CN115253633A - Waste incineration flue gas purification method and system - Google Patents
Waste incineration flue gas purification method and system Download PDFInfo
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Abstract
The invention discloses a method and a system for purifying waste incineration flue gas. The flue gas purification method comprises the following steps: carrying out dry deacidification treatment on the waste incineration flue gas; carrying out SCR denitration treatment on the waste incineration flue gas, wherein a catalyst adopted in the SCR denitration treatment comprises a low-temperature catalyst; and performing wet deacidification treatment on the waste incineration flue gas. The flue gas purification system comprises a dry-method deacidification tower (1), an SCR denitration dust removal device (2), a wet-method deacidification tower (4), an induced draft fan (5) and a chimney (6); the smoke inlet of the SCR denitration dust removal device is communicated with the smoke outlet of the dry-method deacidification tower, and the catalyst adopted by the SCR denitration dust removal device comprises a low-temperature catalyst; the smoke inlet of the wet deacidification tower is communicated with the smoke outlet of the SCR denitration dust removal device, and the smoke outlet of the wet deacidification tower is communicated with a chimney. The flue gas purification method and the flue gas purification system do not need to heat the waste incineration flue gas, and the process flow of flue gas purification is simple.
Description
Technical Field
The invention relates to a flue gas purification technology, in particular to a waste incineration flue gas purification method and system.
Background
At present, the mainstream waste incineration flue gas purification treatment process route in China is SNCR denitration treatment → semidry deacidification treatment → dry deacidification treatment → activated carbon adsorption treatment → dust removal → GGH heat exchange → SGH heating → SCR denitration treatment. However, the current process route for purifying and treating the waste incineration flue gas is too complex, and the current SCR denitration treatment still has high requirement on the temperature of the waste incineration flue gas, and the waste incineration flue gas is required to reach the temperature requirement of 300-350 ℃, but the flue gas temperature after the semi-dry deacidification treatment is not high and is usually only about 145 ℃, so that the requirement on the flue gas temperature by the SCR denitration treatment cannot be met, and therefore the waste incineration flue gas has to be heated (GGH heat exchange and SGH heating) before the SCR denitration treatment, which causes the heat energy consumption of the whole process treatment flow to be large, and is not beneficial to reducing the production cost.
The following are retrieved patent documents relevant in the art:
chinese patent No. CN202022060057.4 discloses a hazardous waste incineration flue gas purification system based on a catalytic ceramic fiber filter tube. Chinese patent No. CN202022057185.3 discloses a waste incineration flue gas purification system based on a ceramic filter element and renewable activated carbon. The reaction temperature of the ceramic fiber filter tube integrated device adopted in the above patents is in a range of about 300-350 ℃, a temperature window in the range is not suitable for activated carbon to adsorb heavy metal and dioxin, and the activated carbon is in a desorption state at about 300-350 ℃ and cannot adsorb, so that an adsorption device is required to be independently arranged for removing the heavy metal and the dioxin, and the process flow and equipment cost for flue gas treatment are increased.
In addition, some other background or concepts related to the present invention are further described below:
the term "SNCR denitration treatment" as used herein refers to a denitration treatment process in the prior art, and SNCR is a term in the art and is an abbreviation of selective non-catalytic reduction, which is a term in the art, and refers to a process of spraying a reducing agent at a temperature range of 800-1000 ℃ suitable for denitration reaction without the action of a catalyst to reduce nitrogen oxides in flue gas into harmless nitrogen and water.
As referred to herein, "semi-dry deacidification" is a prior art deacidification process, and specifically, quicklime is prepared as a lime slurry solution (calcium hydroxide (Ca (OH)) by a lime slurry preparation system2) Solution) and then pressurized to an atomizer rotating at high speed through a lime slurry pump to uniformly inject the rotationally atomized solution into the spray reaction tower to react with the flue gas flowing in the tower so as to remove acid gas.
The dry deacidification treatment is a deacidification treatment process in the prior art, and specifically, solid deacidification powder is mixed and contacted with flue gas in a spraying mode, the deacidification powder usually adopts alkaline substance powder, dispersed particles of the alkaline deacidification powder are contacted with acid gas in the flue gas to generate chemical neutralization reaction to generate neutral salt particles, and then salt particles generated by the reaction are captured together with flue gas dust and unreacted deacidification powder by using a dust removal device, so that the aim of removing the acid gas in the flue gas is fulfilled.
