CN114452814A - Dry denitration process - Google Patents

Dry denitration process Download PDF

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Publication number
CN114452814A
CN114452814A CN202111681005.1A CN202111681005A CN114452814A CN 114452814 A CN114452814 A CN 114452814A CN 202111681005 A CN202111681005 A CN 202111681005A CN 114452814 A CN114452814 A CN 114452814A
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flue gas
denitration
treated
agent
treatment
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陈壁
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Shenzhen Huaming Environmental Protection Technology Co ltd
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Shenzhen Huaming Environmental Protection Technology Co ltd
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Priority to CN202111681005.1A priority Critical patent/CN114452814A/en
Priority to PCT/CN2022/072572 priority patent/WO2023123577A1/en
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Abstract

The invention discloses a dry denitration process, which comprises the following steps: spraying a solid denitrifying agent into the flue gas to be treated to carry out denitrifying treatment on the flue gas to be treated to obtain the denitrifying agentDenitrating flue gas; deacidifying the denitrated flue gas to obtain deacidified flue gas; performing dust removal treatment on the deacidified flue gas to obtain dust-removed flue gas; and carrying out deamination treatment on the dedusting flue gas to obtain treated flue gas. According to the technical scheme, after the denitration treatment is carried out by spraying the solid denitration agent into the flue gas to be treated, the deamination treatment is added, so that NH generated by the denitration treatment of the solid denitration agent3The denitration agent is removed, the problem of ammonia escape caused by poor mixing uniformity of the denitration agent and the flue gas in dry denitration is solved, the denitration efficiency is high, the cost is low, and the national ultra-low emission requirement is met.

