CN110124500B - Device and method for deeply recycling water resources in wet flue gas - Google Patents

Device and method for deeply recycling water resources in wet flue gas Download PDF

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CN110124500B
CN110124500B CN201910409189.2A CN201910409189A CN110124500B CN 110124500 B CN110124500 B CN 110124500B CN 201910409189 A CN201910409189 A CN 201910409189A CN 110124500 B CN110124500 B CN 110124500B
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condensation
flue gas
water
desizing
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CN110124500A (en
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张�荣
张银海
陈伟强
俞钱永
关向军
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Hangzhou Yunze Environmental Technology Co ltd
Xinjiang Tianfu Energy Co ltd
Xinjiang Tianfu Environmental Protection Technology Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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Abstract

The invention discloses a device and a method for deeply recovering water resources in wet flue gas, wherein the device comprises a desulfurizing tower, a desulfurizing circulating pump, a condensing and cooling circulating pump and an air cooling tower; a desulfurization spraying layer, a flue gas pre-condensing layer, a desizing and demisting layer, a liquid accumulation layer, a deep condensation cooling layer and a condensation water-collecting layer are sequentially arranged in the desulfurization tower from bottom to top; the desulfurization spraying layer is communicated with the tower kettle through a desulfurization circulating pump; the air cooling tower comprises a tower body and a cooling spray layer arranged in the tower body; the liquid inlet and the liquid outlet of the flue gas pre-condensation layer, the desizing and defogging layer, the deep condensation cooling layer and the condensation water-receiving layer are respectively communicated with the bottom of the air cooling tower and the liquid inlet of the cooling spray layer through a condensate circulating pipeline; the condensation cooling circulating pump is arranged on the condensate circulating pipeline and is used for conveying condensate to the flue gas pre-condensation layer, the desizing and defogging layer, the deep condensation cooling layer and the condensation water-receiving layer. The invention can realize zero water consumption operation of the wet desulphurization system and treat the smoke pollutants at the same time.

Description

Device and method for deeply recycling water resources in wet flue gas
Technical Field
The invention relates to the field of resource and environmental protection, in particular to a device and a method for deeply recycling water resources in wet flue gas.
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. In a long period of time in the future, the current situation that coal still serves as the most main primary energy in China cannot be changed.
The total amount of fresh water resources in China is 28000 billions of cubic meters, the average occupancy of people is 1/3 which is lower than the average level in the world, and the method is one of the countries with the most shortage of the average water resources of people in the world. The water resource distribution of China is extremely unbalanced, the territorial area of the Yangtze river basin and the south area thereof only accounts for 36.5 percent of the whole country, and the water resource amount accounts for 81 percent of the whole country; the territorial area of the Huaihe river basin and the area of the territorial area north of the Huaihe river basin accounts for 63.5 percent of the whole country, and the water resource amount only accounts for 19 percent of the total water resource amount of the whole country.
The developed areas of coal and electricity production in China are highly matched with the areas with high water resource pressure. In 2015, the total water demand of the whole industrial chain of the coal and electricity base is about 99.75 billion cubic meters, wherein the total water demand of the coal mining industry accounts for 66.6 percent of the total water demand of the production industry, the total water demand of the thermal power industry accounts for 22.2 percent of the total water demand of the production industry, and the total water demand of the coal chemical industry accounts for 11.1 percent, which is equal to more than one fourth of 370 billion cubic meters of water which can be distributed in the normal year of the yellow river. In 2016, coal-fired power plants operated nationwide, the coal-electric loading capacity of 4.37 hundred million kilowatts is located in high-water-pressure areas, accounting for 47.8 percent of the coal-electric loading capacity nationwide, and the total water consumption is 25.73 hundred million m 3. The high density coal and electricity industry has further exacerbated the regional water resource crisis, especially in water-deficient areas such as Xinjiang, inner Mongolia, etc.
