is 0.5-2.5 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.
Compared with the prior art, the beneficial effects of the utility model are that:
(1) the utility model provides a high-efficient solution of retrieving flue gas waste heat: a slurry heat-taking layer is arranged in the washing slurry tank, and the heat in the high-temperature slurry is recovered; a spraying and heat-taking layer is arranged in a high-temperature flue gas area at a flue gas inlet of the washing tower, so that a large amount of waste heat in the flue gas is recovered; the heat of the slurry in the slurry tank and the heat of the high-temperature flue gas are extracted step by step through three-stage different temperature areas in combination with spray heat exchange, so that the heat in the high-temperature flue gas is recovered to the maximum extent;
(2) the utility model provides an utilize flue gas waste heat to reduce solution that generating set consumed coal volume: the high-temperature condensate after heat extraction is sent to an air inlet of a primary fan arranged in a boiler hearth, heat is transferred to air at the inlet of the fan by using a finned tube, the temperature of the air entering a coal-fired hearth is increased, and the coal consumption of a generator set under the unit power generation capacity is reduced;
(3) the utility model provides a reduce solution of gas cleaning device water consumption: the temperature of the washing liquid is reduced through the slurry pool heat-taking layer, the temperature of the flue gas is reduced through the spraying heat-taking layer, and the water evaporation amount 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 utility model provides an improve flue gas purification device purification efficiency's solution: the heat taking pipe in the heat taking module is utilized to rectify the inlet flue gas, 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 high-efficiency purification of the flue gas is realized.
Drawings
FIG. 1 is a schematic structural diagram of a water-saving and energy-saving flue gas purification device;
FIG. 2 is a schematic structural view of a heat removal module;
fig. 3 is a schematic cross-sectional structure of fig. 2.
Detailed Description
The invention will be described in further detail with reference to the following figures and examples, which are intended to facilitate the understanding of the invention without limiting it.
As shown in fig. 1, the water-saving and energy-saving flue gas purification device comprises a washing tower 1, a washing pump 2, a condensate 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-taking layer 1-1 is arranged in the washing slurry tank, and a spraying heat-taking layer 1-2, a washing spraying layer 1-3, a desizing layer 1-4, a liquid-collecting layer 1-5, a condensing spraying 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 layers 1-3 are communicated with the washing slurry pool through the inlet and outlet pipelines of the washing pump 2, the washing pump 2 is used for conveying washing slurry to the washing spraying layers 1-3 and spraying the washing slurry uniformly from the washing spraying layers 1-3 to wash flue gas.
A liquid inlet of a slurry pool heat-taking layer 1-1, a liquid inlet of a spraying heat-taking layer 1-2 and a liquid inlet of a condensation spraying layer 1-6 are respectively communicated with an outlet of a 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 pool 4 through a pipeline; the liquid outlet of the condensate settling pond 4 is communicated with the inlet of the condensate pump 3 through a pipeline.
Valves are arranged on respective connecting pipelines of the liquid inlet 1-1 of the slurry pool heat-taking layer, the liquid inlet 1-2 of the spraying heat-taking layer and the liquid inlet 1-6 of the condensing spraying layer and are used for opening, closing and adjusting the flow of the condensate.
The pulp tank heat-taking layer 1-1 and the spraying heat-taking layer 1-2 are internally provided with a plurality of heat-taking modules which are fully distributed on the cross section of the washing tower. The height of the slurry tank heat-taking module is 0.3-0.5 m, the module is immersed in the washing slurry, and the height from the top end of the module to the liquid level of the slurry tank is 0.5-0.8 m; the height of the spraying heat-taking module is 0.3 m-0.7 m, the distance from the bottom end of the spraying heat-taking module to the top end of the inlet flue is 0.3 m-1.5 m, and the height from the top end of the spraying module to the washing spraying layer is 0.5 m-2.0 m.
