CN211753792U

CN211753792U - Ammonia spraying system for flue gas treatment

Info

Publication number: CN211753792U
Application number: CN201921898526.0U
Authority: CN
Inventors: 魏进超; 康建刚; 彭杰
Original assignee: Zhongye Changtian International Engineering Co Ltd
Current assignee: Zhongye Changtian International Engineering Co Ltd
Priority date: 2019-11-05
Filing date: 2019-11-05
Publication date: 2020-10-27
Anticipated expiration: 2029-11-05

Abstract

An ammonia injection system for flue gas treatment, the system comprising: a denitration tower, an adsorption tower and an ammonia spraying device; the sintering flue gas enters the adsorption tower through a raw flue gas pipeline; the flue gas discharged from the adsorption tower enters a denitration tower through a second pipeline; the denitration tower discharges flue gas through a first pipeline; a first ammonia spraying port of the ammonia spraying device is arranged on the second pipeline; the ammonia gas is communicated with the first ammonia spraying port through a third pipeline; and a branch of the third pipeline is a fourth pipeline, and the fourth pipeline is communicated with the original flue gas pipeline. The utility model provides a technical scheme lets in the ammonia through the sintering flue gas before getting into the adsorption tower and before getting into the denitration tower to improve the desulfurization and the efficiency of denitration of adsorption tower and denitration tower, reduce the escape volume of ammonia, thereby can reduce enterprise manufacturing cost, improve production speed.

Description

Ammonia spraying system for flue gas treatment

Technical Field

The utility model relates to a flue gas processing system, concretely relates to ammonia system is spouted in flue gas treatment belongs to sintering device technical field.

Background

The sintering technology is widely applied to the production process of mineral smelting. The flue gas generated by sintering basically meets the emission standard of the sintering flue gas, but in the prior art, only the ammonia gas is added into the sintering flue gas entering an adsorption tower or the sintering flue gas entering a denitration tower. If less ammonia is introduced into the sintering flue gas entering the adsorption tower, the desulfurization efficiency of the adsorption tower cannot be effectively improved, otherwise, too much ammonia is caused to escape; if less ammonia is introduced into the sintering flue gas entering the denitration tower, the SCR catalyst is poisoned due to sulfur dioxide in the sintering flue gas.

Therefore, how to provide a flue gas treatment ammonia injection system can improve the efficiency of the desulfurization and the denitration of adsorption tower and denitration tower, reduces the escape volume of ammonia, reduces the manufacturing cost of enterprise, improves production speed, and the technical problem that the skilled person in the art needs to solve urgently.

SUMMERY OF THE UTILITY MODEL

Not enough to above-mentioned prior art, the utility model discloses an ammonia is let in through the sintering flue gas before getting into the adsorption tower and before getting into the denitration tower to improve the desulfurization and the efficiency of denitration of adsorption tower and denitration tower, reduce the escape volume of ammonia, thereby can reduce the manufacturing cost of enterprise, improve production speed. The utility model provides an ammonia system is spouted in flue gas treatment, this system includes: a denitration tower, an adsorption tower and an ammonia spraying device; the sintering flue gas enters the adsorption tower through a raw flue gas pipeline; the flue gas discharged from the adsorption tower enters a denitration tower through a second pipeline; the denitration tower discharges flue gas through a first pipeline; a first ammonia spraying port of the ammonia spraying device is arranged on the second pipeline; the ammonia gas is communicated with the first ammonia spraying port through a third pipeline; and a branch of the third pipeline is a fourth pipeline, and the fourth pipeline is communicated with the original flue gas pipeline.

According to the utility model discloses an embodiment provides a flue gas is handled and is spouted ammonia system:

an ammonia injection system for flue gas treatment, the system comprising: a denitration tower, an adsorption tower and an ammonia spraying device; the sintering flue gas enters the adsorption tower through a raw flue gas pipeline; the flue gas discharged from the adsorption tower enters a denitration tower through a second pipeline; the denitration tower discharges flue gas through a first pipeline; a first ammonia spraying port of the ammonia spraying device is arranged on the second pipeline; the ammonia gas is communicated with the first ammonia spraying port through a third pipeline; and a branch of the third pipeline is a fourth pipeline, and the fourth pipeline is communicated with the original flue gas pipeline.

Preferably, the ammonia injection device further comprises: an ammonia-air mixing chamber; the exhaust port of the ammonia-air mixing chamber is communicated with the third pipeline; an ammonia gas inlet of the ammonia-air mixing chamber is communicated with a fifth pipeline, and ammonia gas is introduced into the fifth pipeline; and a heat medium inlet of the ammonia-air mixing chamber is communicated with a sixth pipeline, and a heat medium is introduced into the sixth pipeline.

Preferably, an air bypass is connected to the upstream of the sixth pipeline; the air bypass is provided with a first control valve.

Preferably, the front end of the sixth pipe is connected to the first pipe.