The "GGH heat exchange" referred to herein is a heat exchange process in the prior art, and GGH is an abbreviation of "Gas Heater" in english, and the middle translation is "flue Gas-flue Gas heat exchanger", specifically, two flowing media having temperature difference are subjected to heat exchange by using the GGH heat exchanger in the prior art, so that a medium having a lower temperature is heated and the temperature is increased, and a medium having a higher temperature is cooled and the temperature is decreased. The GGH heat exchanger is a device in the prior art, and the GGH heat exchanger heats desulfurized clean flue gas by using original flue gas, so that the temperature of the flue gas reaches above a dew point, the corrosion to an inlet flue and a chimney is reduced, and the diffusion degree of pollutants is improved.
The SGH heating is an abbreviation of "Steam-Gas-Heater" in english, and the middle translation is "Steam-flue Gas heat exchanger", specifically, the SGH heat exchanger in the prior art is used for exchanging heat between Steam and flue Gas, so that the flue Gas with lower temperature is heated and the temperature is increased. The SGH heat exchanger is a device in the prior art, and heats the desulfurized clean flue gas by using steam, so that the temperature of the flue gas is raised to 300-350 ℃, the temperature range of the conventional SCR denitration reaction is met, and the denitration efficiency is improved.
As used herein, the term "SCR denitration treatment" is a treatment process of the prior art, and SCR is a term of art in the art and is an abbreviation of "Selective Catalytic Reduction" in the English language, and the translation thereof is "Selective Catalytic Reduction method", and the basic principle thereof is to use ammonia molecules (NH) in ammonia water3) As a denitration reducing agent and nitrogen oxides (NO and NO) in flue gas2) Reacting to generate harmless nitrogen (N)2). Specifically, ammonia (NH) which is a reducing agent is denitrated under the action of a catalyst3) Selectively adding Nitric Oxide (NO) and nitrogen dioxide (NO) at a temperature of 200-400 deg.C2) Reduction to nitrogen (N)2) While almost no ammonia (NH) gas is generated3) With oxygen (O)2) Thereby increasing the nitrogen contentSelectivity, reduced denitration reductant ammonia (NH)3) The consumption of (c). The catalyst used in the conventional SCR denitration treatment is generally a vanadium-titanium (V-Ti) -based or vanadium-tungsten-titanium (V-W-Ti) -based catalyst.
Disclosure of Invention
The invention aims to provide a waste incineration flue gas purification method and system, which do not need to perform additional heating treatment on waste incineration flue gas, thereby avoiding waste of heat energy consumption, and reducing investment of process equipment due to simple process flow of flue gas purification.
In order to achieve the technical purpose, the invention adopts the following technical scheme:
a waste incineration flue gas purification method comprises the following steps:
s1, performing dry deacidification treatment on waste incineration flue gas;
s2, carrying out SCR denitration treatment on the waste incineration flue gas, wherein a catalyst adopted in the SCR denitration treatment comprises a low-temperature catalyst;
s3, performing wet deacidification treatment on the waste incineration flue gas;
and S4, discharging the waste incineration flue gas into the atmosphere.
Further, the low-temperature catalyst is a manganese-based catalyst and/or a copper-based catalyst.
Further, cerium and/or zirconium are added to the low-temperature catalyst.
Further, the S2 further includes: and in the SCR denitration treatment process, spraying activated carbon powder into the waste incineration flue gas.
Further, the S3 further includes: in the wet deacidification treatment process, the heat exchanger is adopted to carry out heat exchange on the waste incineration flue gas before the wet deacidification treatment and the waste incineration flue gas after the wet deacidification treatment.
A waste incineration flue gas purification system comprises a dry-method deacidification tower, an SCR denitration dust removal device, a wet-method deacidification tower, an induced draft fan and a chimney; the smoke inlet of the dry deacidification tower is communicated with the smoke outlet of the garbage incinerator; the smoke inlet of the SCR denitration dust removal device is communicated with the smoke outlet of the dry-method deacidification tower, and the catalyst adopted by the SCR denitration dust removal device comprises a low-temperature catalyst; the smoke inlet of the wet-process deacidification tower is communicated with the smoke outlet of the SCR denitration dust removal device, the smoke outlet of the wet-process deacidification tower is communicated with the smoke inlet of a chimney, and the induced draft fan is arranged at the smoke inlet of the chimney.
