CN113457405A - Device and method for cooperatively removing sulfur trioxide and hydrogen chloride in coal-fired flue gas - Google Patents
Device and method for cooperatively removing sulfur trioxide and hydrogen chloride in coal-fired flue gas Download PDFInfo
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- CN113457405A CN113457405A CN202110901002.8A CN202110901002A CN113457405A CN 113457405 A CN113457405 A CN 113457405A CN 202110901002 A CN202110901002 A CN 202110901002A CN 113457405 A CN113457405 A CN 113457405A
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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
- B01D53/46—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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- 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
- B01D53/504—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 device
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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
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
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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
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/204—Inorganic halogen compounds
- B01D2257/2045—Hydrochloric acid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Abstract
The embodiment of the application provides a device and a method for cooperatively removing sulfur trioxide and hydrogen chloride from coal-fired flue gas, wherein an absorbent solution injection system is connected with an absorbent solution preparation system through a pipeline, the absorbent solution injection system is used for receiving absorbent solution conveyed by the absorbent solution preparation system and injecting the absorbent solution to the flue gas in a flue so as to enable an absorbent in the absorbent solution to react with gas to be removed in the flue gas to generate a solid product and remove the gas to be removed from the flue gas, therefore, the cooperative removal of the sulfur trioxide and the hydrogen chloride in the flue gas can be realized, the corrosion and scaling blockage risks of tail flue equipment and a heat exchange surface can be reduced, the emission of sulfur trioxide to the atmosphere is reduced, the standard emission of sulfur trioxide is realized, the desulfurization wastewater amount can be greatly reduced, and meanwhile, downstream equipment is protected from the corrosion and damage of the sulfur trioxide and the hydrogen chloride, and maintaining the stable operation of the equipment.
Description
Technical Field
The application relates to the technical field of flue gas treatment, in particular to a device and a method for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas in a synergistic manner.
Background
The sulfur trioxide is one of the important precursors of particulate matters and acid rain, and the sulfur trioxide discharged into the atmosphere of a coal-fired power plant reacts with alkaline components to generate sulfate particulate matters, so that blue smoke plume is generated. Sulfur trioxide also combines with moisture in the air and exists in the form of acid rain. In addition to environmental concerns, sulfur trioxide in coal-fired flue gas can cause the acid dew point of the flue gas to rise, causing acid corrosion of the flue. Sulfur trioxide and SCR denitration escape ammonia in the flue gas generate Ammonium Bisulfate (ABS), which causes the problems of blockage of an air preheater, bag pasting of a bag-type dust remover, dust sticking of polar plates and polar lines of an electric dust remover and the like, and brings hidden dangers to economic, safe and stable operation of a unit.
Coal-fired power plants consume large quantities of coal, chlorine-containing substances are decomposed during the combustion of the coal, and chlorine elements are mainly released into flue gas in the form of HCl. Because of the relatively low HCl content in the coal-fired flue gas, at present, no independent dechlorination facility exists, and most of the chlorine in the flue gas is enriched in the desulfurizing tower through a wet desulphurization system. In the operation process of the wet desulphurization facility, chloride ions are continuously enriched in the slurry, thus influencing the desulphurization reaction and reducing the desulphurization efficiency. In order to avoid affecting the desulfurization operation and preventing corrosion of equipment, the wastewater is periodically discharged to reduce the concentration of chloride ions in the slurry. In recent years, a series of water resource conservation policies are intensively developed in China, and from the aspects of economic operation and environmental protection, coal-fired power plants are required to adopt advanced water conservation and wastewater zero discharge technologies. The desulfurization wastewater has complex water quality, large treatment difficulty and high cost, the investment cost of several main desulfurization wastewater zero-discharge technical routes at present reaches 150-200 ten thousand per ton, and the problems of scaling blockage, high energy consumption, high cost and the like exist in different degrees after the desulfurization wastewater is put into operation. Desulfurization wastewater has become a main factor that restricts coal-fired power plants from realizing zero discharge of wastewater.
At present, the technology for removing sulfur trioxide from coal-fired flue gas is not completely mature. The hydrogen chloride removal from the flue gas is only reported in the literature, and no engineering application is found. Sulfur trioxide in the flue gas causes great harm to downstream equipment. The hydrogen chloride content in the flue gas is high, so that the discharge amount of desulfurization waste water is large, and the implementation difficulty and investment of zero discharge of the waste water of a coal-fired power plant are increased. Sulfur trioxide and hydrogen chloride in the flue gas seriously affect the economical, safe and environment-friendly operation of the coal-fired unit.
Disclosure of Invention
The embodiment of the application provides a device and a method for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas in a synergistic manner, and the sulfur trioxide and the hydrogen chloride in the flue gas can be removed efficiently in a synergistic manner.