As shown in fig. 2 and 3, the slurry tank heat-extracting module and the spray heat-extracting module have the same structure and are horizontally arranged in the washing tower, each heat-extracting module consists of a pipe box and a heat-extracting pipe, two ends of each heat-extracting module are respectively provided with one pipe box, and the two pipe boxes at the two ends are communicated and connected by a plurality of layers of heat-extracting pipes which are 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 equalizing plate 1-2-2, and each liquid equalizing plate 1-2-2 is provided with a plurality of liquid equalizing holes which horizontally penetrate through the liquid equalizing plate 1-2-2 and are used for equalizing 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%.
Liquid passing holes which are distributed at equal intervals and communicated with the heat taking pipes are arranged on the vertical side plates at the inner sides of the pipe boxes at the two ends of the heat taking module.
The heat taking pipes are thin metal pipes with two penetrating ends, and two ends of each heat taking pipe are respectively welded and communicated with the liquid passing holes corresponding to the pipe boxes at two ends. The heat taking pipes are arranged in an even number of layers and distributed at equal intervals, and each heat taking pipe is positioned right above the middle point of two adjacent heat taking pipes below and right below the middle point of two adjacent heat taking pipes above.
The end heat taking pipe above the liquid separating plate 1-2-3 is an upper heat taking pipe 1-2-5, the heat taking pipe below the liquid separating plate 1-2-3 is a lower heat taking pipe 1-2-6, and liquid in the upper heat taking pipe and the lower heat taking pipe flows reversely.
The diameter of a heat taking pipe in the slurry pool heat taking module is 20 mm-50 mm, and the gap distance of the heat taking pipe is 30 mm-60 mm; the diameter of the heat taking pipe in the spraying heat taking module is 30-80 mm, and the gap distance of the heat taking pipe is 50-100 mm.
The condensation spraying layer 1-6 is positioned above the liquid receiving layer 1-5 and below the demisting drying layer 1-7, and a plurality of atomizing nozzles are arranged in the condensation spraying layer 1-6. The condensate spraying liquid-gas ratio of the condensate in the condensation spraying layer is 0.5L/Nm3～3.0L/Nm3。
The air cooling pipe grid 5 is arranged at an air inlet of a primary air supply fan room of the power plant boiler; the air cooling pipe grid 5 consists of a liquid inlet, a liquid outlet and a plurality of metal finned pipes communicated with the liquid inlet and the liquid outlet. The residence time of the liquid in the metal fin tubes is 10-50 s, the flow velocity of the liquid in the metal fin tubes is 0.5-2.5 m/s, and the ratio of the surface area of the fins to the surface area of the outer walls of the tubes is 10-50: 1.
The process flow for realizing water and energy conservation in the flue gas purification process by adopting the device is as follows:
complete the dust removal and NO removalXThe high-temperature flue gas enters the washing tower 1 from a flue gas inlet, sequentially passes through a spraying heat-taking layer 1-2 and a washing spraying layer 1-3, rapidly exchanges heat with low-temperature liquid in the spraying heat-taking layer 1-3 heat-taking pipes 1-2-5 and 1-2-6, is uniformly rectified by the spraying heat-taking layer 1-2 heat-taking pipes 1-2-5 and 1-2-6, and then enters the washing spraying layer 1-3. The washing spray liquid is sent to the washing spray layers 1-3 by the washing pump 2 to further exchange heat with the rising flue gas, part of water in the washing liquid is evaporated in the heat exchange process, the temperature of the flue gas is reduced to reach a saturated state, and meanwhile, the flue gas is removedSOXGaseous contaminants such as HF, HCl, etc. The high-temperature washing liquid which completes the washing heat exchange falls into the slurry tank under the action of gravity. The washed and purified saturated flue gas enters a de-sizing layer 1-4 to remove residual washing liquid drops in the flue gas. Clean saturated flue gas which finishes heat taking, washing and desizing passes through the liquid receiving layers 1-5 to enter the condensation spraying layers 1-6 to continue to exchange heat with low-temperature condensation spraying liquid for cooling, the saturated flue gas is cooled to be supersaturated, a large amount of water vapor in the flue gas is condensed into liquid condensate, the condensate falls into the liquid receiving layers 1-5 under the action of gravity along with the condensation spraying liquid, and