Description

Dry denitration process
Technical Field
The invention relates to the technical field of flue gas denitration, and particularly relates to a dry-method denitration process.
Background
When denitration is performed on flue gas, a dry denitration process is adopted in the prior art to perform denitration treatment, namely, a powder or particle denitration agent is sprayed into a boiler to react with the flue gas in the boiler, so that denitration is realized.
Disclosure of Invention
The invention mainly aims to provide a dry-method denitration process, and aims to solve the problems that when denitration treatment is carried out by the dry-method denitration process, the denitration agent and flue gas are poor in mixing uniformity, and the denitration agent cannot react completely, so that ammonia escape is serious.
In order to achieve the purpose, the invention provides a dry-method denitration process, which comprises the following steps:
spraying a solid-state denitration agent into the flue gas to be treated so as to carry out denitration treatment on the flue gas to be treated, thereby obtaining denitration flue gas;
deacidifying the denitration flue gas to obtain deacidified flue gas;
performing dust removal treatment on the deacidified flue gas to obtain dust-removed flue gas;
and carrying out deamination treatment on the dedusting flue gas to obtain treated flue gas.
Optionally, the solid denitration agent is sprayed into the flue gas to be treated to perform denitration treatment on the flue gas to be treated, and the step of obtaining the denitration flue gas is performed at 850-900 ℃.
Optionally, the solid denitration agent comprises urea and a polymeric catalyst.
Optionally, the polymeric catalyst comprises at least one of polyethylene glycol, polyacrylic acid, sodium polyacrylate, polyvinyl alcohol, and polyvinyl pyrrolidone.
Optionally, the solid denitration agent further comprises a polymer auxiliary agent, and the polymer auxiliary agent comprises at least one of ammonium stearate, magnesium stearate, calcium stearate, precipitated calcium carbonate, magnesium oxide and zeolite.
Optionally, the solid denitration agent further comprises a silica carrier, and the metal sulfate is loaded on the silica carrier.
Optionally, the deamination treatment is performed on the dedusting flue gas, and the obtaining of the treated flue gas includes:
and removing ammonia gas in the dedusting flue gas by using a deamination agent at the temperature of 130-140 ℃ to obtain the treated flue gas.
Optionally, the deaminating agent comprises at least one of a heavy metal catalyst, activated carbon, and an acidic substance.
According to the technical scheme, after the denitration treatment is carried out by spraying the solid denitration agent into the flue gas to be treated, the deamination treatment is added, so that NH generated by the denitration treatment of the solid denitration agent3The denitration agent is removed, the problem of ammonia escape caused by poor mixing uniformity of the denitration agent and the flue gas in dry denitration is solved, the denitration efficiency is high, the cost is low, and the national ultra-low emission requirement is met.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other related drawings can be obtained according to the drawings without creative efforts.
Fig. 1 is a schematic flow chart of an embodiment of a dry denitration process provided by the present invention.
The implementation, functional features and advantages of the objects of the present invention will be further explained with reference to the accompanying drawings.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. It is to be understood that the described embodiments are merely a few embodiments of the invention, and not all embodiments.
It should be noted that those whose specific conditions are not specified in the examples were performed according to the conventional conditions or the conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially. In addition, the meaning of "and/or" appearing throughout includes three juxtapositions, exemplified by "A and/or B" including either A or B or both A and B. In addition, technical solutions between various embodiments may be combined with each other, but must be realized by a person skilled in the art, and when the technical solutions are contradictory or cannot be realized, such a combination should not be considered to exist, and is not within the protection scope of the present invention. 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 invention.
When denitration is performed on flue gas, a dry denitration process is adopted in the prior art to perform denitration treatment, namely, a powder or particle denitration agent is sprayed into a boiler to react with the flue gas in the boiler, so that denitration is realized.
In view of this, the present invention provides a dry denitration process, referring to fig. 1, including the following steps:
and step S10, spraying a solid denitration agent into the flue gas to be treated to carry out denitration treatment on the flue gas to be treated so as to obtain the denitration flue gas.
And step S10, the reaction is carried out at 850-900 ℃, and the solid denitration agent can fully react with the flue gas to be treated within the temperature range, so that denitration is realized.
The solid denitration agent comprises urea and a high polymer catalyst, the urea is responsible for reacting with NOx in the flue gas to realize denitration of the flue gas, and the addition of the high polymer catalyst is helpful for promoting the reaction of the urea and improving the denitration efficiency.
Further, the polymer catalyst includes at least one of polyethylene glycol, polyacrylic acid, sodium polyacrylate, polyvinyl alcohol, and polyvinylpyrrolidone, that is, the polymer catalyst may be any one or a combination of polyethylene glycol, polyacrylic acid, sodium polyacrylate, polyvinyl alcohol, and polyvinylpyrrolidone, which is not described in detail herein.
The solid denitrifying agent also comprises a high molecular auxiliary agent, wherein the high molecular auxiliary agent comprises at least one of ammonium stearate, magnesium stearate, calcium stearate, precipitated calcium carbonate, magnesium oxide and zeolite.
The solid denitration agent also comprises a silicon dioxide carrier, and metal sulfate is loaded on the silicon dioxide carrier.
And step S20, performing deacidification treatment on the denitration flue gas to obtain deacidified flue gas.
After the flue gas to be treated is denitrated, SO still can be contained in the flue gas2Acid gases such as HCl and HF, and therefore, the denitration flue gas needs to be deacidified to remove SO in the denitration flue gas2HCl and HF, etc.
The invention does not limit the specific process of deacidification treatment, and can be carried out according to the following steps: introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
And step S30, performing dust removal treatment on the deacidified flue gas to obtain dust-removed flue gas.
The deacidified flue gas still contains dust, so the deacidified flue gas needs to be subjected to dust removal treatment to remove the dust.
The invention does not limit the specific process of dust removal treatment, and can be carried out according to the following steps: providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
And step S40, performing deamination treatment on the dedusting flue gas to obtain treated flue gas.