Further, the low-temperature catalyst is a manganese-based catalyst and/or a copper-based catalyst.
Further, cerium and/or zirconium are added to the low-temperature catalyst.
Furthermore, an activated carbon powder agent supply device is arranged on a pipeline communicated with a smoke inlet of the SCR denitration dust removal device.
Further, the flue gas purification system also comprises a flowing medium heat exchanger; the smoke inlet of the wet deacidification tower is communicated with the smoke outlet of the SCR denitration dust removal device, and the smoke inlet of the wet deacidification tower is communicated with the smoke outlet of the SCR denitration dust removal device through a heat release medium pipeline of the flowing medium heat exchanger; the smoke outlet of the wet deacidification tower is communicated with the smoke inlet of the chimney, and the smoke outlet of the wet deacidification tower is communicated with the smoke inlet of the chimney through a heated medium pipeline of the flowing medium heat exchanger.
In the method and the system for purifying the waste incineration flue gas, a manganese-based and/or copper-based low-temperature catalyst is adopted during SCR denitration treatment, so that the temperature of the waste incineration flue gas required by the SCR denitration treatment is controlled within the temperature range of 150-250 ℃, and then the whole process route of the flue gas purification is set to be dry deacidification treatment → SCR denitration treatment → wet deacidification treatment, wherein the temperature of the waste incineration flue gas before the dry deacidification treatment is about 180-230 ℃, and the temperature of the waste incineration flue gas after the dry deacidification treatment is maintained about 180-230 ℃, so that the temperature is just suitable for the SCR denitration treatment, the subsequent wet deacidification treatment has no special requirements on the temperature of the waste incineration flue gas, the whole process flow of the flue gas purification is carried out in the process of descending the gradient of the flue gas temperature, and the complicated process steps such as heating treatment on the waste incineration flue gas are not needed in the implementation process flow of the whole process flow of the flue gas purification. In addition, the temperature of the waste incineration flue gas at about 180-230 ℃ after the dry method deacidification treatment is also very suitable for the activated carbon to adsorb heavy metal and dioxin, and the process of adsorbing the heavy metal and the dioxin by using the activated carbon can be implemented while the SCR denitration treatment is carried out.
Compared with the prior art, the waste incineration flue gas purification method and the waste incineration flue gas purification system have the advantages that: on one hand, the waste incineration flue gas does not need to be additionally heated, so that the waste of heat energy consumption is avoided, the energy is saved, and the production cost is reduced; on the other hand, the whole process flow of the flue gas purification only comprises three process treatment processes of dry deacidification treatment, SCR denitration treatment and wet deacidification treatment, and the process of adsorbing heavy metals and dioxin by using the activated carbon is simultaneously carried out in the process of SCR denitration treatment, so that the whole process flow of the flue gas purification is simplified, and the investment of process equipment is reduced.
Drawings
FIG. 1 is a flow chart of the waste incineration flue gas purification method of the present invention;
FIG. 2 is a schematic diagram of the composition of the waste incineration flue gas purification system of the present invention.
In the figure: the system comprises a 1-dry deacidification tower, a 11-dry powder supply device, a 12-ammonia water supply device, a 13-activated carbon powder agent supply device, a 2-SCR denitration dust removal device, a 21-fly ash storage bin, a 3-flowing medium heat exchanger, a 4-wet deacidification tower, a 41-deacidification agent supply device, a 5-induced draft fan and a 6-chimney.
Detailed Description
The invention is further described with reference to the following figures and specific examples:
the embodiment provides a waste incineration flue gas purification method, which purifies flue gas generated by incinerating waste in a waste incinerator, makes the flue gas harmless and then discharges the flue gas into the atmosphere, thereby achieving the purpose of protecting the atmospheric environment. The smoke generated by burning the garbage in the garbage incinerator is called as garbage burning smoke.
