CN113769555A - Deep desulfurization and dust removal waste heat recovery system - Google Patents

Deep desulfurization and dust removal waste heat recovery system Download PDF

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Publication number
CN113769555A
CN113769555A CN202111052012.5A CN202111052012A CN113769555A CN 113769555 A CN113769555 A CN 113769555A CN 202111052012 A CN202111052012 A CN 202111052012A CN 113769555 A CN113769555 A CN 113769555A
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flue gas
desulfurization
air preheater
absorption tower
dust removal
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Inventor
段璐
纪任山
张鑫
崔豫泓
牛芳
王瀚锋
王乃继
张红顺
罗伟
龚艳艳
魏琰荣
颜淑娟
柳冠青
程晓磊
梁星
王建朋
刘振宇
夏少波
张朝
杨石
王志强
程鹏
李美军
王永英
李慧
肖翠微
陈隆
李婷
裘星
王志星
王实朴
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China Coal Research Institute Ccri Energy Saving Technology Co ltd
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China Coal Research Institute Ccri Energy Saving Technology Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
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    • 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
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
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    • 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
    • B01D53/60—Simultaneously removing sulfur oxides and 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/80—Semi-solid phase processes, i.e. by using slurries
    • 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
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • 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
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    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L15/00—Heating of air supplied for combustion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
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    • 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
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

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Abstract

The application provides a degree of depth desulfurization is removed dustThe waste heat recovery system comprises a first air preheater, a desulfurization reactor, a pre-deduster, a second air preheater, a deduster and a spray absorption tower; the desulfurization reactor is connected with the first air preheater; the pre-deduster is connected with the desulfurization reactor, and the second air preheater is respectively connected with the pre-deduster and the first air preheater; the dust remover links to each other with the second air preheater, and the spraying absorption tower links to each other with the dust remover, can carry out desulfurization treatment to coal-fired flue gas through desulfurization reactor, and the flue gas after the desulfurization carries out secondary dust removal in getting into the dust remover after the preliminary dust removal through the dust remover in advance, carries out degree of depth desulfurization dust removal through the spraying absorption tower at last for SO in the exhaust flue gas2And the smoke dust reaches the ultra-low emission standard, and the heat is recovered through the connection between the first air preheater and the second air preheater in the dust removal process, so that the energy-saving effect is achieved, and the stable operation of the dust remover is ensured.

Description

Deep desulfurization and dust removal waste heat recovery system
Technical Field
The application relates to the technical field of flue gas treatment, in particular to a deep desulfurization and dedusting waste heat recovery system.
Background
The semidry desulfurization technique is one of the important coal-fired flue gas desulfurization techniques. Water can digest lime and increase the surface activity of the lime, so a large amount of water is generally added in the semi-dry desulfurization, and domestic and foreign researches show that the outlet temperature of a desulfurization reactor is one of the leading factors influencing the semi-dry desulfurization efficiency, and when the outlet temperature of the desulfurization reactor is 10-20 ℃ higher than the adiabatic saturation temperature, the semi-dry desulfurization effect is optimal. This means that when the inlet temperature of the desulfurization reactor is high, a large amount of cold water needs to be added to achieve high desulfurization reaction efficiency, which causes a series of problems in the subsequent flue gas treatment: firstly, the steam in the desulfurization reactor needs a period of evaporation and heat absorption to reduce the temperature of the flue gas to the optimal temperature window of the desulfurization reaction, so that the effective retention time of the desulfurization reaction is reduced, and the desulfurization reaction efficiency is reduced; secondly, the safe and stable operation of the dust collector is influenced by the excessive water vapor content in the flue gas, when the relative humidity of the flue gas is too high, the bag of the bag-type dust collector is easily pasted, the problem of overhigh differential pressure is caused, and the electric field of the electrostatic dust collector is easily punctured, so that the electrostatic dust collector is directly failed; finally, the water vapor content in the flue gas is too large, and the water vapor contains a large amount of latent heat of vaporization and is directly discharged into the atmosphere, so that a large amount of water resources and heat can be wasted. In addition, the desulfurization efficiency of the semi-dry desulfurization technology is lower than that of wet desulfurization, and the semi-dry desulfurization technology is generally suitable for low-sulfur coal and SO2The ultra-low emission is not easy to achieve, which is one of the bottlenecks limiting the popularization of the semi-dry desulfurization technology.