Specifically, step S40 includes: and removing ammonia gas in the dedusting flue gas by using a deamination agent at the temperature of 130-140 ℃ to obtain the treated flue gas. Removal of NH from flue gas by deaminating agents3The problem of ammonia escape generated during denitration is solved, and the dosage of the reducing agent containing amino can be increased during denitration so as to ensure the denitration efficiency.
Further, the deamination agent comprises at least one of a heavy metal catalyst, activated carbon, and an acidic substance. Preferably, the heavy metal catalyst is a copper metal catalyst or a manganese metal catalyst.
It should be noted that step S40 can be performed in a deamination tower, which can be in the form of a fixed bed.
According to the technical scheme, after the denitration treatment is carried out by spraying the solid denitration agent into the flue gas to be treated, the deamination treatment is added, so that NH generated by the denitration treatment of the solid denitration agent3The denitration agent is removed, the problem of ammonia escape caused by poor mixing uniformity of the denitration agent and the flue gas in dry denitration is solved, the denitration efficiency is high, the cost is low, and the national ultra-low emission requirement is met.
The technical solutions of the present invention are further described in detail below with reference to specific examples and drawings, it should be understood that the following examples are merely illustrative of the present invention and are not intended to limit the present invention.
Example 1
(1) Spraying a solid denitration agent into the flue gas to be treated at 850 ℃ to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of polyethylene glycol, 5% of zeolite and 0.6% of silicon dioxide carrier by mass percentage.
(2) Introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidificationFlue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
(4) And removing ammonia gas in the dedusting flue gas by using a heavy metal catalyst at 130 ℃ to obtain the treated flue gas.
Example 2
(1) Spraying a solid denitration agent into the flue gas to be treated at 870 ℃ to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of polyacrylic acid, 5% of ammonium stearate and 0.6% of silicon dioxide carrier by mass percentage.
(2) Introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
(4) And removing ammonia gas in the dedusting flue gas by using activated carbon at the temperature of 140 ℃ to obtain the treated flue gas.
Example 3
(1) And spraying a solid denitration agent into the flue gas to be treated at 860 ℃ to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of sodium polyacrylate, 5% of magnesium stearate and 0.6% of silicon dioxide carrier by mass percentage.
(2) Introducing the denitrated flue gas into a semidry methodThe reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
(4) And removing ammonia gas in the dedusting flue gas by using an acidic substance at 135 ℃ to obtain the treated flue gas.
Example 4
(1) Spraying a solid denitration agent into the flue gas to be treated at 900 ℃ to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of polyvinyl alcohol, 5% of calcium stearate and 0.6% of silicon dioxide carrier by mass percentage.
(2) Introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
(4) And removing ammonia gas in the dedusting flue gas by using a heavy metal catalyst at 135 ℃ to obtain the treated flue gas.
Example 5
(1) Spraying a solid denitration agent into the flue gas to be treated at 890 ℃ to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of polyvinylpyrrolidone, 5% of precipitated calcium carbonate and 0.6% of silica carrier by mass percentage.
(2) Introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
(4) And removing ammonia gas in the dedusting flue gas by using activated carbon at the temperature of 130 ℃ to obtain the treated flue gas.
Example 6
(1) At 880 ℃, spraying a solid denitration agent into the flue gas to be treated to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of a high-molecular catalyst (comprising polyethylene glycol and polyacrylic acid in a mass ratio of 1: 1), 5% of magnesium oxide and 0.6% of a silicon dioxide carrier in percentage by mass.
(2) Introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
(4) And removing ammonia gas in the dedusting flue gas by using an acidic substance at 140 ℃ to obtain the treated flue gas.
Example 7
(1) At 880 ℃, spraying a solid denitration agent into the flue gas to be treated to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of polyethylene glycol, 5% of a high-molecular auxiliary agent (comprising magnesium oxide and ammonium stearate in a mass ratio of 1: 1) and 0.6% of a silicon dioxide carrier according to mass percentage.
(2) Introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the pulp by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized pulp at high speed to form liquid drops with the particle size of 20-501 xm, spraying the liquid drops into a semi-dry reaction tower, fully mixing the liquid drops with denitration flue gas in the semi-dry reaction tower, reacting for 1s at 150 ℃, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
(4) And removing ammonia gas in the dedusting flue gas by using an acidic substance at 140 ℃ to obtain the treated flue gas.
Comparative example 1
(1) And carrying out selective catalytic reduction denitration treatment on the flue gas to be treated to obtain the denitration flue gas.
(2) Introducing the denitration flue gas into a semi-dry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
Comparative example 2
(1) Spraying a solid denitration agent into the flue gas to be treated at 900 ℃ to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas, wherein the solid denitration agent comprises 90% of urea, 4.4% of polyethylene glycol, 5% of zeolite and 0.6% of silicon dioxide carrier by mass percentage.
(2) Introducing the denitration flue gas into a semidry reaction tower; pulping slaked lime at normal temperature, atomizing the slurry by a rotary atomizing disc (the rotating speed is 15000rph), spraying the atomized slurry at high speed to form droplets with the particle size of 20-501 xm, spraying the droplets into a semi-dry reaction tower, fully mixing the droplets with denitration flue gas in the semi-dry reaction tower, reacting at 150 ℃ for 1s, and removing SO2HCl and HF to obtain deacidified flue gas.
(3) Providing a bag-type dust collector, wherein a plurality of filter bags are arranged in the bag-type dust collector; and (2) introducing deacidified flue gas into a bag-type dust remover, wherein the deacidified flue gas passes through the filter bags at the wind speed of 2-4 m/min, and dust in the deacidified flue gas is adsorbed on the filter bags to obtain dedusting flue gas.
The flue gas treatment test was carried out on the flue gas produced from the garbage incinerator in a treatment amount of 500t/d by the process steps of examples 1 to 7 and comparative examples 1 to 2, and the results are shown in the following table 1. Wherein the environmental protection indexes are as follows: NOx is less than or equal to 80mg/Nm 3; NH3 is less than or equal to 8mg/Nm 3.
TABLE 1 Process steps of examples 1-7, comparative examples 1-2 for treating flue gas costs and effectiveness
Figure BDA0003448709800000091
As can be seen from Table 1, the dry denitration process provided by the embodiment of the invention can meet the environmental protection requirement, and has high denitration efficiency, low investment cost and low operation cost.
The above are only preferred embodiments of the present invention, and do not limit the scope of the present invention, and it is obvious to those skilled in the art that various modifications and variations can be made in the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention shall be included in the scope of the present invention.