the condensate is discharged out of the washing tower through the liquid receiving layers 1-5. And the flue gas after condensation and temperature reduction is subjected to demisting and drying layers 1-7 to remove fine liquid drops and then is discharged from an outlet of the washing tower. The high-temperature washing liquid falling into the slurry pool and the low-temperature liquid in the slurry pool heat-taking layer 1-1 exchange heat rapidly, the temperature of the slurry in the slurry pool is reduced, and meanwhile, the heat-taking pipe of the slurry pool heat-taking layer is used for carrying out layered oxidation on the slurry in the slurry pool. The flue gas is cooled by the spraying heat-taking layer 1-3, and the washing liquid is cooled by the slurry pool 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 the liquid inlets of the slurry pool heat taking layer 1-1, the spraying heat taking layer 1-2 and the condensing spraying layer 1-6 by a condensing pump 3 through pipelines, and a plurality of heat taking modules which are fully distributed on the horizontal sections of the washing tower 1 are arranged in the slurry pool heat taking layer 1-1 and the spraying heat taking layer 1-2. Under the pressure action of a condensing pump 3, low-temperature condensate enters a liquid inlet cavity 1-2-1 above a liquid distribution plate 1-2-3 from a liquid inlet of a heat taking module, after the low-temperature condensate is subjected to flow equalization through a liquid equalization plate 1-2-2 pore plate in the liquid inlet cavity 1-2-1, the condensate enters a liquid inlet of an upper heat taking pipe 1-2-5 at the same flow rate and flows along the horizontal direction and exchanges heat with high-temperature flue gas or high-temperature washing liquid, the condensate flowing out of a liquid outlet of the upper heat taking pipe 1-2-5 is guided by a pipe box and then enters a liquid inlet of a lower heat taking pipe 1-2-6 corresponding to the liquid outlet of the upper heat taking pipe 1-2-5 and flows along the reverse direction with the upper heat taking pipe 1-2-5 to continuously exchange heat with the high-temperature flue. The high-temperature condensate after heat exchange enters the liquid outlet cavity 1-2-4 from the liquid outlet of the lower heat taking pipe 1-2-6 and is discharged out of the tower through the liquid outlet of the heat taking module. A plurality of atomizing nozzles are arranged in the condensing and spraying layers 1 to 7, low-temperature condensate is atomized into fog drops through the atomizing nozzles to exchange heat with saturated flue gas, and then the fog drops and condensed water drops fall into the liquid receiving layers 1 to 6 under the action of gravity and are discharged out of the washing tower 1 through the liquid receiving layers 1 to 6.
High-temperature cooling liquid discharged from liquid outlets of the slurry pool heat taking layer 1-1, the spray heat taking layer 1-2 and the liquid receiving layer 1-6 carries absorbed heat and is conveyed to a liquid inlet of an air cooling pipe grid 5 positioned at an air inlet of a primary fan of the boiler through a pipeline, and when the high-temperature cooling liquid flows through finned tubes in the air cooling pipe grid 5, low-temperature ambient air vertically penetrates through the finned tubes in the air cooling pipe grid 5 under the action of negative pressure at the inlet of the primary fan and rapidly exchanges heat with the high-temperature cooling liquid in the tubes. The ambient air which completes heat exchange and temperature rise enters a 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 temperature reduction in the air-cooling tube grid 5 finned tube enters a liquid inlet of a condensate clarifying tank 4 through a liquid outlet of the air-cooling tube grid, fine particulate matter-less dust trapped in the condensation washing process is removed through precipitation, and the low-temperature condensate which completes precipitation and clarification is respectively sent to a liquid inlet of a slurry tank heat taking layer 1-1, a spraying heat taking layer 1-2 and a condensation spraying layer 1-6 through a condensing pump 3 and is used as condensate for recycling.
The above-mentioned embodiment is right the technical scheme and the beneficial effect of the utility model have carried out the detailed description, it should be understood to be above only do the concrete embodiment of the utility model, and not be used for the restriction the utility model discloses, the fan is in any modification, supplementary and equivalence replacement etc. of doing in the principle scope of the utility model all should be contained within the protection scope of the utility model.