The first aspect of the embodiment of this application provides a device of coal-fired flue gas sulfur trioxide of desorption and hydrogen chloride in coordination, includes: an absorbent solution preparation system and an absorbent solution injection system;
the absorbent solution preparation system is used for preparing an absorbent solution, and the absorbent solution comprises an absorbent;
the absorbent solution injection system is connected with the absorbent solution preparation system through a pipeline, and is used for receiving the absorbent solution conveyed by the absorbent solution preparation system and injecting the absorbent solution to the flue gas in the flue so that the absorbent in the absorbent solution reacts with the gas to be removed in the flue gas to generate a solid product and the gas to be removed is removed from the flue gas, wherein the gas to be removed comprises at least one of sulfur trioxide and hydrogen chloride.
The second aspect of the embodiment of the present application provides a method for cooperatively removing sulfur trioxide and hydrogen chloride from coal-fired flue gas, where the method is applied to a device for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas, and the method includes:
preparing an absorbent solution, the absorbent solution comprising an absorbent;
and receiving the absorbent solution, and spraying the absorbent solution to the flue gas in the flue so that the absorbent in the absorbent solution reacts with the gas to be removed in the flue gas to generate a solid product, so that the gas to be removed is removed from the flue gas, wherein the gas to be removed comprises at least one of sulfur trioxide and hydrogen chloride.
The device for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas in a coordinated mode in the embodiment of the application comprises an absorbent solution preparation system and an absorbent solution injection system, the absorbent solution preparation system is used for preparing absorbent solution, the absorbent solution injection system is connected with the absorbent solution preparation system through a pipeline, the absorbent solution injection system is used for receiving the absorbent solution conveyed by the absorbent solution preparation system and injecting the absorbent solution into flue gas in a flue, so that an absorbent in the absorbent solution reacts with gas to be removed in the flue gas to generate a solid product, the gas to be removed is removed from the flue gas, and the gas to be removed comprises at least one of sulfur trioxide and hydrogen chloride. Therefore, the synergistic removal of sulfur trioxide and hydrogen chloride in the flue gas can be realized, on one hand, the generation of Ammonium Bisulfate (ABS) can be reduced, the corrosion and scaling blockage risks of tail flue equipment and a heat exchange surface are reduced, the emission of sulfur trioxide to the atmosphere is reduced, and the standard emission of sulfur trioxide is realized; on the other hand, by removing hydrogen chloride in the flue gas, the amount of the desulfurization wastewater can be greatly reduced, the investment and the operation cost of zero emission of the desulfurization wastewater are greatly reduced, downstream equipment is protected from being corroded by sulfur trioxide and hydrogen chloride, the safe and stable operation of the equipment is kept, and the economic benefit of the generator set is improved.
Drawings
FIG. 1 is a schematic structural diagram of an apparatus for synergistically removing sulfur trioxide and hydrogen chloride from coal-fired flue gas in the embodiment of the application.
Detailed Description
The technical solutions of the present application will be described clearly and completely in conjunction with the embodiments of the present application, and it is obvious that the described embodiments are only a part of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
The application provides a device for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas in a synergic manner, a base absorbent solution is sprayed into flue gas in a flue between an outlet of a denitration reactor and an inlet of an air preheater, the absorbent solution is atomized to a proper particle size and then reacts with sulfur trioxide and hydrogen chloride gas in the flue gas to generate sulfate and chloride, and the sulfate and the chloride are solidified into fly ash, so that the synergistic removal of the sulfur trioxide and the hydrogen chloride in the flue gas is realized, on one hand, the generation of Ammonium Bisulfate (ABS) is reduced, the corrosion and scaling blockage risks of tail flue equipment and a heat exchange surface are reduced, the emission of sulfur trioxide to the atmosphere is reduced, and the emission of sulfur trioxide up to the standard is realized; on the other hand, by removing hydrogen chloride in the flue gas, the amount of the desulfurization wastewater can be greatly reduced, the zero-emission investment and the operation cost of the desulfurization wastewater are greatly reduced, downstream equipment is protected from being corroded by sulfur trioxide and hydrogen chloride, the stable and safe operation of the equipment is kept, and the economic benefit of the generator set is improved.
The technical solution of the embodiment of the present application will be described in further detail below with reference to the schematic structural diagram of the above-mentioned apparatus. As shown in fig. 1, the purification apparatus includes: absorbent solution preparation system, absorbent solution injection system.
Wherein the absorbent solution preparation system is used for preparing an absorbent solution, and the absorbent solution comprises an absorbent; the absorbent solution injection system is connected with the absorbent solution preparation system through a pipeline, and is used for receiving the absorbent solution conveyed by the absorbent solution preparation system and injecting the absorbent solution to the flue gas in the flue so that the absorbent in the absorbent solution reacts with the gas to be removed in the flue gas to generate a solid product and the gas to be removed is removed from the flue gas, wherein the gas to be removed comprises at least one of sulfur trioxide and hydrogen chloride.
In a preferred embodiment of this embodiment, the absorbent solution spraying system includes a compressed air tank 5, an absorbent solution delivery pump 9, an absorbent solution spraying device 3;
the inlet of the absorbent solution delivery pump 9 is connected with the absorbent solution preparation system through a pipeline, the outlet of the absorbent solution delivery pump 9 is connected with the absorbent solution injection device 3 through a pipeline, and the absorbent solution delivery pump 9 is used for delivering the absorbent solution prepared by the absorbent solution preparation system to the absorbent solution injection device 3;
the pipeline between the absorbent solution delivery pump 9 and the absorbent solution spraying device 3 is provided with a compressed air interface, the compressed air interface is connected with a compressed air tank 5, and the compressed air tank 5 is used for providing compressed air for the absorbent solution spraying device 3.