The wet desulphurization device is one of main water consumption units of a coal-electric machine set, taking a 300MW unit as an example, a desulphurization system consumes about 60m of water per hour3Annual water consumption is about 50 ten thousand tons. Meanwhile, in the operation process of the wet desulphurization device of the thermal power unit, the high-humidity desulphurization tail gas discharges a large amount of moisture to the environment in the form of water vapor, when a 300MW coal-fired unit runs at full load, the desulphurization device discharges about 120 tons of water vapor to the environment per hour, the annual water consumption is about 100 million tons, and the coal and electricity are usedThe water discharge amount of the wet desulphurization device of the unit to the environment is far larger than the water consumption of the wet desulphurization device. 10000Nm of flue gas discharged according to burning ton coal3112g/Nm of moisture contained in wet flue gas3It 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 water evaporated by wet desulphurization. In China, 34-37 billion tons of coal are consumed in a year, and the moisture discharged into the atmosphere by a coal-fired boiler flue gas desulfurization device is as high as thirty billion tons every year. In the operation process of the wet desulphurization device, a large amount of water resource loss is caused by the wet flue gas discharged into the ambient air.
The water resource recovery in the wet desulphurization high-humidity tail gas not only can realize zero water consumption in the desulphurization of the thermal power generating unit, but also can provide part of new water sources. At present, the technology for recovering high-humidity flue gas water resources in China is still in a starting stage.
Disclosure of Invention
The invention provides a device and a method for deeply recovering water resources in wet flue gas, which comprises the steps of firstly removing desulfurization slurry droplets carried in nearly saturated wet flue gas after wet washing by using a one-section tubular condensation demister, primarily completing wet flue gas condensation, temperature reduction and saturation, completing primary water resource recovery and deep purification of flue gas pollutants by performing two-section condensation and temperature reduction on saturated wet flue gas, enabling the flue gas to be supersaturated by performing three-section condensation and temperature reduction on clean saturated wet flue gas, and completing secondary water recovery by performing four-section condensation, temperature reduction and demisting on the primary recovered water, wherein the primary recovered water is used as pulping water and system make-up water of a wet desulfurization system after precipitation and purification treatment, and the secondary recovered clean water is used as other industrial production water, so that zero water consumption operation of the wet desulfurization system is realized, the production water consumption of an industrial plant is reduced, and various pollutants in the flue gas are cooperatively treated.
The specific technical scheme is as follows:
a device for deeply recycling water resources in wet flue gas comprises a desulfurizing tower, a desulfurizing circulating pump, a condensing and cooling circulating pump and an air cooling tower;
a flue gas inlet is formed in the side wall of the bottom of the desulfurization tower, a flue gas outlet is formed in the top of the desulfurization tower, and a tower kettle is arranged at the bottom of the desulfurization tower; a desulfurization spraying layer, a flue gas pre-condensing layer, a desizing and demisting layer, a liquid accumulating layer, a deep condensation cooling layer and a condensation water collecting layer are sequentially arranged in the desulfurization tower and above the flue gas inlet from bottom to top;
the desulfurization spraying layer is communicated with the tower kettle through an inlet and outlet pipeline of a desulfurization circulating pump;
the air cooling tower comprises a tower body and a cooling spraying layer arranged in the tower body; the bottom of the tower body is provided with an air inlet, and the top of the tower body is provided with an air outlet;
condensed fluid pipelines are arranged in the flue gas pre-condensation layer, the desizing and defogging layer, the deep condensation layer and the condensation water-receiving layer, liquid inlets of the condensed fluid pipelines are communicated with an outlet of a condensation cooling circulating pump through pipelines, and liquid outlets of the condensed fluid pipelines are communicated with a liquid inlet of a cooling spraying layer of the air cooling tower through pipelines; the bottoms of the desizing demisting layer and the liquid accumulation layer are provided with liquid discharge ports and are communicated with the outside of the desulfurizing tower through pipelines.
Preferably, the liquid inlets of the condensate pipelines in the flue gas pre-condensation layer, the desizing and demisting layer, the deep condensation layer and the condensation water-receiving layer are provided with regulating valves for controlling the flow of the condensate, so that the temperature drop amplitude of each layer of flue gas is controlled.
In flue gas got into the desulfurizing tower from flue gas entry, the desulfurization circulating pump carried the desulfurization thick liquid in with the tower cauldron to the desulfurization and sprays the layer, sprays the fog nozzle blowout on layer through the desulfurization, carries out the desulfurization washing to the flue gas, and the desulfurization thick liquid falls back the tower cauldron again.
The flue gas pre-condensation layer carries out preliminary condensation cooling on the flue gas carrying the desulfurized slurry liquid drops, so that the flue gas reaches a supersaturated state.
Preferably, a plurality of tube grid type condenser modules are arranged in the flue gas pre-condensation layer, each tube grid type condenser module consists of a plurality of layers of hollow heat exchange tubes distributed at equal intervals and supporting and fixing components, and condensate circulates in the hollow heat exchange tubes. The inlet of the hollow heat exchange tube is connected with the outlet of the condensation cooling circulating pump through a pipeline, and the outlet of the hollow heat exchange tube is connected with the cooling spraying layer in the air cooling tower through a pipeline.