Disclosure of Invention
The present application is directed to solving, at least to some extent, one of the technical problems in the related art.
Therefore, the purpose of this application is to provide a degree of depth desulfurization dust removal waste heat recovery system, can carry out desulfurization treatment to coal-fired flue gas through desulfurization reactor, flue gas after the desulfurization carries out the secondary dust removal in getting into the dust remover after the preliminary dust removal through the dust remover in advance, at last the rethread spraying absorption tower carries out degree of depth desulfurization dust removal, smoke and dust and harmful gas content greatly reduced in the feasible exhaust flue gas, and realize thermal recovery and utilization through being connected between first air preheater and the second air preheater in the dust removal process, reach energy-conservation and guarantee the stable effect of dust remover operation.
In order to achieve the above object, the present application provides a deep desulfurization dust removal waste heat recovery system, which comprises:
the first air preheater is used for cooling the coal-fired flue gas introduced into the first air preheater and recovering heat;
the desulfurization reactor is connected with the first air preheater so that the cooled coal-fired flue gas is introduced into the desulfurization reactor for desulfurization;
the pre-dust remover is connected with the desulfurization reactor and is used for receiving the desulfurized flue gas from the desulfurization reactor and carrying out primary dust removal on the desulfurized flue gas;
the second air preheater is respectively connected with the pre-dust remover and the first air preheater so as to lead the heat recovered in the first air preheater to be introduced into the second air preheater, and the second air preheater heats the flue gas subjected to primary dust removal and received from the pre-dust remover by utilizing the recovered heat;
the dust remover is connected with the second air preheater and is used for receiving the flue gas heated and heated from the second air preheater and performing secondary dust removal on the flue gas heated and heated;
and the spray absorption tower is connected with the dust remover and is used for deeply desulfurizing and dedusting the secondary dedusting smoke received from the dust remover.
And the humidifying stirrer is respectively connected with the pre-dust remover and the desulfurization reactor, is used for receiving a product removed in the pre-dust remover, humidifying and stirring the product and slaked lime fed into the humidifying stirrer, and feeding the mixture after humidifying and stirring into the desulfurization reactor so as to desulfurize the coal-fired flue gas in the desulfurization reactor by using the mixture.
Further, the lime slaking device also comprises a lime tank, wherein the lime tank is connected with the humidifying stirrer and is used for continuously introducing the hydrated lime into the humidifying stirrer.
Further, the humidifying stirrer is connected with the spray absorption tower through a first pipeline, and the humidifying stirrer is used for receiving cooling water in the spray absorption tower so as to perform humidifying and stirring by using the cooling water;
the first pipeline is provided with a first flow regulating valve.
Furthermore, the desulfurization reactor is connected with the spray absorption tower through a second pipeline, and the desulfurization reactor is used for receiving cooling water in the spray absorption tower so as to further humidify the cooled coal-fired flue gas by using the cooling water, thereby improving the desulfurization reaction efficiency;
and a second flow regulating valve is arranged on the second pipeline.
Furthermore, a first atomizing spray gun is arranged in the desulfurization reactor, and the first atomizing spray gun is connected with the second pipeline, so that cooling water in the second pipeline is atomized through the first atomizing spray gun after being introduced into the desulfurization reactor.
The cooling water pipeline is connected with the spray absorption tower and is used for introducing cooling water into the spray absorption tower so as to cool the secondary dedusting smoke introduced into the spray absorption tower by using the cooling water;
the introduction amount of the cooling water is calculated by the following formula:
Figure BDA0003253311830000021
where ρ isgThe density of the flue gas subjected to secondary dust removal in the spray absorption tower is kg/m3，qgIs the volume flow of flue gas, m3/h，t1The temperature at the flue gas inlet of the spray absorption tower is DEG C; t is t2The temperature at the flue gas outlet of the spray absorption tower is DEG C; cWater (W)The specific heat capacity of cooling water is kJ/(kg. K); d is the moisture content of the flue gas in the spray absorption tower, kg/kg.