In a preferred embodiment of this embodiment, the absorbent solution spraying device 3 comprises a plurality of two-fluid atomizing spray guns for atomizing the absorbent solution with the compressed air supplied from the compressed air tank 5 and spraying the atomized absorbent solution to the flue gas in the flue.
In a preferred embodiment of the present embodiment, a plurality of two-fluid atomization spray guns are uniformly arranged in the flue between the outlet of the denitration reactor 1 and the inlet of the air preheater 2, and the two-fluid atomization spray guns are connected with the flue wall of the flue through flanges.
In a preferred embodiment of the present embodiment, the absorbent solution injection system further comprises a static mixer 4, and the static mixer 4 is disposed in the flue between the outlet of the denitration reactor 1 and the inlet of the air preheater 2 and is disposed downstream of the two-fluid atomization spray gun along the flow direction of the flue gas.
The static mixer is a high-efficiency mixing device without moving parts, and the basic working mechanism of the static mixer is to change the flowing state of fluid in a pipe by using a mixing unit body fixed in the pipe so as to achieve the purposes of good dispersion and full mixing of different fluids. Therefore, the incompletely reacted absorbent and the flue gas flow through the static mixer 4 to form a turbulent flow field, meanwhile, the retention time of the flue gas in the flue is prolonged, the contact probability of sulfur trioxide and hydrogen chloride with the absorbent is improved, the neutralization reaction of the sulfur trioxide and the hydrogen chloride with the absorbent is promoted, and the removal rate is improved.
In a preferred embodiment of this embodiment, the absorbent solution preparation system comprises an absorbent pneumatic feeding system 14, an absorbent dissolving tank 12, a dissolving tank stirrer 13;
an inlet of the absorbent dissolving tank 12 is connected with an outlet of the absorbent pneumatic feeding system 14 through a pipeline, the absorbent pneumatic feeding system 14 is used for conveying an absorbent to the absorbent dissolving tank 12, and the absorbent dissolving tank 12 is used for dissolving the received absorbent by using a solvent to prepare an absorbent solution;
the dissolving tank stirrer 13 is provided inside the tank body of the absorbent dissolving tank 12, and stirs the mixed liquid of the absorbent and the solvent to sufficiently dissolve the absorbent when dissolving the absorbent.
The solvent may be, specifically, a solvent such as demineralized water, industrial water, circulating water, or treated wastewater, and preferably is demineralized water. In order to accelerate the dissolving rate of the absorbent, a heating coil can be arranged in the tank body of the absorbent dissolving tank 12 and used for heating the mixed liquid of the absorbent and the solvent to improve the dissolving rate. Preferably, the heating coil can keep the temperature of the mixed solution at 20-40 ℃, and can further improve the dissolution rate.
In certain embodiments of the present application, the absorbent dissolution tank 12 may be self-made, typically field-made, and sized according to the installed capacity of the unit and the concentration of contaminants. In certain embodiments of the present application, the absorbent dissolving tank 12 is required to meet the consumption of absorbent solution for 1 day of the plant rated operating condition. The material of the absorbent dissolving tank 12 is preferably 304L stainless steel, and the heating coil and the dissolving tank stirrer 13 are preferably 316L stainless steel.
In a preferred embodiment, the feeding mode of the absorbent pneumatic feeding system 14 is pneumatic feeding, and the pneumatic feeding is to utilize the energy of air flow to convey granular materials in the direction of the air flow in a closed pipeline, which is a specific application of fluidization technology. The pneumatic feeding operation is convenient, the pneumatic feeding device can be used for horizontal, vertical or inclined conveying, and physical operations or certain chemical operations such as heating, cooling, drying, airflow classification and the like of materials can be simultaneously carried out in the conveying process.
And is a closed loop flow air duct system which specifically comprises a feed hopper 14-1, a Roots blower 14-2 and a separator 14-3. Absorbent particles enter a material conveying pipeline through a feed hopper 14-1, are powered by a Roots blower 14-2 and enter a separator 14-3, and separated materials enter an absorbent dissolving tank 12 to finish feeding; the separated conveying air enters an air return pipeline, and enters a material conveying pipeline after being accelerated by a Venturi to finish the task of conveying materials again, so that a closed loop is formed.
In a preferred embodiment of this embodiment, the absorbent solution preparation system further comprises a dissolving pump 11, an absorbent solution storage tank 10 and a solution circulating pump 8;
the dissolving pump 11 is arranged on a pipeline between an outlet of the absorbent dissolving tank 12 and an inlet of the absorbent solution storage tank 10, and is used for conveying the absorbent solution prepared by the absorbent dissolving tank 12 to the absorbent solution storage tank 10;
an inlet of the solution circulating pump 8 is connected with the bottom of the absorbent solution storage tank 10, an outlet of the solution circulating pump 8 is connected with the top of the absorbent solution storage tank 10, and the solution circulating pump 8 is used for conveying the absorbent solution from the bottom of the absorbent solution storage tank 10 to the top of the absorbent solution storage tank 10 so that the absorbent solution circularly flows in the tank body of the absorbent solution storage tank 10;
the inlet of the absorbent solution delivery pump 9 is connected to the outlet of the absorbent solution storage tank 10 through a pipe.