Further preferably, the height of the flue gas pre-condensation layer is 0.1-0.5 m, the number of the hollow heat exchange tubes is 2-4, and the flue gas temperature reduction amplitude of the flue gas pre-condensation layer is 0.2-2 ℃.
The desizing and demisting layer is positioned above the flue gas pre-condensation layer, so that supersaturated wet flue gas is condensed and cooled, and residual slurry fog drops and particles in the flue gas are removed.
Preferably, the desizing and demisting layer consists of a desizing and demisting module, a supporting beam and a liquid guide groove, an upper layer of condensing tube and a lower layer of condensing tube penetrate through the desizing and demisting module, a plurality of desizing and demisting modules are obliquely and symmetrically placed on the supporting beam, the liquid guide groove with a liquid guide plate at the upper part is installed at the bottoms of the two adjacent desizing and demisting modules and is fixed on the outer side of the supporting beam, and a liquid outlet communicated with the outside of the desulfurizing tower is formed in one end of the liquid guide groove.
The inclined symmetrical arrangement of the desizing and demisting modules can increase the flow area of flue gas, reduce the flow velocity of the flue gas, prolong the residence time of the flue gas in the desizing and demisting layers, and is favorable for desizing, demisting and water collection.
The saturated wet flue gas contacts with the desizing and demisting module in the desizing and demisting layer, part of steam condenses into fine fog drops, and contacts with the wall surface of the desizing and demisting module to form a liquid film, and meanwhile, particle dust in the flue gas and the small fog drops gather and grow up and are captured by the liquid film, and the liquid film falls to the bottom end along the inclined wall surface of the desizing and demisting module, falls into the liquid guide groove below, completes the primary water collection and is discharged out of the desulfurizing tower through the discharge port of the liquid guide groove.
Further preferably, the height of the desizing and demisting module in the desizing and demisting layer is 0.5m-1.5m, and the smoke temperature reduction range of the desizing and demisting layer is 0.5-3 ℃.
The liquid accumulation layer is positioned below the deep condensation cooling layer and the condensation water collecting layer and used for collecting condensed water generated by the deep condensation cooling layer and the condensation water collecting layer and discharging the condensed water out of the desulfurizing tower through an outlet.
The deep condensation cooling layer is located above the liquid accumulation layer and is used for cooling clean saturated wet flue gas to enable vapor in the flue gas to reach supersaturation and condense to separate out liquid drops.
Preferably, a plurality of layers of tube sheet type condensation heat exchangers are arranged in the deep condensation cooling layer; the finned tube type condensing heat exchanger is composed of a plurality of metal folding blades arranged at equal intervals and upper and lower two rows of condensing tubes which penetrate through the metal folding blades at equal intervals vertically, one end of each upper-layer condensing tube is communicated with one adjacent lower-layer condensing tube, the upper-layer condensing tube is a condensate liquid inlet tube, and the lower-layer condensing tube is a condensate liquid outlet tube.
Furthermore, the condensation pipe is a corrugated pipe, the corrugated pipe increases the turbulence degree of the condensate in the pipe, the thermal resistance of a boundary layer in the pipe is reduced, on one hand, the metal folding blades increase the heat exchange area so as to increase the cooling amplitude of the flue gas, on the other hand, the metal folding blades can contact the condensed and separated fog drops in the flue gas, and meanwhile, the metal folding blades play a role in fixing and supporting the whole heat exchanger module.
Further preferably, a liquid inlet of each layer of the tube sheet type condensation heat exchanger is provided with a valve for controlling the flow of the condensation liquid, and a liquid outlet is communicated with a cooling spraying layer in the air cooling tower through a pipeline. The number of layers of the condensing heat exchanger can be adjusted according to the temperature and the humidity of inlet flue gas.
Further preferably, in the deep condensation cooling layer, the height of the single-layer condensation heat exchanger is 0.1-0.5 m, the interlayer spacing is 0.1-1.5 m, and the smoke temperature reduction range of the single-layer condensation heat exchanger is 5-10 ℃.