Furthermore, a second atomization spray gun is arranged in the spray absorption tower, and the second atomization spray gun is connected with a water outlet of the cooling water pipeline and is used for atomizing the cooling water introduced into the spray absorption tower.
And further, the device also comprises a sodium hydroxide solution tank, wherein the sodium hydroxide solution tank is connected with the second atomization spray gun so that the sodium hydroxide solution in the sodium hydroxide solution tank is introduced into the second atomization spray gun to be atomized in the spray absorption tower, and the atomized sodium hydroxide solution reacts with the secondarily dedusted flue gas in the spray absorption tower to perform deep desulfurization.
The third air preheater is respectively connected with the spray absorption tower and the first air preheater so as to lead the heat recovered in the first air preheater to be introduced into the third air preheater, the third air preheater utilizes the recovered heat to heat and raise the temperature of the flue gas which is received from the spray absorption tower and is subjected to deep dust removal, and the flue gas after being heated and raised in temperature is discharged from a chimney.
Additional aspects and advantages of the present application will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the present application.
Drawings
The foregoing and/or additional aspects and advantages of the present application will become apparent and readily appreciated from the following description of the embodiments, taken in conjunction with the accompanying drawings of which:
fig. 1 is a schematic structural diagram of a deep desulfurization dust removal waste heat recovery system according to an embodiment of the present application.
In the figure, 1, a first air preheater; 2. a desulfurization reactor; 3. a pre-deduster; 4. a second air preheater; 5. a dust remover; 6. a spray absorption tower; 7. a humidifying agitator; 8. a first flow regulating valve; 9. a lime tank; 10. a second flow regulating valve; 11. a first atomizing spray gun; 12. a cooling water pipeline; 13. a second atomizing spray gun; 14. a sodium hydroxide solution tank; 15. and a third air preheater.
Detailed Description
Reference will now be made in detail to embodiments of the present application, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present application and are not to be construed as limiting the present application. On the contrary, the embodiments of the application include all changes, modifications and equivalents coming within the spirit and terms of the claims appended hereto.
Fig. 1 is a schematic structural diagram of a deep desulfurization dust removal waste heat recovery system according to an embodiment of the present application.
Referring to fig. 1, a deep desulfurization dust removal waste heat recovery system comprises a first air preheater 1, a desulfurization reactor 2, a pre-dust remover 3, a second air preheater 4, a dust remover 5 and a spray absorption tower 6; the first air preheater 1 is used for cooling the coal-fired flue gas introduced into the first air preheater and recovering heat, and the desulfurization reactor 2 is connected with the first air preheater 1 so that the cooled coal-fired flue gas is introduced into the desulfurization reactor 2 for desulfurization.
Specifically, because the temperature of the coal-fired flue gas is high, the direct introduction into the desulfurization reactor 2 affects the desulfurization efficiency and increases the water consumption in the desulfurization reaction process, and deteriorates the operation environment of the dust remover, thereby causing problems of equipment corrosion and 'white smoke and rain', etc., therefore, the temperature of the coal-fired flue gas needs to be reduced before desulfurization treatment, wherein the first air preheater 1 can be an air heat exchanger, after the coal-fired flue gas is introduced into the first air preheater 1, the temperature of the coal-fired flue gas is reduced to 80-100 ℃ by cooling the cold air in the first air preheater 1, so that the flue gas temperature reaches the temperature window for efficient removal of the desulfurization reactor 2, the desulfurization efficiency is improved while the water consumption is reduced, the temperature of the cold air in the first air preheater 1 is increased by heat exchange while the coal-fired flue gas is reduced, so that the temperature of the cold air in the first air preheater 1 is increased, and the heat in the flue gas is stored in the first air preheater 1 In (1).