The waste incinerator according to the present embodiment has a waste heat recovery device, and the temperature of the waste incineration flue gas at the time of final discharge after the waste incineration flue gas is subjected to waste heat recovery processing by the waste heat recovery device is about 180 to 230 ℃.
Referring to fig. 1, the flue gas purification method of the present embodiment includes the following steps S1 to S4.
S1, performing dry deacidification treatment on the waste incineration flue gas, and maintaining the temperature of the treated waste incineration flue gas at about 180-230 ℃.
The dry deacidification treatment is a conventional deacidification process, and the adopted solid deacidification powder is also called dry powder in the field, and the most common deacidification powder in actual production is sodium bicarbonate (NaHCO)3) Powder, slaked lime (Ca (OH)2) And (4) powder preparation.
Because the dry deacidification treatment has little influence on the temperature of the flue gas, the temperature of the waste incineration flue gas can still be maintained at about 180-230 ℃ after the dry deacidification treatment.
S2, carrying out SCR denitration treatment on the waste incineration flue gas subjected to dry deacidification treatment.
In the flue gas purification method of the embodiment, in the process of performing SCR denitration treatment, besides the traditional vanadium-titanium (V-Ti) -based and vanadium-tungsten-titanium (V-W-Ti) -based catalysts, a manganese (Mn) -based and/or copper (Cu) -based low-temperature catalyst is also used, and a small amount of cerium (Ce), zirconium (Zr) and other elements are added to the catalyst, so that the dispersibility of Mn and Cu active components in the catalyst is enhanced, and the low-temperature denitration activity of the catalyst is significantly improved.
The manganese-based low-temperature catalyst comprises MnO2、Mn2O3、Mn3O4MnO and the like, wherein MnO is mainly used2And Mn2O3Mainly comprises the following steps. MnO2Activity per unit area, mn2O3The NOx removal efficiency can reach 90% at the temperature of 180 ℃.
The copper-based low-temperature catalyst comprises CuO and Cu2O, etc., and the NOx removing efficiency can reach 80 percent in the temperature range of 180-230 ℃.
In the embodiment, the SCR denitration treatment uses a low-temperature catalyst, so that a good denitration reaction can be realized as long as the waste incineration flue gas is kept in a temperature range of 150 to 250 ℃, and usually 80% denitration efficiency can be realized, and the temperature of the waste incineration flue gas after the dry-method deacidification treatment is about 180 to 230 ℃, which is just in the temperature range of 150 to 250 ℃, so that the waste incineration flue gas does not need to be additionally heated or cooled.
In addition, the activated carbon is favorable for adsorbing heavy metal and dioxin at the temperature of 150-250 ℃, so that activated carbon powder is sprayed into the waste incineration flue gas in the SCR denitration treatment process of the waste incineration flue gas to adsorb the heavy metal and dioxin in the waste incineration flue gas. Therefore, a special device for adsorbing heavy metal and dioxin by the activated carbon is not needed. Meanwhile, the vanadium-titanium-based and vanadium-tungsten-titanium-based catalysts can promote the reaction of dioxin and oxygen, and the dioxin is easily decomposed into CO2、H25363 and discharging nontoxic substances such as O, HCl, and decomposing dioxin to a certain extent, thereby really realizing that the denitration treatment and the dioxin removal are carried out together.
And S3, performing wet deacidification treatment on the waste incineration flue gas to further remove residual acid gas in the waste incineration flue gas and further remove dust particles in the waste incineration flue gas. The deacidification agent adopted in the wet deacidification treatment is alkaline sodium hydroxide (NaOH) solution.
In the process, the heat exchanger is adopted to carry out heat exchange between the waste incineration flue gas before wet deacidification and the waste incineration flue gas after wet deacidification, so that the temperature of the waste incineration flue gas before wet deacidification is reduced, and the temperature of the waste incineration flue gas after wet deacidification is increased to 100-150 ℃, thereby preventing white smoke emission during subsequent flue gas emission. The "white smoke emission condition" refers to a phenomenon that water vapor in smoke discharged from a chimney cannot be rapidly absorbed by the atmosphere to generate water vapor condensation, so that the white smoke is visually polluted.