Preferably, the water layer is received in the condensation is equipped with the condensation that a plurality of slopes symmetries were placed and receives the water module, wears to be equipped with two-layer condenser pipe from top to bottom in every condensation receives the water module, and every layer of condenser pipe receives the equidistant distribution of water module incline direction along the condensation, and the one end of every upper condensing pipe and the one end intercommunication of adjacent lower floor's condenser pipe, and the upper condensing pipe is the condensate inlet tube, and the lower floor's condenser pipe is the condensate drain pipe.
The condensation water collecting modules in the condensation water collecting layer are obliquely and symmetrically arranged, so that the flow speed of flue gas can be reduced, the condensation cooling of the flue gas is completed, the density of water mist drops in the flue gas in unit volume is increased, the probability of collision, convergence and growth of the water mist drops is increased, and meanwhile, the water collecting module collects water for three-section condensation and four-section condensation water mist drops.
Further preferably, the height of the condensed water-collecting layer is 0.3m-1.0m, and the smoke temperature reduction amplitude of the condensed water-collecting layer is 1-10 ℃.
Cold air enters from the bottom of the air cooling tower and is in countercurrent contact with condensate sprayed from the cooling spraying layer to exchange heat, the condensate is cooled, and air after heat exchange is discharged from the top of the tower.
Preferably, the cooling amplitude of the condensate in the air cooling tower is 5-20 ℃.
The invention also provides a method for deeply recovering water resources in wet flue gas, which comprises the following steps:
(1) the low-temperature condensate is sent into condensate pipeline inlets in the flue gas pre-condensation layer, the desizing and demisting layer, the deep condensation layer and the condensation water-receiving layer by a condensation cooling circulating pump and enters a condensate pipeline;
(2) the flue gas after wet desulphurization enters a flue gas pre-condensation layer, exchanges heat with the flue gas pre-condensation layer for cooling, and is condensed to a saturated or slightly supersaturated state;
(3) the saturated wet flue gas which is pre-condensed enters a desizing demisting layer, slurry liquid drops and dust particles carried in slurry are removed, the temperature is continuously reduced and condensed in the desizing demisting layer, and partial condensed water generated by water vapor carries out self-cleaning on the desizing demisting layer to prevent the desizing demisting layer from being blocked;
(4) after the desizing and demisting are finished, the supersaturated flue gas enters a deep condensation cooling layer for multistage deep condensation, and most of water vapor in the flue gas is condensed and cooled to generate liquid condensate water;
(5) demisting and collecting water by a condensation water collecting layer, and then discharging the flue gas subjected to deep condensation from a flue gas outlet at the top of the desulfurizing tower;
(6) the high-temperature condensate which completes the condensation and heat exchange of the desulfurization tail gas is sent to the air cooling tower through a pipeline from a condensate liquid outlet to be condensed and cooled on the cooling and spraying layer, and then is recycled as the condensate.
Compared with the prior art, the invention has the following beneficial effects:
(1) the invention provides a solution for realizing the stable operation of a desulfurization tail gas water resource recovery device, which adopts a condenser pipe to pre-condense desulfurized flue gas to saturation and then receive water, utilizes condensed water generated in the condensation process to self-clean a water receiving device, prevents the device from scaling and blocking caused by slurry and dust adhered to the surface of a condensation unit due to flue gas unsaturation in the condensation water receiving process, and greatly improves the operation stability of the condensation water receiving device;
(2) the invention provides a solution for deeply recycling clean water resources in wet flue gas, which removes most of gypsum slurry and dust particles in the flue gas by pre-condensing, desizing and demisting the flue gas, greatly reduces the impurity content in condensed water generated in the deep condensation process, and realizes direct recycling of clean water resources from wet desulphurization tail gas;
(3) the invention provides a production solution with low water consumption or near zero water consumption in an industrial plant area, which is characterized in that deep condensation is carried out on wet flue gas, a large amount of water resources in the wet flue gas are recycled and recycled, the overall water consumption of the plant area is reduced, and near zero water consumption production can be realized in a low-water-consumption plant area.
Drawings
FIG. 1 is a schematic view of a device for deeply recovering water resources in wet flue gas;
FIG. 2 is a schematic diagram of a tube grid condenser module;
FIG. 3 is a schematic view of a partial structure of a desizing and demisting layer;
the reference numbers in the drawings are as follows:
1. a desulfurizing tower; 2. a desulfurization circulating pump; 3. a condensation cooling circulating pump; 4. an air cooling tower; 1-1, a desulfurization spray layer; 1-2, a flue gas pre-condensation layer; 1-2-1, hollow heat exchange tubes; 1-2-2, supporting and fixing parts; 1-3, desizing and demisting layers; 1-3-1, and a liquid accumulation groove; 1-3-2, a condensation heat exchange module; 1-4, collecting liquid layer; 1-5, deep condensation layer; 1-6, condensing and collecting water layer.