In addition, after the coal-fired flue gas is treated by the desulfurization reactor 2, further dust removal is needed, so that the dust remover 5 is arranged, the relative humidity in the flue gas subjected to desulfurization treatment by the desulfurization reactor 2 is too high, and the moisture content of particulate matters is too large, so that the abnormal operation of the dust remover is easily caused, and therefore preliminary dust removal treatment needs to be carried out before the flue gas is introduced into the dust remover 5 for further dust removal, large granular substances in the flue gas are reduced, meanwhile, the flue gas needs to be heated, and the relative humidity of the flue gas is reduced, so that the flue gas is pretreated by arranging the pre-dust remover 3, and the flue gas is heated by arranging the second air pre-dust remover 4, wherein the pre-dust remover 3 can be connected with the desulfurization reactor 2 for receiving the desulfurized flue gas from the desulfurization reactor 2 and preliminarily removing dust from the desulfurized flue gas; wherein the pre-dust remover 3 can be a cyclone separator and can remove 80-95% of desulfurization reaction products in the flue gas desulfurized by the desulfurization reactor 2, and the desulfurization reaction products mainly comprise dust and Ca (OH)2Particles, reduce the ash load and particle size entering the dust remover 5, reduce the abrasion to the air preheater 4, and recycle the separated desulfurization reaction products into the humidifying stirrer 7 for a plurality of times, and increase Ca (OH)2The utilization rate is high, the second air preheater 4 is respectively connected with the pre-dust collector 3 and the first air preheater 1, so that the heat recovered in the first air preheater 1 is introduced into the second air preheater 4, the second air preheater 4 heats and heats the primarily dedusted flue gas received from the pre-dust collector 3 by utilizing the recovered heat, the dust collector 5 is connected with the second air preheater 4, and the dust collector 5 can be a bag dust collector, an electrostatic dust collector or an electric bag dust collector and is used for receiving the heated and heated flue gas from the second air preheater 4 and secondarily dedusting the heated and heated flue gas; wherein the second air preheater 4 can be an air heat exchanger, and the hot air (namely, the stored heat) heated by the first air preheater 1 in the heat exchange process with the coal-fired flue gas can be directly introduced into the second air preheaterIn the air preheater 4 for the flue gas after tentatively removing dust heats for relative humidity in the flue gas reduces, and then prevents effectively that the flue gas from directly letting in dust remover 5 and causing dust remover 5 to operate unusually easily (the sack is stuck with paste, electric precipitation high-voltage electric field is unstable in the high humid environment operation, the breakdown phenomenon appears).
The smoke processed by the dust remover 5 still contains certain sulfur dioxide and a small amount of smoke, so the smoke is deeply processed by the spray absorption tower 6, and the spray absorption tower 6 is connected with the dust remover 5 and used for deeply desulfurizing and dedusting the secondary dust-removed smoke received from the dust remover 5.
In an embodiment of the present application, the waste heat recovery system further includes a humidifying agitator 7, the humidifying agitator 7 is respectively connected to the pre-dust collector 3 and the desulfurization reactor 2, and is configured to receive the product removed from the pre-dust collector 3, humidify and agitate the product and slaked lime introduced into the humidifying agitator 7, and introduce the humidified and agitated mixture into the desulfurization reactor 2, so as to utilize the mixture to desulfurize the coal-fired flue gas in the desulfurization reactor 2, that is, because slaked lime can be used during the desulfurization reaction in the desulfurization reactor 2, slaked lime directly reacts with sulfur dioxide in the coal-fired flue gas, but because both the smoke dust and calcium oxide particles discharged during the pretreatment of flue gas in the pre-dust collector 3 can treat sulfur dioxide, the smoke dust and calcium oxide particles generated in the pre-dust collector 3 can be introduced into the desulfurization reactor 2 for the desulfurization reaction, however, the desulfurization effect is not good when the dry material is directly added into the desulfurization reactor 2, and the desulfurization efficiency is easily reduced because the components are not uniformly distributed after the material is directly added, so that before the material is added into the desulfurization reactor 2, the product removed from the pre-deduster 3 and the hydrated lime are simultaneously added into the humidifying stirrer 7, and the humidifying stirrer 7 is stirred while adding water, so that the obtained mixture contains certain moisture, the moisture can improve the surface activity of the lime, and the Ca (OH) content is improved2With SO2The reaction of (2) is controlled, the water content of the mixture entering the desulfurization reactor (2), namely the desulfurization reactant, is 1.5-2.5%, because the water content is too low, the desulfurization reaction efficiency is reduced, the desulfurization reactant with too high water content is easy to discharge and is not smooth, and the desulfurization reaction is carried outThe sulfur reactor 2 is not easy to disperse, so that the desulfurization efficiency is reduced, the massive reactants are directly precipitated to the bottom of the desulfurization reactor 2 under the action of gravity, and the serious one causes bed collapse.