In addition, a heating coil can be arranged inside the tank body of the absorbent solution storage tank 10 for heat preservation of the absorbent solution. Preferably, the temperature of the absorbent solution can be maintained at 20-40 ℃. The absorbent solution storage tank 10 may be self-made, typically field-made, and the size may be calculated based on the installed capacity of the unit and the concentration of the contaminants. Preferably, the absorbent solution storage tank 10 can meet the absorbent solution consumption of 7 days of the rated working condition of the whole plant. The absorbent solution tank 10 is preferably made of 304L stainless steel, and the heating coil is preferably made of 316L stainless steel.
In a preferred embodiment of this embodiment, the purification device further comprises a spraying device cleaning system, wherein the spraying device cleaning system comprises a cleaning solution storage tank 7 and a cleaning pump 6;
the pipeline between the absorbent solution delivery pump 9 and the absorbent solution spraying device 3 is further provided with a cleaning solution interface, the cleaning pump 6 is arranged on the pipeline between the cleaning solution interface and the cleaning solution storage tank 7, and the cleaning pump 6 is used for delivering the cleaning solution in the cleaning solution storage tank 7 to the cleaning solution interface, so that the cleaning solution flows to the absorbent solution spraying device 3 under the action of the compressed air delivered by the compressed air tank 5 to clean the absorbent solution spraying device 3.
The cleaning liquid can be specifically an acidic solution, a composite cleaning liquid and other liquids capable of cleaning pipelines or devices, preferably an acidic solution, and the acidic solution can react with absorbent particles scaled on the two-fluid atomization spray gun to dissolve the scaled absorbent particles, so that the aim of cleaning the spray gun is fulfilled.
In some embodiments of the present application, the above-mentioned purification device may be disposed at a flue gas outlet of a denitration reactor in a general flue gas treatment system, and the denitration reactor is provided with a flue gas inlet and a flue gas outlet, for denitration of flue gas.
In some embodiments of the present application, the above-described purification apparatus further comprises an online flue gas analyzer for monitoring sulfur trioxide concentration and hydrogen chloride concentration of the coal-fired flue gas before and after the removal treatment. On-line flue gas analyzer can set up flue wall upper reaches and low reaches at absorbent solution injection apparatus 3 locates, specifically can set up in denitration reactor 1's exhanst gas outlet department and 2 entrances of air preheater for sulfur trioxide concentration and hydrogen chloride concentration in monitoring denitration reactor 1 exhanst gas outlet exhaust flue gas and the desorption back flue gas.
Because the desulfurization methods such as a dry absorbent injection method (DSI), a wet absorbent injection method (WSI) and the like and the dechlorination methods such as the fixation of gaseous chlorides by adding a calcium-based absorbent have a plurality of problems, for example, the removal of single components is only considered, the multi-component synergistic removal is not considered, the capital investment is large, the particle size of the injected dry powder is large, the removal efficiency is low, the consumption of the absorbent is large and the like, so that compared with the desulfurization method or the dechlorination method, the purification device can synergistically remove sulfur trioxide and hydrogen chloride in the flue gas, realize the multi-component removal, greatly reduce the capital investment, realize the standard emission of sulfur trioxide, solve the problems of blockage of an air preheater, bag pasting on a bag on the bag, polar plates of an electric dust remover, dust sticking and the like caused by the generation of Ammonium Bisulfate (ABS), and greatly reduce the amount of desulfurization waste water, the investment and the operation cost of zero discharge of the desulfurization wastewater are greatly reduced, downstream equipment is protected from being corroded by sulfur trioxide and hydrogen chloride, the safe and stable operation of the equipment is maintained, and the economic benefit of a generator set is improved; on the other hand, the particle size of the absorbent particles is greatly reduced due to the atomization operation of the absorbent solution, the contact probability and the reaction efficiency of the absorbent particles with sulfur trioxide and hydrogen chloride are improved, the removal efficiency of the sulfur trioxide and the hydrogen chloride is improved, the consumption of the absorbent can be reduced, and the input cost of the absorbent is reduced.
The method for synergistically removing sulfur trioxide and hydrogen chloride from coal-fired flue gas, which is implemented by the above device in the embodiment of the present application, will be further described in detail in conjunction with the structure of the above purification device, and one embodiment of the method comprises:
the purification device is used for preparing absorbent solution, the absorbent solution comprises absorbent, the absorbent solution is received, the absorbent solution is sprayed to the flue gas in the flue, so that the absorbent in the absorbent solution and the gas to be removed in the flue gas react to generate solid products, the gas to be removed is removed from the flue gas, and the gas to be removed comprises at least one of sulfur trioxide and hydrogen chloride.