The heat exchanger referred to herein is a flowing medium heat exchanger, which is a device in the prior art, and specifically, the heat exchanger has two medium flowing pipelines, and the mediums flowing in the two pipelines can transfer heat to each other across the pipe wall, so that the medium with a lower temperature is heated and the temperature thereof is increased, and the medium with a higher temperature is cooled and the temperature thereof is decreased. In the present embodiment, the heat exchanger used is a heat exchanger called "GGH heat exchanger", which is also an existing heat exchanger, wherein GGH is an abbreviation of "Gas Heater" in english, and the translation is "flue Gas-flue Gas heat exchanger".
And S4, finally, discharging the waste incineration flue gas subjected to purification treatment into the atmosphere.
The steps S1 to S4 included in the flue gas purification method of the present embodiment are ended up to this point.
In the flue gas purification method of the present embodiment, a manganese (Mn) based and/or copper (Cu) based low-temperature catalyst is used during the SCR denitration treatment, so that the temperature of the waste incineration flue gas required for the SCR denitration treatment is controlled within a temperature range of 150 to 250 ℃, and then the whole process route of the flue gas purification is set to "dry deacidification treatment → SCR denitration treatment → wet deacidification treatment", the temperature of the waste incineration flue gas before the dry deacidification treatment is about 180 to 230 ℃, and the temperature of the waste incineration flue gas after the dry deacidification treatment is maintained about 180 to 230 ℃, which is just suitable for the SCR denitration treatment, and the subsequent wet deacidification treatment has no special requirement for the temperature of the waste incineration flue gas, and the whole process flow of the flue gas purification is performed in the process of descending the flue gas temperature step, so that there is no need to perform complicated process steps such as heating treatment on the waste incineration flue gas during the whole implementation of the flue gas purification method. Therefore, the flue gas purification method has the advantages of two aspects, on one hand, the waste incineration flue gas does not need to be additionally heated, so that the waste of heat energy consumption is avoided, the energy is saved, and the production cost is reduced. In addition, the temperature of the waste incineration flue gas at about 180-230 ℃ after the dry method deacidification treatment is also very suitable for the activated carbon to adsorb heavy metal and dioxin, and the process of adsorbing heavy metal and dioxin by using the activated carbon can be implemented while the SCR denitration treatment is carried out, so that the process flow of flue gas purification is further simplified.
The embodiment also provides a waste incineration flue gas purification system, and the flue gas purification system is used for implementing the flue gas purification method.
Referring to fig. 2, the flue gas purification system of the present embodiment includes a dry deacidification tower 1, an SCR denitration dust removal device 2, a wet deacidification tower 4, a flowing medium heat exchanger 3, an induced draft fan 5, and a chimney 6.
The smoke inlet of the dry deacidification tower 1 is communicated with the smoke outlet of the garbage incinerator (not shown in the figure) through a smoke pipeline, the garbage incineration smoke discharged from the garbage incinerator firstly enters the dry deacidification tower 1 for dry deacidification treatment, the temperature of the treated garbage incineration smoke is maintained at about 180-230 ℃, and the treated garbage incineration smoke leaves from the smoke outlet of the dry deacidification tower 1.
A dry powder supply device 11 is arranged above the dry deacidification tower 1, and the dry powder supply device 11 is used for supplying deacidification powder (namely 'dry powder') for dry deacidification treatment, wherein the deacidification powder can be sodium bicarbonate (NaHCO)3) Powder or slaked lime (Ca (OH)2) And (4) powder preparation.
It should be noted that the dry powder supply device 11 is a conventional configuration of the dry deacidification tower 1 in the prior art.
The smoke inlet of the SCR denitration dust removal device 2 is communicated with the smoke outlet of the dry deacidification tower 1 through a smoke pipeline, the waste incineration smoke treated by the dry deacidification tower 1 enters the SCR denitration dust removal device 2 for SCR denitration treatment, and the treated waste incineration smoke leaves from the smoke outlet of the SCR denitration dust removal device 2.