The spray absorption tower 6 is used for recovering the waste heat of the tail flue gas and simultaneously recovering SO in the flue gas2And deep removal of smoke dust. In addition, in order to save water, cooling water discharged after cooling the flue gas in the spray absorption tower 6 can be directly introduced into the humidifying stirrer 7 to be stirred with solid matters added into the humidifying stirrer 7, therefore, the humidifying stirrer 7 is connected with the spray absorption tower 6 through a first pipeline, the humidifying stirrer 7 is used for receiving the cooling water in the spray absorption tower 6 to perform humidifying and stirring by using the cooling water, sensible heat and latent heat in the flue gas are recovered by the cooling water in the spray absorption tower 6, the temperature of the cooling water is increased, the cooling water is favorable for digestion and activation of fly ash and slaked lime after entering the humidifying stirrer 7, and meanwhile, a first flow regulating valve 8 is arranged on the first pipeline so that the amount of the cooling water introduced into the humidifying stirrer 7 can be controlled through the first flow regulating valve 8.
Meanwhile, it should be noted that the lime slaking device further comprises a lime tank 9, the slaked lime is stored in the lime tank 9, and then the lime tank 9 is controlled to be connected with the humidifying agitator 7 for continuously feeding the slaked lime into the humidifying agitator 7.
In another embodiment of the present application, the desulfurization reactor 2 is connected to the spray absorption tower 6 through a second pipe, the desulfurization reactor 2 is configured to receive cooling water in the spray absorption tower 6, the cooling water humidifies flue gas in the middle and upper parts of the desulfurization reactor 2 in multiple stages, the desulfurization reaction can be further promoted, the desulfurization reaction efficiency is improved, and in addition, in order to control the water flow of the second pipe, a second flow regulating valve 10 is disposed on the second pipe.
It should be described in detail that, the desulfurization reactor 2 is provided with the first atomizing spray gun 11, and the first atomizing spray gun 11 is connected with the second pipeline, so that the cooling water in the second pipeline is atomized by the first atomizing spray gun 11 after being introduced into the desulfurization reactor 2, and the atomized liquid drops can be fully agglomerated with the desulfurization reactant particles in the flue gas, thereby improving the activation performance of the desulfurization reactant surface and enhancing the desulfurization efficiency.
In another embodiment of the present application, the cooling water pipeline 12 is further included, the cooling water pipeline 12 is connected to the spray absorption tower 6, and is used for introducing cooling water into the spray absorption tower 6, so as to cool the flue gas subjected to secondary dust removal in the spray absorption tower 6 by using the cooling water, the temperature of the flue gas is reduced to 30-40 ℃, water vapor in the flue gas is condensed into liquid water, latent heat of vaporization is released, the cooling water absorbs sensible heat and latent heat in the flue gas, the temperature of the flue gas is increased, and the heated water can be used for humidification in a desulfurization reaction and can be used as boiler water after treatment. The process avoids the phenomenon of 'white smoke', realizes the recycling of waste water and waste heat, has higher temperature of recycled water, and is beneficial to the activation of lime and the desulfurization reaction process when being used for semidry desulfurization.
In addition, the flow rate of the cooling water can be controlled by a flow regulating valve on the cooling water pipeline 12, and the inlet amount of the cooling water is calculated by the following formula:
Figure BDA0003253311830000061
where ρ isgThe density of the flue gas subjected to secondary dust removal in the spray absorption tower is kg/m3，qgIs the volume flow of flue gas, m3/h，t1The temperature at the flue gas inlet of the spray absorption tower is DEG C; t is t2The temperature at the flue gas outlet of the spray absorption tower is DEG C; cWater (W)The specific heat capacity of cooling water is kJ/(kg. K); d is the moisture content of the flue gas in the spray absorption tower, kg/kg.