In a preferred embodiment of this embodiment, the spraying of the sorbent solution into the flue gas in the flue comprises:
controlling the absorbent solution and compressed air to atomize through a double-fluid atomization spray gun at a preset gas-liquid ratio and pressure and spraying the atomized absorbent solution to the flue gas in the flue;
the atomized absorbent solution is evaporated in the high-temperature flue gas to form absorbent particles, and the absorbent particles react with sulfur trioxide and hydrogen chloride gas in the flue gas to generate chloride and sulfate which are solidified into fly ash, so that the synergistic removal of the sulfur trioxide and the hydrogen chloride in the flue gas is realized.
In a preferred embodiment of this embodiment, the pressure of the compressed air is 0.2 to 0.5MPa, the pressure of the absorbent solution is 0.1 to 0.6MPa, and the gas-liquid ratio is (0.5 to 1): 1, the particle size of the absorbent particles is 10-30 mu m.
In a preferred embodiment of this example, an absorbent solution is prepared comprising:
conveying an absorbent to an absorbent dissolving tank, and dissolving the absorbent in the absorbent dissolving tank by using a solvent to prepare an absorbent solution;
when dissolving the absorbent, the mixture of the absorbent and the solvent is stirred to dissolve the absorbent sufficiently.
In a preferred implementation manner of this embodiment, the method further includes:
conveying the absorbent solution prepared in the absorbent dissolving tank to an absorbent solution storage tank;
the absorbent solution is transported from the bottom of the absorbent solution tank to the top of the absorbent solution tank so that the absorbent solution circulates inside the tank body of the absorbent solution tank.
In a preferred embodiment of this example, the absorbent consists of sodium carbonate, sodium hydroxide and calcium carbonate in a ratio of 1: (1-2): (0.001-0.1).
In a preferred implementation manner of this embodiment, the method further includes:
and conveying the cleaning liquid in the cleaning liquid storage tank to an absorbent solution spraying device for spraying an absorbent solution, and cleaning the absorbent solution spraying device.
In a preferred embodiment of this embodiment, the cleaning solution is an acid solution, the acid solution is one of a sulfuric acid solution and a hydrochloric acid solution, and the concentration of the acid solution is 5 to 10%.
For further explanation of the present application, the following detailed description will be given of the above-mentioned purification apparatus and purification method provided in the present application with reference to examples, but they should not be construed as limiting the scope of the present application.
Example 1
Denitration reactionThe temperature of the flue gas at the outlet of the reactor is 300 ℃, and the concentration of sulfur trioxide in the flue gas is 48mg/Nm3The concentration of hydrogen chloride was 36.5mg/Nm3。
The device for removing sulfur trioxide and hydrogen chloride by using the coal-fired flue gas as shown in figure 1 comprises:
a denitration reactor 1; the denitration reactor is provided with a flue gas inlet and a flue gas outlet;
a flue gas inlet is connected with the flue gas outlet of the denitration reactor, and the flue gas outlet is connected with the static mixer 4;
and an absorbent solution injection device 3 is arranged on the flue wall between the flue gas outlet of the denitration reactor and the flue gas inlet of the static mixer. The absorbent solution injection device 3 can be a two-fluid atomization spray gun which is fixed on the flue wall between the flue gas outlet of the denitration reactor and the flue gas inlet of the static mixer through a flange; the two-fluid atomization spray guns are uniformly distributed on the flue wall between the flue gas outlet of the denitration reactor and the flue gas inlet of the static mixer;
the pneumatic absorbent feeding system 14 is used for conveying the absorbent to the absorbent dissolving tank, the feeding mode of the pneumatic absorbent feeding system 14 is pneumatic feeding, and the pneumatic absorbent feeding system is a closed-loop flowing air pipe system and comprises a feed hopper 14-1, a Roots blower 14-2 and a separator 14-3. Absorbent particles enter a material conveying pipeline through a feed hopper 14-1, are powered by a Roots blower 14-2 and enter a separator 14-3, and separated materials enter an absorbent dissolving tank to finish feeding; the separated conveying air enters an air return pipeline, enters a material conveying pipeline after being accelerated by a Venturi to finish the task of conveying materials again, and a closed loop is formed;
the absorbent dissolving tank 12 is provided with a material inlet, an absorption liquid outlet and a demineralized water inlet, wherein the demineralized water inlet is used for inputting demineralized water, and an absorbent is prepared into an absorbent solution; a dissolving tank stirrer 13 is further arranged in the absorbent dissolving tank, a heating coil is arranged at the bottom of the absorbent dissolving tank 12, and the temperature of the absorption liquid in the absorbent dissolving tank is kept at 20-40 ℃ through heating;
a dissolving pump 11 for delivering the absorption liquid in the absorbent dissolving tank to the absorption liquid storage tank 10;
the absorption liquid storage tank 10 is used for storing absorbent solution and is provided with an absorption liquid inlet and an absorption liquid outlet, the absorption liquid inlet of the absorption liquid storage tank is connected with the absorption liquid outlet of the absorbent dissolving tank, and the absorption liquid outlet of the absorption liquid storage tank is connected with the absorption liquid inlet of the two-fluid atomization spray gun; a heating coil is arranged at the bottom of the absorption liquid storage tank, and the temperature of the absorption liquid in the absorption liquid storage tank is kept at 20-40 ℃ through heating;
the solution circulating pump 8 is used for conveying the solution at the bottom of the absorption liquid storage tank to the top of the absorption liquid storage tank so as to uniformly mix the absorption liquid;
the absorbent solution delivery pump 9 is used for delivering the absorption liquid in the absorption liquid storage tank to the two-fluid atomization spray gun;
the compressed air tank 5 is provided with a compressed air interface on a pipeline between the absorbent solution spraying device 3 and the absorbent solution delivery pump 9, and the compressed air interface is connected with the compressed air tank 5;
a cleaning liquid storage tank 7 and a cleaning pump 6, wherein a cleaning liquid interface is arranged on a pipeline between the absorbent solution spraying device 3 and the compressed air interface, and the cleaning liquid interface is connected with the cleaning liquid storage tank 7; the cleaning liquid storage tank 7 conveys the cleaning liquid to the two-fluid atomization spray gun through the cleaning pump 6;
and the air preheater 2 is connected with the smoke outlet of the static mixer.