Detailed Description
The invention will be described in further detail below with reference to the drawings and examples, which are intended to facilitate the understanding of the invention without limiting it in any way.
As shown in fig. 1, a device for deeply recycling water resources in wet flue gas includes a desulfurization tower 1, a desulfurization circulating pump 2, a condensation cooling circulating pump 3, an air cooling tower 4, and a condensation circulating water pipeline.
Wherein the side wall of the bottom of the desulfurizing tower 1 is provided with a flue gas inlet, the top of the desulfurizing tower is provided with a flue gas outlet, and the bottom in the tower is a tower kettle. A desulfurization spraying layer 1-1, a flue gas pre-condensing layer 1-2, a desizing and demisting layer 1-3, a liquid accumulating layer 1-4, a deep condensation cooling layer 1-5 and a condensation water collecting layer 1-6 are arranged above a smoke inlet in the desulfurizing tower 1 from bottom to top.
At least two layers of sprayers are arranged in the desulfurization spraying layer 1-1, liquid inlets of the sprayers are communicated with the tower kettle through pipelines, a desulfurization circulating pump 2 is arranged on the pipelines, cleaning liquid in the tower kettle is conveyed to the sprayers, and desulfurization washing is carried out on flue gas entering from a flue gas inlet.
The air cooling tower 4 comprises a tower body and a condensate cooling and spraying layer in the tower body, an air inlet is formed in the bottom of the tower body, and an air outlet is formed in the top of the tower body.
Condensed fluid pipelines are arranged in the flue gas pre-condensation layer 1-2, the desizing and defogging layer 1-3, the deep condensation and cooling layer 1-5 and the condensation and water-collecting layer 1-6, liquid inlets of the condensed fluid pipelines are communicated with an outlet of a condensation and cooling circulating pump through pipelines, and a condensed fluid liquid outlet is communicated with a liquid inlet of a cooling and spraying layer of the air cooling tower through a pipeline. The condensate is extracted and conveyed from the bottom of the air cooling tower 4 by the condensation cooling circulating pump 3, the condensate outlets of the condensation heat exchangers overflow to the spraying layer of the air cooling tower 4 through pipelines, fine liquid drops are sprayed out through spray atomization and perform convective heat transfer with rising cold air to perform condensation cooling, the condensate is cooled by 5-20 ℃, and the condensate inlets of the cold heat exchangers on all layers are provided with condensate adjusting valves to control the flow of the condensate.
The flue gas pre-condensation layer 1-2 consists of a plurality of tubular condensation demister modules, as shown in figure 2, each tubular condensation demister module consists of a hollow heat exchange tube 1-2-1 and a supporting and fixing part 1-2-2, an inlet of the hollow heat exchange tube 1-2-1 is connected with an outlet of a condensation cooling circulating pump 3 through a pipeline, and an outlet of the hollow heat exchange tube 1-2-1 is connected with a spray layer in an air cooling tower 4 through a pipeline. The height of the flue gas pre-condensation layer 1-2 is 0.1m-0.5m, and the flow of the condensate is controlled by adjusting the condensate control valve, so that the temperature drop amplitude of the flue gas pre-condensation layer 1-2 is 0.2-2 ℃. The flue gas pre-condensation layer 1-2 can remove desulfurization spray liquid drops carried by flue gas, and simultaneously, the wet flue gas is preliminarily cooled and saturated.
As shown in figure 3, the desizing and defogging layer 1-3 consists of a first-stage water receiving module and a second-stage condensing module. The two-section condensation module is formed by combining a plurality of condensation heat exchange modules 1-3-2, each condensation heat exchange module 1-3-2 is formed by a flaky baffle plate and a heat exchange tube, adjacent flaky baffle plates are combined into a ridge shape, and the upper side and the lower side of each flaky baffle plate are provided with the heat exchange tubes. Wherein, the liquid accumulating tank 1-3-1 of the primary water collecting module is positioned on the supporting beam of the primary condensing demisting module, and the upper port of the liquid accumulating tank 1-3-1 is close to the ridge-shaped lower end of the two-section condensing module.