In addition, be provided with second atomizing spray gun 13 in the spraying absorption tower 6, second atomizing spray gun 13 links to each other with the delivery port of cooling water pipeline 12 for cooling water to letting in spraying absorption tower 6 atomizes, can increase the area of contact of water through atomizing, make the cooling water homodisperse in spraying absorption tower 6, the cooling is even, and homodisperse water droplet can increase the area of contact with the flue gas, and then catch remaining smoke and dust granule in the flue gas in spraying absorption tower 6 in a large number, realize the effect of degree of depth dust removal.
In another embodiment of this application, still include solution tank 14, can add NaOH or aqueous ammonia in the solution tank, solution tank 14 links to each other with second atomizing spray gun 13, so that sodium hydroxide solution or aqueous ammonia among the solution tank 14 let in second atomizing spray gun 13 in the spraying absorption tower 6 atomize, so that the flue gas that makes the secondary dust removal among atomized sodium hydroxide solution or aqueous ammonia and the spraying absorption tower 6 reacts, can react with the sulfur dioxide in the flue gas through sodium hydroxide, realize further desulfurization's effect, the aqueous ammonia can react with sulfur dioxide and the nitrogen oxide in the flue gas, realize degree of depth SOx/NOx control.
In addition, the mass concentration of the sodium hydroxide solution or the ammonia water in the solution tank is 10%, and the ratio of the NaOH solution or the ammonia water to the cooling water is 1: 10000-.
In another embodiment of the present application, a third air preheater 15 is further included, the third air preheater 15 is respectively connected to the spray absorption tower 6 and the first air preheater 1, so that the heat recovered in the first air preheater 1 is introduced into the third air preheater 15, the third air preheater 15 heats the flue gas which is received from the spray absorption tower 6 and is subjected to deep desulfurization and dust removal by utilizing the recovered heat, the temperature of the flue gas is increased to 50-60 ℃, the flue gas after heating and temperature increase is discharged from a chimney, wherein the third air preheater 15 can be an air heat exchanger, because the heated hot air (i.e. the stored heat) of the first air preheater 1 in the heat exchange process with the coal-fired flue gas can be directly introduced into the third air preheater 15, the flue gas heating device is used for heating flue gas after advanced treatment and then discharging the flue gas through the chimney after heating, and can effectively prevent the problems that the flue gas temperature is too low, the chimney is corroded, the CEMS system is abnormally monitored, and the like.
It should be noted that, in the description of the present application, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance. In addition, in the description of the present application, "a plurality" means two or more unless otherwise specified.
Any process or method descriptions in flow charts or otherwise described herein may be understood as representing modules, segments, or portions of code which include one or more executable instructions for implementing specific logical functions or steps of the process, and the scope of the preferred embodiments of the present application includes other implementations in which functions may be executed out of order from that shown or discussed, including substantially concurrently or in reverse order, depending on the functionality involved, as would be understood by those reasonably skilled in the art of the present application.
In the description herein, reference to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the application. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
Although embodiments of the present application have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present application, and that variations, modifications, substitutions and alterations may be made to the above embodiments by those of ordinary skill in the art within the scope of the present application.

Claims (10)

1. The utility model provides a degree of depth desulfurization dust removal waste heat recovery system which characterized in that includes:
the first air preheater is used for cooling the coal-fired flue gas introduced into the first air preheater and recovering heat;
the desulfurization reactor is connected with the first air preheater so that the cooled coal-fired flue gas is introduced into the desulfurization reactor for desulfurization;
the pre-dust remover is connected with the desulfurization reactor and is used for receiving the desulfurized flue gas from the desulfurization reactor and carrying out primary dust removal on the desulfurized flue gas;
the second air preheater is respectively connected with the pre-dust remover and the first air preheater so as to lead the heat recovered in the first air preheater to be introduced into the second air preheater, and the second air preheater heats the flue gas subjected to primary dust removal and received from the pre-dust remover by utilizing the recovered heat;
the dust remover is connected with the second air preheater and is used for receiving the flue gas heated and heated from the second air preheater and performing secondary dust removal on the flue gas heated and heated;
and the spray absorption tower is connected with the dust remover and is used for deeply desulfurizing and dedusting the secondary dedusting smoke received from the dust remover.