Claims (10)
1. A water-saving and energy-saving 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-taking layer, a spraying heat-taking 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 arranged on the tower wall between the slurry pool heat taking layer and the spraying heat taking layer, and a flue gas outlet is arranged at the tower top;
the washing spraying layer is communicated with the washing slurry tank through an inlet and outlet pipeline of the washing pump;
the slurry pool heat taking layer liquid inlet, the spraying heat taking layer liquid inlet and the condensation spraying layer liquid inlet are respectively communicated with the outlet of the condensation pump through pipelines; the slurry pool heat taking layer liquid outlet, the spraying heat taking layer liquid outlet and the liquid receiving layer liquid outlet are respectively communicated with the air cooling pipe grid liquid inlet through pipelines; valves are arranged on respective connecting pipelines of the slurry tank heat-taking layer liquid inlet, the spraying heat-taking layer liquid inlet and the condensing spraying layer liquid inlet and are used for opening, closing and adjusting the flow of the condensate liquid;
the liquid outlet of the air cooling tube grid is communicated with the liquid inlet of the condensate clarifying pool through a pipeline; the liquid outlet of the condensate settling pond is communicated with the inlet of the condensate pump through a pipeline.
2. The water-saving and energy-saving flue gas purification device according to claim 1, wherein the height of the slurry tank heat-extracting module is 0.3m to 0.5m, the slurry tank heat-extracting module is immersed under the washing slurry, and the distance from the top end of the slurry tank heat-extracting module to the liquid level of the washing slurry tank is 0.5m to 0.8 m.
3. The water-saving and energy-saving flue gas purification device according to claim 1, wherein the height of the spraying and heat-taking module is 0.3m to 0.7m, the distance from the bottom end of the spraying and heat-taking module to the flue gas inlet is 0.3m to 1.5m, and the distance from the top end of the spraying and heat-taking module to the washing and spraying layer is 0.5m to 2.0 m.
4. The water-saving and energy-saving flue gas purification device according to claim 1, wherein the slurry tank heat-taking module and the spraying heat-taking module have the same structure; each heat taking module consists of two pipe boxes and a plurality of heat taking pipes communicated between the two pipe boxes.
5. The water-saving and energy-saving flue gas purification device according to claim 4, wherein in each heat-taking module, one end of the pipe box is communicated with the upper part and the lower part, and the other end of the pipe box is divided into an upper cavity and a lower cavity which are not communicated by the 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 heat taking module.
6. The water-saving and energy-saving flue gas purification device according to claim 5, wherein liquid-equalizing plates are vertically arranged in the liquid inlet cavity, and each liquid-equalizing plate is provided with a liquid-equalizing hole horizontally penetrating through the liquid-equalizing plate.
7. The water-saving and energy-saving flue gas purification device according to claim 5, wherein the aperture of the liquid homogenizing hole is 5mm to 20mm, and the opening ratio of the liquid homogenizing plate is 10% to 25%.
8. The water-saving and energy-saving type flue gas purification device according to claim 4, wherein the heat taking pipe is a thin metal pipe; the diameter of a heat taking pipe in the slurry pool heat taking module is 20 mm-50 mm, and the gap distance of the heat taking pipe is 30 mm-60 mm; the diameter of the heat taking pipe in the spraying heat taking module is 30-80 mm, and the gap distance of the heat taking pipe is 50-100 mm.
9. The water-saving and energy-saving flue gas purification device according to claim 1, wherein the air-cooling pipe grid comprises a plurality of metal finned pipes; the residence time of the liquid in the metal fin tubes is 10-50 s, and the flow velocity of the liquid in the metal fin tubes is 0.5-2.5 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. The water-saving and energy-saving flue gas purification device according to claim 1 or 9, wherein the air-cooling pipe grid is installed at an air inlet of a primary air fan of a boiler furnace.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112675690A (en) * | 2020-12-11 | 2021-04-20 | 杭州蕴泽环境科技有限公司 | Low-water-consumption wet desulphurization system and method |
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