The inside of the SCR denitration dust collector 2 is provided with a filter component coated with a catalyst, which is different from the traditional filter component, the catalyst coated on the filter component comprises a manganese (Mn) based and/or copper (Cu) based low-temperature catalyst besides the traditional vanadium-titanium (V-Ti) based and vanadium-tungsten-titanium (V-W-Ti) based catalysts, that is, the catalyst adopted by the SCR denitration dust collector 2 comprises a manganese (Mn) based and/or copper (Cu) based low-temperature catalyst, so that a good denitration reaction can be realized as long as the waste incineration flue gas is kept in the temperature range of 150-250 ℃, and the denitration efficiency of 80% can be realized usually. After the waste incineration flue gas is treated by the dry deacidification tower 1, the temperature of the waste incineration flue gas is about 180-230 ℃, and is just in the temperature range of 150-250 ℃, so that the waste incineration flue gas does not need to be additionally heated or cooled.
The filter part coated with the catalyst can adopt a catalytic ceramic fiber pipe or a catalytic filter bag. The catalyst ceramic fiber pipe and the catalytic filter bag have the same size, can be communicated and used interchangeably in the SCR denitration dust removal device 2, and can select the most economical equipment according to market cost change in the catalyst ceramic fiber pipe and the catalytic filter bag, so that the application scene of the flue gas purification process is enlarged.
An ammonia water supply device 12 and an activated carbon powder supply device 13 are arranged on a pipeline communicated with a smoke inlet of the SCR denitration dust removal device 2, ammonia gas in the ammonia water provided by the ammonia water supply device 12 is used as a denitration reducing agent required by SCR denitration treatment, and activated carbon powder provided by the activated carbon powder supply device 13 is used for absorbing heavy metals and dioxin in the waste incineration smoke while SCR denitration treatment is carried out on the waste incineration smoke.
A fly ash storage bin 21 is arranged below the SCR denitration dust removal device 2, and the fly ash storage bin 21 is used for storing salt particles, flue gas dust and unreacted deacidification powder generated in the reaction in the SCR denitration treatment process.
It should be noted that the ammonia water supply device 12, the fly ash storage 21, and the filter member coated with the catalyst are conventional configurations of the SCR denitration dust removal device 2 in the related art.
The flowing medium heat exchanger 3 is a device in the prior art, and has two medium flowing pipelines, wherein one medium flowing pipeline is called as a heat releasing medium pipeline, the other medium flowing pipeline is called as a heated medium pipeline, the temperature of the medium flowing in the heat releasing medium pipeline is higher than that of the medium flowing in the heated medium pipeline, and the medium in the heat releasing medium pipeline can transfer heat to the medium in the heated medium pipeline through a pipe wall. The fluid medium heat exchanger 3 used in the present embodiment is a heat exchanger called a "GGH heat exchanger", which is also a conventional heat exchanger.
The flue gas inlet of the wet deacidification tower 4 is communicated with the flue gas outlet of the SCR denitration dust removal device 2 through a flue gas pipeline and a heat release medium pipeline of the flowing medium heat exchanger 3, the flue gas outlet of the wet deacidification tower 4 is communicated with the flue gas inlet of the chimney 6 through a flue gas pipeline and a heated medium pipeline of the flowing medium heat exchanger 3, and the draught fan 5 is arranged on the flue gas pipeline communicated with the flue gas inlet of the chimney 6.
The waste incineration flue gas treated by the SCR denitration dust removal device 2 enters the wet deacidification tower 4 for wet deacidification treatment, and the treated waste incineration flue gas leaves from a smoke outlet of the wet deacidification tower 4. In the process, the flowing medium heat exchanger 3 exchanges heat between the waste incineration flue gas before entering the wet deacidification tower 4 and the waste incineration flue gas after leaving the wet deacidification tower 4, so that the temperature of the waste incineration flue gas before entering the wet deacidification tower 4 is reduced, and the temperature of the waste incineration flue gas after leaving the wet deacidification tower 4 is increased to 100-150 ℃, thereby preventing the condition of white smoke when the subsequent chimney 6 discharges the flue gas.
The wet deacidification tower 4 is provided with a deacidification agent supply device 41, and the deacidification agent supply device 41 is used for supplying deacidification agents for wet deacidification treatment. The deacidification agent adopts alkaline sodium hydroxide (NaOH) solution, the flue gas enters a wet deacidification tower and is further in countercurrent contact with the sodium hydroxide solution, so that the flue gas and the sodium hydroxide solution are fully reacted, and meanwhile, the solution at the bottom of the wet deacidification tower is recycled through a circulating pump.