The method for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas comprises the following steps:
reacting the denitrated flue gas with absorption liquid atomized and sprayed by a two-fluid atomization spray gun, and then feeding the reaction product into a static mixer;
the absorbent in the absorption liquid comprises sodium carbonate, sodium hydroxide and calcium carbonate, and the mass ratio of the sodium carbonate to the sodium hydroxide is 1: 1: 0.01, the mass concentration of the absorption liquid is 15 percent; the particle size of the atomized absorption liquid is 10-30 microns;
when the absorbent solution spraying device 3 sprays the absorption liquid in an atomizing manner, the pressure of compressed air is 0.2MPa, and the pressure of the absorption liquid is 0.4 MPa;
the gas-liquid ratio in the absorbent solution spraying device 3 was 0.5: 1;
the injection amount of the absorption liquid is 233mg/Nm3；
The absorbent reacts with sulfur trioxide and hydrogen chloride gas in the flue gas to generate chloride and sulfate which are solidified into fly ash. Then, the incompletely reacted absorbent and the flue gas flow through a static mixer to form a turbulent flow field, meanwhile, the retention time of the flue gas in a flue is prolonged, the contact probability of sulfur trioxide and hydrogen chloride with the absorbent is improved, the neutralization reaction of the sulfur trioxide and the hydrogen chloride with the absorbent is promoted, and the removal rate is improved;
the flue gas is purified flue gas after passing through the static mixer, and directly enters the air preheater.
Detection shows that the concentration of the hydrogen chloride in the purified flue gas is less than 7.3mg/Nm3The removal efficiency reaches 80 percent; the concentration of sulfur trioxide is less than 12mg/Nm3And the desulfurization efficiency reaches 75 percent.
When the absorbent solution injection device 3 (a two-fluid atomization spray gun) is in fouling, the spray gun is taken out from a flue, and sulfuric acid or hydrochloric acid with the mass concentration of 5% -10% is conveyed to the spray gun for cleaning through an acid solution pump and a compressed air tank.
Example 2
The temperature of the flue gas at the outlet of the denitration reactor is 300 ℃, and the sulfur trioxide content in the flue gas is 60mg/Nm3The concentration of hydrogen chloride is 50mg/Nm3。
A device for removing sulfur trioxide and hydrogen chloride by using the same coal-fired flue gas as in example 1;
the method for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas comprises the following steps:
reacting the denitrated flue gas with absorption liquid atomized and sprayed by a two-fluid atomization spray gun, and then feeding the reaction product into a static mixer;
the absorbent in the absorption liquid comprises sodium carbonate, sodium hydroxide and calcium carbonate, and the mass ratio of the sodium carbonate to the sodium hydroxide is 1: 1.5: 0.05, the mass concentration of the absorption liquid is 20 percent; the particle size of the atomized absorption liquid is 10-30 microns;
when the absorbent solution spraying device 3 sprays the absorption liquid in an atomizing manner, the pressure of compressed air is 0.4MPa, and the pressure of the absorption liquid is 0.5 MPa;
the gas-liquid ratio in the absorbent solution injection device 3 was 1: 1;
the injection amount of the absorption liquid is 434mg/Nm3；
The absorbent reacts with sulfur trioxide and hydrogen chloride gas in the flue gas to generate chloride and sulfate which are solidified into fly ash. Then, the incompletely reacted absorbent and the flue gas flow through a static mixer to form a turbulent flow field, meanwhile, the retention time of the flue gas in a flue is prolonged, the contact probability of sulfur trioxide and hydrogen chloride with the absorbent is improved, the neutralization reaction of the sulfur trioxide and the hydrogen chloride with the absorbent is promoted, and the removal rate is improved;
the flue gas is purified flue gas after passing through the static mixer, and directly enters the air preheater.
Through detection, the concentration of the hydrogen chloride in the purified flue gas is less than 9mg/Nm3The removal efficiency reaches 85 percent; the concentration of sulfur trioxide is less than 10mg/Nm3And the desulfurization efficiency reaches 80 percent.