2. The deep desulfurization dust removal waste heat recovery system according to claim 1, further comprising a humidifying agitator, wherein the humidifying agitator is respectively connected to the pre-dust remover and the desulfurization reactor, and is configured to receive the product removed from the pre-dust remover, humidify and agitate the product and slaked lime introduced into the humidifying agitator, and introduce the humidified and agitated mixture into the desulfurization reactor, so as to desulfurize the coal-fired flue gas in the desulfurization reactor by using the mixture.
3. The deep desulfurization dust removal waste heat recovery system of claim 2, further comprising a lime tank connected with the humidification agitator for continuously feeding the slaked lime into the humidification agitator.
4. The deep desulfurization dust removal waste heat recovery system as set forth in claim 2 or 3, wherein the humidifying agitator is connected with the spray absorption tower through a first pipeline, and is used for receiving cooling water in the spray absorption tower so as to perform humidifying agitation by using the cooling water;
the first pipeline is provided with a first flow regulating valve.
5. The deep desulfurization dust removal waste heat recovery system of claim 1, wherein the desulfurization reactor is connected with the spray absorption tower through a second pipeline, and the desulfurization reactor is used for receiving cooling water in the spray absorption tower so as to further humidify the cooled coal-fired flue gas by using the cooling water, thereby improving the desulfurization reaction efficiency;
and a second flow regulating valve is arranged on the second pipeline.
6. The deep desulfurization dust removal waste heat recovery system of claim 5, wherein a first atomizing spray gun is arranged in the desulfurization reactor, and the first atomizing spray gun is connected with the second pipeline, so that the cooling water in the second pipeline is atomized by the first atomizing spray gun after being introduced into the desulfurization reactor.
7. The deep desulfurization dust removal waste heat recovery system of claim 1, further comprising a cooling water pipeline, wherein the cooling water pipeline is connected with the spray absorption tower and is used for introducing cooling water into the spray absorption tower so as to utilize the cooling water to cool the flue gas subjected to secondary dust removal and introduced into the spray absorption tower;
the introduction amount of the cooling water is calculated by the following formula:
Figure FDA0003253311820000021
where ρ isgThe density of the flue gas subjected to secondary dust removal in the spray absorption tower is kg/m3，qgIs the volume flow of flue gas, m3/h，t1The temperature at the flue gas inlet of the spray absorption tower is DEG C; t is t2The temperature at the flue gas outlet of the spray absorption tower is DEG C; cWater (W)The specific heat capacity of cooling water is kJ/(kg. K); d is the moisture content of the flue gas in the spray absorption tower, kg/kg.
8. The deep desulfurization dust removal waste heat recovery system of claim 7, wherein a second atomization spray gun is arranged in the spray absorption tower, and the second atomization spray gun is connected with the water outlet of the cooling water pipeline and is used for atomizing the cooling water introduced into the spray absorption tower.
9. The deep desulfurization dust removal waste heat recovery system of claim 8, further comprising a sodium hydroxide solution tank, wherein the sodium hydroxide solution tank is connected with the second atomization spray gun, so that the sodium hydroxide solution in the sodium hydroxide solution tank is introduced into the second atomization spray gun to be atomized in the spray absorption tower, so that the atomized sodium hydroxide solution reacts with the secondarily dedusted flue gas in the spray absorption tower to perform deep desulfurization.
10. The deep desulfurization dust removal waste heat recovery system according to claim 1, further comprising a third air preheater, wherein the third air preheater is connected to the spray absorption tower and the first air preheater respectively, so that the heat recovered in the first air preheater is introduced into the third air preheater, the third air preheater heats the flue gas, which is received from the spray absorption tower and subjected to deep dust removal, by using the recovered heat, and the heated flue gas is discharged from a chimney.
CN202111052012.5A 2021-09-08 2021-09-08 Deep desulfurization and dust removal waste heat recovery system Pending CN113769555A (en)

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