The deacidification agent supply device 41 is a conventional configuration of the wet deacidification tower 4 in the related art.
Finally, the waste incineration flue gas after purification treatment is discharged to the atmosphere through a chimney 6 under the action of induced air of an induced draft fan 5.
The flue gas purification system of the embodiment can realize the waste incineration flue gas purification method, so that the two advantages of the flue gas purification method are realized, namely, on one hand, waste of heat energy consumption is avoided, energy is saved, production cost is reduced, on the other hand, the whole process flow of flue gas purification is simplified, and investment of process equipment is reduced.
The present invention is not limited to the above embodiments, and any modifications, equivalent replacements, improvements, etc. within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for purifying waste incineration flue gas is characterized by comprising the following steps: the flue gas purification method comprises the following steps:
s1, performing dry deacidification treatment on waste incineration flue gas;
s2, carrying out SCR denitration treatment on the waste incineration flue gas, wherein a catalyst adopted in the SCR denitration treatment comprises a low-temperature catalyst;
s3, performing wet deacidification treatment on the waste incineration flue gas;
and S4, discharging the waste incineration flue gas into the atmosphere.
2. The method for purifying waste incineration flue gas according to claim 1, characterized in that: the low-temperature catalyst is a manganese-based catalyst and/or a copper-based catalyst.
3. The method for purifying waste incineration flue gas according to claim 2, characterized in that: cerium and/or zirconium are added into the low-temperature catalyst.
4. The method for purifying waste incineration flue gas according to claim 1, characterized in that: the S2 further comprises: and in the SCR denitration treatment process, spraying activated carbon powder into the waste incineration flue gas.
5. The method for purifying waste incineration flue gas according to claim 1, characterized in that: the S3 further comprises: in the wet deacidification treatment process, the heat exchanger is adopted to carry out heat exchange on the waste incineration flue gas before the wet deacidification treatment and the waste incineration flue gas after the wet deacidification treatment.
6. The utility model provides a msw incineration gas cleaning system which characterized in that: comprises a dry deacidification tower (1), an SCR denitration dust removal device (2), a wet deacidification tower (4), an induced draft fan (5) and a chimney (6);
the smoke inlet of the dry deacidification tower (1) is communicated with the smoke outlet of the garbage incinerator;
a smoke inlet of the SCR denitration dust removal device (2) is communicated with a smoke outlet of the dry-method deacidification tower (1), and a catalyst adopted by the SCR denitration dust removal device (2) comprises a low-temperature catalyst;
the flue gas inlet of the wet-process deacidification tower (4) is communicated with the flue gas outlet of the SCR denitration dust removal device (2), the flue gas outlet of the wet-process deacidification tower (4) is communicated with the flue gas inlet of a chimney (6), and the induced draft fan (5) is arranged at the flue gas inlet of the chimney (6).
7. The waste incineration flue gas purification system according to claim 6, wherein: the low-temperature catalyst is a manganese-based catalyst and/or a copper-based catalyst.
8. The waste incineration flue gas purification system according to claim 7, wherein: cerium and/or zirconium are added into the low-temperature catalyst.
9. The waste incineration flue gas purification system according to claim 6, wherein: an active carbon powder supply device (13) is arranged on a pipeline communicated with a smoke inlet of the SCR denitration dust removal device (2).
10. The waste incineration flue gas purification system according to claim 6, wherein: the flue gas purification system also comprises a flowing medium heat exchanger (3);
the smoke inlet of the wet-process deacidification tower (4) is communicated with the smoke outlet of the SCR denitration dust removal device (2), and the smoke inlet of the wet-process deacidification tower (4) is communicated with the smoke outlet of the SCR denitration dust removal device (2) through a heat release medium pipeline of the flowing medium heat exchanger (3);
the smoke outlet of the wet deacidification tower (4) is communicated with the smoke inlet of the chimney (6), and the smoke outlet of the wet deacidification tower (4) is communicated with the smoke inlet of the chimney (6) through a heated medium pipeline of the flowing medium heat exchanger (3).
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