The flaky baffle plate increases the heat exchange area on one hand, and collects condensed water as a defogging core component on the other hand. The adjacent flaky baffle plates are combined into a ridge shape, so that the flue gas flow area can be increased, the flue gas flow rate can be reduced, the retention time of the flue gas in the desizing and demisting layers 1-3 can be prolonged, and the two-stage condensation demisting and water collection can be facilitated. In order to increase the condensation and temperature reduction amplitude of the flue gas, the inlet and the outlet of the heat exchange tube in each condensation heat exchange module are respectively connected with the inlet and the outlet of the heat exchange main tube, and the inlet and the outlet of the heat exchange main tube are communicated with the bottom of the air cooling tower 4 through a pipeline. The height of the condensation module of the desizing and demisting layers 1-3 is 0.5m-1.5m, and the flow of the condensate is controlled by adjusting the condensate control valve, so that the temperature drop amplitude of the flue gas of the desizing and demisting layers 1-3 is 0.5-3 ℃. And the desizing and defogging layers 1-3 finish condensation, temperature reduction, defogging and water collection of the saturated wet flue gas.
The liquid accumulation layer is positioned above the desizing and demisting layers 1-3, and condensed water of the three sections and the condensed water collecting layer is collected and discharged to the industrial water storage tank through the outlet for industrial production.
The deep condensation cooling layer 1-5 is provided with a plurality of layers of tube sheet type condensation heat exchangers, wherein a heat exchange unit of the tube sheet type condensation heat exchanger is composed of a corrugated pipe and fins, the corrugated pipe increases the turbulence degree of cold liquid in the pipe, the thermal resistance of a boundary layer in the pipe is reduced, the fins increase the heat exchange area on the one hand, so that the cooling range of smoke is increased, on the other hand, fog drops separated out by condensation in smoke are removed, meanwhile, a valve is arranged at the inlet of each layer of heat exchanger to control the flow of cold fluid, the outlet is connected with a spraying layer in the air cooling tower 4 through a pipeline, and the number of layers of the condensation heat exchanger is adjusted and operated according to the inlet smoke temperature and humidity. The heat exchangers in the deep condensation cooling layers 1-5 are preferably provided with two layers, the height of a single-layer condensation module is 0.1-0.5 m, the interlayer spacing is 0.1-1.5 m, and the smoke temperature reduction amplitude of the single-layer heat exchanger is 5-10 ℃.
The condensing heat exchanger in the condensing water-collecting layer 1-6 is similar to the condensing heat exchanger in the desizing and demisting layer 1-3, and is formed into a ridge shape by combining a plurality of condensing heat exchange modules, so that the flow rate of flue gas is reduced, the flue gas is condensed and cooled, the density of water droplets in the flue gas in unit volume is increased, the probability of collision and aggregation and growth of the water droplets is increased, and meanwhile, water is collected for three-section condensation and four-section condensed water droplets. The condensation heat exchange module consists of a sheet baffle plate and heat exchange tubes, wherein the upper side of the condensation heat exchange module is provided with a cold liquid inlet, the lower side of the condensation heat exchange module is provided with a cold liquid outlet, an inlet and an outlet of each heat exchange tube in each heat exchange module are respectively connected with an inlet and an outlet of a heat exchange main tube, the inlet and the outlet of the main tube are communicated with a spraying layer of the air cooling tower 4 through pipelines, the height of a condensation water collecting layer is 1-6 m, and the smoke temperature reduction amplitude of the four sections of condensation heat exchangers is 1-10 ℃.