Claims (8)

1. A dry denitration process is characterized by comprising the following steps:
spraying a solid-state denitration agent into the flue gas to be treated so as to carry out denitration treatment on the flue gas to be treated, thereby obtaining denitration flue gas;
deacidifying the denitration flue gas to obtain deacidified flue gas;
performing dust removal treatment on the deacidified flue gas to obtain dust-removed flue gas;
and carrying out deamination treatment on the dedusting flue gas to obtain treated flue gas.
2. The dry denitration process of claim 1, wherein the step of spraying the solid denitration agent into the flue gas to be treated to perform denitration treatment on the flue gas to be treated to obtain the denitration flue gas is performed at 850-900 ℃.
3. The dry denitration process according to claim 1, wherein the solid denitration agent comprises urea and a polymeric catalyst.
4. The dry denitration process according to claim 3, wherein the polymeric catalyst comprises at least one of polyethylene glycol, polyacrylic acid, sodium polyacrylate, polyvinyl alcohol and polyvinylpyrrolidone.
5. The dry denitration process of claim 3, wherein the solid denitration agent further comprises a polymer auxiliary agent, and the polymer auxiliary agent comprises at least one of ammonium stearate, magnesium stearate, calcium stearate, precipitated calcium carbonate, magnesium oxide and zeolite.
6. The dry denitration process of claim 3, wherein the solid denitration agent further comprises a silica support, and the metal sulfate is supported on the silica support.
7. The dry denitration process of claim 1, wherein the deamination of the dedusting flue gas to obtain a treated flue gas comprises:
and removing ammonia gas in the dedusting flue gas by using a deamination agent at the temperature of 130-140 ℃ to obtain the treated flue gas.
8. The dry denitration process of claim 2, wherein the deaminating agent comprises at least one of a heavy metal catalyst, activated carbon, and an acidic material.
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