When the absorbent solution injection device 3 (a two-fluid atomization spray gun) is in fouling, the spray gun is taken out from a flue, and sulfuric acid or hydrochloric acid with the mass concentration of 5% -10% is conveyed to the spray gun for cleaning through an acid solution pump and a compressed air tank.
Example 3
The temperature of the flue gas at the outlet of the denitration reactor is 360 ℃, and the concentration of sulfur trioxide in the flue gas is 80mg/Nm3The concentration of hydrogen chloride is 60mg/Nm3。
A device for removing sulfur trioxide and hydrogen chloride by using the same coal-fired flue gas as in example 1;
the method for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas comprises the following steps:
reacting the denitrated flue gas with absorption liquid atomized and sprayed by a two-fluid atomization spray gun, and then feeding the reaction product into a static mixer;
the absorbent in the absorption liquid comprises sodium carbonate, sodium hydroxide and calcium carbonate, and the mass ratio of the sodium carbonate to the sodium hydroxide is 1: 2: 0.1, the mass concentration of the absorption liquid is 20 percent; the particle size of the atomized absorption liquid is 10-30 microns;
when the absorbent solution spraying device 3 sprays the absorption liquid in an atomizing manner, the pressure of compressed air is 0.5MPa, and the pressure of the absorption liquid is 0.5 MPa;
the gas-liquid ratio in the absorbent solution injection device 3 was 1: 1;
the injection amount of the absorption liquid is 589mg/Nm3；
The absorbent reacts with sulfur trioxide and hydrogen chloride gas in the flue gas to generate chloride and sulfate which are solidified into fly ash. Then, the incompletely reacted absorbent and the flue gas flow through a static mixer to form a turbulent flow field, meanwhile, the retention time of the flue gas in a flue is prolonged, the contact probability of sulfur trioxide and hydrogen chloride with the absorbent is improved, the neutralization reaction of the sulfur trioxide and the hydrogen chloride with the absorbent is promoted, and the removal rate is improved;
the flue gas is purified flue gas after passing through the static mixer, and directly enters the air preheater.
Through detection, the concentration of the hydrogen chloride in the purified flue gas is less than 6mg/Nm3The removal efficiency reaches 90 percent; the concentration of sulfur trioxide is less than 12mg/Nm3And the desulfurization efficiency reaches 85 percent. When the absorbent solution injection device 3 (a two-fluid atomization spray gun) is in fouling, the spray gun is taken out from a flue, and sulfuric acid or hydrochloric acid with the mass concentration of 5% -10% is conveyed to the spray gun for cleaning through an acid solution pump and a compressed air tank.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (16)
1. A device for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas in a synergic manner comprises: an absorbent solution preparation system and an absorbent solution injection system;
the absorbent solution preparation system is used for preparing an absorbent solution, and the absorbent solution comprises an absorbent;
the absorbent solution injection system is connected with the absorbent solution preparation system through a pipeline, and is used for receiving the absorbent solution conveyed by the absorbent solution preparation system and injecting the absorbent solution to the flue gas in the flue so that the absorbent in the absorbent solution reacts with the gas to be removed in the flue gas to generate a solid product and the gas to be removed is removed from the flue gas, wherein the gas to be removed comprises at least one of sulfur trioxide and hydrogen chloride.
2. The apparatus of claim 1, wherein the absorbent solution spraying system comprises a compressed air tank, an absorbent solution delivery pump, an absorbent solution spraying device;
the inlet of the absorbent solution delivery pump is connected with the absorbent solution preparation system through a pipeline, the outlet of the absorbent solution delivery pump is connected with the absorbent solution injection device through a pipeline, and the absorbent solution delivery pump is used for delivering the absorbent solution prepared by the absorbent solution preparation system to the absorbent solution injection device;
and a compressed air interface is arranged on a pipeline between the absorbent solution delivery pump and the absorbent solution spraying device, the compressed air interface is connected with the compressed air tank, and the compressed air tank is used for providing compressed air for the absorbent solution spraying device.
3. The apparatus of claim 2 wherein the sorbent solution injection means comprises a plurality of two-fluid atomizing spray guns for atomizing the sorbent solution with compressed air delivered by the compressed air tank and spraying the atomized sorbent solution onto the flue gas in the flue.
4. The apparatus of claim 3, wherein the plurality of two-fluid atomizing spray guns are uniformly arranged in the flue between the outlet of the denitrification reactor and the inlet of the air preheater, and the two-fluid atomizing spray guns are connected with the flue wall of the flue through flanges.
5. The apparatus of claim 4, wherein the sorbent solution injection system further comprises a static mixer disposed in the flue between the denitration reactor outlet and the air preheater inlet and downstream of the plurality of two-fluid atomizing lances in a direction of flue gas flow.
6. The apparatus of claim 2, wherein the absorbent solution preparation system comprises an absorbent pneumatic feeding system, an absorbent dissolving tank, a dissolving tank agitator;
an inlet of the absorbent dissolving tank is connected with an outlet of the absorbent pneumatic feeding system through a pipeline, the absorbent pneumatic feeding system is used for conveying the absorbent to the absorbent dissolving tank, and the absorbent dissolving tank is used for dissolving the received absorbent by using a solvent to prepare the absorbent solution;
the dissolving tank stirrer is arranged in the tank body of the absorbent dissolving tank and is used for stirring the mixed liquid of the absorbent and the solvent when the absorbent is dissolved so as to fully dissolve the absorbent.