Flue gas enters a desulfurizing tower 1 from a flue gas inlet, is washed by a desulfurizing spray layer 1-1, then is subjected to desulfurization slurry liquid drops carried by the flue gas by a flue gas pre-condensation layer 1-2, and is subjected to preliminary condensation and temperature reduction of 0.2-2 ℃ on wet flue gas, so that steam in the flue gas reaches a saturated state; saturated wet flue gas passes through a desizing and demisting layer 1-3, the flow cross section of the flue gas is increased due to a ridge type condensation heat exchange module, so that the flow velocity of the flue gas is reduced, the contact time of the flue gas and the wall surface of a condensation heat exchanger tube or a baffle plate is prolonged, the secondary deep condensation temperature of the flue gas is reduced by 0.5-3 ℃, water vapor in the flue gas reaches a supersaturated state and is condensed into fine fog drops, the fine fog drops are mutually aggregated and grow, a layer of liquid film is formed at the tube or plate wall and is reduced to a bottom liquid accumulation tank along an inclined baffle plate to finish primary recovered water, meanwhile, fine particle dust and the fine fog drops in the flue gas are aggregated into large-particle-diameter liquid drops to impact the wall surface of the liquid film, the dust is captured by the liquid film, the primary recovered water containing the dust is discharged out of a tower from a liquid accumulation tank outlet, and is subjected to precipitation purification treatment and then used as water for pulping of a wet desulfurization system and system replenishing water; because wet flue gas is subjected to two-stage condensation, dust removal and demisting, the obtained purified flue gas is clean saturated wet flue gas, the clean saturated wet flue gas rises to pass through a liquid accumulation groove of a liquid accumulation layer 1-4 and contacts with the wall surface of a condensing heat exchanger tube sheet of a deep condensation cooling layer 1-5 above the liquid accumulation layer 1-4 for cooling, at least two layers of tube sheet type condensing heat exchangers are arranged in the deep condensation cooling layer 1-5, the condensing heat exchangers adopt a corrugated tube inserted fin structure, the corrugated tube strengthens the turbulence degree of cold fluid in the tube, reduces the thermal resistance near the inner wall surface of the tube, increases the heat exchange area of the condensing heat exchangers by fins, improves the heat exchange effect, the smoke temperature reduction amplitude of a single-layer condensing heat exchanger reaches 5-10 ℃, saturated vapor in the flue gas is condensed into fine water mist drops again, one part of the water mist drops carried by the flue gas is captured by colliding with the heat exchanger fins, and a liquid accumulation groove from large drops to the lower part of the wall surface is formed, the other part of fine fog drops enter the condensation water-receiving layer 1-6 along with the flue gas, saturated vapor is condensed on the surfaces of the fine fog drops, the fog drops collide with each other and gather and grow up, because the condensation heat exchanger modules in the condensation water-receiving layer 1-6 are arranged in a ridge shape, the flue gas circulation area is increased, the low-flow-rate flue gas carries the fog drops to be captured by the wall surface of the condensation heat exchanger baffle plate, the fog drops fall into the liquid accumulation groove of the liquid accumulation layer 1-4 to complete secondary water recovery, and the purified flue gas is discharged from a chimney.
The above-mentioned embodiments are intended to illustrate the technical solutions and advantages of the present invention, and it should be understood that the above-mentioned embodiments are only specific embodiments of the present invention, and are not intended to limit the present invention, and any modifications, additions, equivalents, etc. made within the scope of the principles of the present invention should be included in the scope of the present invention.

Claims (9)

1. A device for deeply recycling water resources in wet flue gas is characterized by comprising a desulfurizing tower, a desulfurizing circulating pump, a condensing and cooling circulating pump and an air cooling tower;
a flue gas inlet is formed in the side wall of the bottom of the desulfurization tower, a flue gas outlet is formed in the top of the desulfurization tower, and a tower kettle is arranged at the bottom of the desulfurization tower; a desulfurization spraying layer, a flue gas pre-condensing layer, a desizing and demisting layer, a liquid accumulating layer, a deep condensation cooling layer and a condensation water collecting layer are sequentially arranged in the desulfurization tower and above the flue gas inlet from bottom to top;
the desulfurization spraying layer is communicated with the tower kettle through an inlet and outlet pipeline of a desulfurization circulating pump;
the air cooling tower comprises a tower body and a cooling spraying layer arranged in the tower body; the bottom of the tower body is provided with an air inlet, and the top of the tower body is provided with an air outlet;
condensed fluid pipelines are arranged in the flue gas pre-condensation layer, the desizing and defogging layer, the deep condensation layer and the condensation water-receiving layer, liquid inlets of the condensed fluid pipelines are communicated with an outlet of a condensation cooling circulating pump through pipelines, and liquid outlets of the condensed fluid pipelines are communicated with a liquid inlet of a cooling spraying layer of the air cooling tower through pipelines;
the desizing demisting layer consists of desizing demisting modules, a support beam and a liquid guide groove, an upper layer of condensing pipe and a lower layer of condensing pipe are arranged in each desizing demisting module in a penetrating mode, a plurality of desizing demisting modules are obliquely and symmetrically placed on the support beam, the liquid guide groove with a liquid guide plate at the upper part is installed at the bottom of each two adjacent desizing demisting modules and is fixed on the outer side of the support beam, and a liquid discharge port communicated with the outside of the desulfurization tower is arranged at one end of each liquid guide groove;
and a liquid outlet is formed in the bottom of the liquid accumulation layer and is communicated with the outside of the desulfurizing tower through a pipeline.
2. The device for deeply recovering water resources in wet flue gas as claimed in claim 1, wherein a plurality of tube grid type condenser modules are arranged in the flue gas pre-condensation layer, each tube grid type condenser module is composed of a plurality of layers of hollow heat exchange tubes distributed at equal intervals and supporting and fixing parts, and condensate circulates in the hollow heat exchange tubes.
3. The device for deeply recycling water resources in wet flue gas according to claim 1 or 2, wherein the height of the flue gas pre-condensation layer is 0.1-0.5 m, the number of the hollow heat exchange tubes is 2-4, and the smoke temperature reduction amplitude of the flue gas pre-condensation layer is 0.2-2 ℃.
4. The device for deeply recovering water resources in wet flue gas as claimed in claim 1, wherein the height of the desizing and demisting module in the desizing and demisting layer is 0.5m-1.5m, and the smoke temperature reduction range of the desizing and demisting layer is 0.5 ℃ -3 ℃.
5. The device for deeply recovering the water resource in the wet flue gas according to claim 1, wherein a plurality of layers of tube-sheet type condensing heat exchangers are arranged in the deep condensation layer; the finned tube type condensing heat exchanger is composed of a plurality of metal folding blades arranged at equal intervals and upper and lower two rows of condensing tubes which penetrate through the metal folding blades at equal intervals vertically, one end of each upper-layer condensing tube is communicated with one adjacent lower-layer condensing tube, the upper-layer condensing tube is a condensate liquid inlet tube, and the lower-layer condensing tube is a condensate liquid outlet tube.
6. The device for deeply recovering the water resource in the wet flue gas according to claim 5, wherein in the deep condensation cooling layer, the height of the single-layer condensation heat exchanger is 0.1-0.5 m, the interlayer spacing is 0.1-1.5 m, and the flue gas temperature reduction amplitude of the single-layer condensation heat exchanger is 5-10 ℃.
7. The device for deeply recovering water resources in wet flue gas as claimed in claim 1, wherein the condensation water-collecting layer is provided with a plurality of condensation water-collecting modules which are obliquely and symmetrically arranged by penetrating upper and lower layers of condensation pipes, each layer of condensation pipe is distributed at equal intervals along the inclination direction of the condensation water-collecting module, one end of each upper layer of condensation pipe is communicated with one end of an adjacent lower layer of condensation pipe, the upper layer of condensation pipe is a condensation liquid inlet pipe, and the lower layer of condensation pipe is a condensation liquid outlet pipe.
8. The device for deeply recycling water resources in wet flue gas according to claim 7, wherein the height of the condensed water-collecting layer is 0.3m-1.0m, and the flue gas temperature reduction range of the condensed water-collecting layer is 1 ℃ to 10 ℃.
9. A method for deeply recovering water resources in wet flue gas, which is implemented based on the device of any one of claims 1-8, and comprises the following steps:
(1) the low-temperature condensate is sent into condensate inlets in the flue gas pre-condensation layer, the desizing and defogging layer, the deep condensation layer and the condensation and water-receiving layer by a condensation and cooling circulating pump and then enters a condensate pipeline;
(2) the flue gas after wet desulphurization enters a flue gas pre-condensation layer, exchanges heat with the pre-condensation layer for cooling, and is condensed to a saturated or slightly supersaturated state;
(3) the saturated wet flue gas which is pre-condensed enters a desizing demisting layer, slurry liquid drops and dust particles carried in slurry are removed, the temperature is continuously reduced and condensed in the desizing demisting layer, and partial condensed water generated by water vapor carries out self-cleaning on desizing demisting and demisting to prevent the blockage of the desizing demisting layer;
(4) after the desizing and demisting are finished, the supersaturated flue gas enters a deep condensation layer to carry out multistage deep condensation, and most of water vapor in the flue gas is condensed and cooled to generate liquid condensate water;
(5) demisting and collecting water by a condensation water collecting layer, and then discharging the flue gas subjected to deep condensation from a flue gas outlet at the top of the desulfurizing tower;
(6) the high-temperature condensate which completes the condensation and heat exchange of the desulfurization tail gas is sent to the air cooling tower through a pipeline from a condensate liquid outlet to be condensed and cooled on the cooling and spraying layer, and then is recycled as the condensate.
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