7. The apparatus of claim 6, wherein the absorbent solution preparation system further comprises a dissolution pump, an absorbent solution storage tank, and a solution circulation pump;
the dissolving pump is arranged on a pipeline between an outlet of the absorbent dissolving tank and an inlet of the absorbent solution storage tank and is used for conveying the absorbent solution prepared by the absorbent dissolving tank to the absorbent solution storage tank;
the inlet of the solution circulating pump is connected with the bottom of the absorbent solution storage tank, the outlet of the solution circulating pump is connected with the top of the absorbent solution storage tank, and the solution circulating pump is used for conveying the absorbent solution from the bottom of the absorbent solution storage tank to the top of the absorbent solution storage tank so that the absorbent solution circularly flows inside the tank body of the absorbent solution storage tank;
and the inlet of the absorbent solution delivery pump is connected with the outlet of the absorbent solution storage tank through a pipeline.
8. The apparatus of any one of claims 2 to 7, wherein the purification apparatus further comprises a spray apparatus cleaning system comprising a cleaning solution storage tank and a cleaning pump;
and a cleaning liquid interface is further arranged on a pipeline between the absorbent solution delivery pump and the absorbent solution spraying device, the cleaning pump is arranged on a pipeline between the cleaning liquid interface and the cleaning liquid storage tank, and the cleaning pump is used for delivering the cleaning liquid in the cleaning liquid storage tank to the cleaning liquid interface, so that the cleaning liquid flows to the absorbent solution spraying device under the action of compressed air delivered by the compressed air tank to clean the absorbent solution spraying device.
9. A method for cooperatively removing sulfur trioxide and hydrogen chloride from coal-fired flue gas is characterized in that the method is applied to a device for removing sulfur trioxide and hydrogen chloride from coal-fired flue gas, and comprises the following steps:
preparing an absorbent solution, the absorbent solution comprising an absorbent;
and receiving the absorbent solution, and spraying the absorbent solution to the flue gas in the flue so that the absorbent in the absorbent solution reacts with the gas to be removed in the flue gas to generate a solid product, so that the gas to be removed is removed from the flue gas, wherein the gas to be removed comprises at least one of sulfur trioxide and hydrogen chloride.
10. The method of claim 9, wherein the injecting the sorbent solution into the flue gas in the flue includes:
controlling the absorbent solution and compressed air to atomize through a double-fluid atomization spray gun at a preset gas-liquid ratio and pressure and spraying the atomized absorbent solution to the flue gas in the flue;
the atomized absorbent solution is evaporated in the high-temperature flue gas to form absorbent particles, and the absorbent particles react with sulfur trioxide and hydrogen chloride gas in the flue gas to generate chloride and sulfate which are solidified into fly ash, so that the synergistic removal of the sulfur trioxide and the hydrogen chloride in the flue gas is realized.
11. The method according to claim 10, wherein the pressure of the compressed air is 0.2-0.5 MPa, the pressure of the absorbent solution is 0.1-0.6 MPa, and the gas-liquid ratio is (0.5-1): 1, the particle size of the absorbent particles is 10-30 μm.
12. The method of claim 9, wherein the preparing an absorbent solution comprises:
conveying the absorbent to the absorbent dissolving tank, and dissolving the absorbent in the absorbent dissolving tank by using a solvent to prepare the absorbent solution;
the mixed solution of the absorbent and the solvent is stirred to sufficiently dissolve the absorbent when dissolving the absorbent.
13. The method of claim 12, further comprising:
conveying the absorbent solution prepared in the absorbent dissolving tank to an absorbent solution storage tank;
conveying the absorbent solution from the bottom of the absorbent solution storage tank to the top of the absorbent solution storage tank to circulate the absorbent solution inside the tank body of the absorbent solution storage tank.
14. The method according to claim 12, characterized in that the absorbent consists of sodium carbonate, sodium hydroxide and calcium carbonate, the ratio of sodium carbonate, sodium hydroxide and calcium carbonate being 1: (1-2): (0.001-0.1).
15. The method according to any one of claims 9 to 14, further comprising:
and conveying the cleaning liquid in the cleaning liquid storage tank to an absorbent solution spraying device for spraying the absorbent solution, and cleaning the absorbent solution spraying device.
16. The method according to claim 15, wherein the cleaning solution is an acid solution, the acid solution is one of a sulfuric acid solution and a hydrochloric acid solution, and the concentration of the acid solution is 5-10%.
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| CN114292673A (en) * | 2021-12-29 | 2022-04-08 | 北京北科环境工程有限公司 | Blast furnace gas wet pervaporation dechlorination method and dechlorination device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114292673A (en) * | 2021-12-29 | 2022-04-08 | 北京北科环境工程有限公司 | Blast furnace gas wet pervaporation dechlorination method and dechlorination device |
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