Preferably, the system further comprises: a flue gas flow monitoring sensor, a sulfur dioxide concentration monitoring sensor, a nitrogen oxide concentration monitoring sensor, an ammonia gas flow monitoring sensor, an escape ammonia gas concentration monitoring sensor and a second control valve; the flue gas flow monitoring sensor, the sulfur dioxide concentration monitoring sensor and the nitrogen oxide concentration monitoring sensor are all arranged on an original flue gas pipeline; the ammonia gas flow monitoring sensor and the second control valve are both arranged on the fifth pipeline; the escaping ammonia concentration monitoring sensor is arranged on the first pipeline; the smoke flow monitoring sensor detects the flow of the original smoke and is marked as Q_{Flue gas}(ii) a The sulfur dioxide concentration monitoring sensor detects the content of sulfur dioxide in the original flue gas, and the mark is C_{Sulfur dioxide}And (c); nitrogen oxidesThe content of nitrogen oxide in the raw smoke of the concentration monitoring sensor is marked as C_{Nitrogen oxides}And (c); the escaping ammonia concentration monitoring sensor detects the escaping amount of ammonia in the first pipeline, and the mark is C_{Ammonia slip}And (c); the conveying capacity Q in the fifth pipeline is adjusted through a second control valve_{Ammonia gas}Comprises the following steps:

Q_{ammonia gas}＝Q_{Flue gas}×(aC_{Sulfur dioxide}+bC_{Nitrogen oxides}-C_{Ammonia slip})；

Wherein: a is the reaction coefficient of sulfur dioxide consuming ammonia in the flue gas, the value of a is 0.1-0.6, preferably the value of a is 0.15-0.5, and more preferably the value of a is 0.1-0.4; b is the reaction coefficient of nitrogen oxide in the flue gas for consuming ammonia, and the value of b is 0.5-2; preferably, b has a value of 0.6 to 1.5; more preferably, b has a value of 0.7 to 1.2.

Preferably, the sixth pipeline is provided with a third control valve and a heat medium flow monitoring sensor, and the third control valve is positioned upstream of the heat medium flow monitoring sensor; the flow Q of the hot medium in the sixth pipeline is regulated by a third control valve_{Heat generation}Comprises the following steps:

Q_{heat generation}＝Q_{Ammonia gas}/c；

Wherein: c is 1% to 20%, preferably 1.5% to 10%, more preferably 2% to 5%.

Preferably, a fourth control valve is arranged on the third pipeline, and the fourth control valve is positioned at the downstream of the position of the fourth pipeline separated from the third pipeline; and a fifth control valve is arranged on the fourth pipeline.

Preferably, the fourth control valve is adjusted so that the amount Q of the ammonia gas and the heat medium delivered to the first ammonia injection port via the third pipe_DenitrationComprises the following steps:

adjusting the fifth control valve to ensure that the quantity Q of the ammonia gas and the heat medium conveyed into the raw flue gas pipeline through the fourth pipeline_{Desulfurization of}Comprises the following steps:

preferably, the system further comprises: a dilution fan; the dilution fan is disposed in the sixth conduit downstream of the location where the sixth conduit connects to the air bypass.

Preferably, the communication between the fourth pipeline and the raw flue gas pipeline is specifically as follows: and an eighth pipeline for separating the raw flue gas pipeline is connected into the adsorption tower, and the fourth pipeline is communicated with the eighth pipeline.

Preferably, the position where the eighth pipe joins the adsorption tower is located at the upper part of the adsorption tower.

Preferably, in the SCR denitration device of the denitration tower, the adsorption tower is an activated carbon adsorption tower.

Preferably, m SCR denitration devices and n CO catalytic oxidation layers are arranged in the denitration tower, and the SCR denitration devices and the CO catalytic oxidation layers are arranged at intervals; wherein: m and n are each independently 1 to 5, preferably 2 to 4.

In this application, spout ammonia device and spout ammonia mouth intercommunication through third pipeline with first, add the ammonia to the sintering flue gas that has just passed through the adsorption tower desulfurization absorption. Meanwhile, the ammonia spraying device is also communicated with the flue gas pipeline through a fourth pipeline, and ammonia gas is added into the sintering flue gas which is about to enter the adsorption tower. The sintering flue gas lets in the ammonia before getting into the adsorption tower, and when the ammonia reacted with the nitrogen oxide in the sintering flue gas and reduced nitrogen oxide content, the ammonia still combined with the sulfur dioxide in the flue gas and generated ammonium sulfite, was favorable to activated carbon to sulfur dioxide's absorption to the efficiency of entire system's SOx/NOx control has been improved. A small amount of sulfur dioxide is also present in the sintering flue gas discharged from the adsorption tower. Research shows that a small amount of sulfur dioxide in the sintering flue gas can poison the SCR catalyst in the SCR denitration device, and finally the denitration efficiency of the denitration tower is reduced. In this scheme, to adding a large amount of ammonia in the sintering flue gas from the adsorption tower exhaust, can further reduce sulfur dioxide's in the sintering flue gas concentration effectively to prevent that the SCR catalyst from poisoning, finally further improved whole SOx/NOx control system's SOx/NOx control efficiency, reduce SOx/NOx control's catalyst's use amount, reduced enterprise manufacturing cost.

It should be noted that the fourth pipeline may also be directly connected to the ammonia gas outlet of the ammonia injection device.

In this application, mix ammonia and gas medium through ammonia air mixing chamber to reduce the concentration of ammonia, prevent that the ammonia from gathering into the explosion when high temperature sintering flue gas.

In this application, the gaseous medium of sneaking into ammonia air mixing chamber is the hot medium, and hot medium gas mixes the temperature that can improve the ammonia with the ammonia, lies in the same temperature of sintering flue gas with the temperature control of ammonia, can prevent because low temperature ammonia mixes the back with sintering flue gas, and the condensation takes place for the sintering flue gas to the pipeline that prevents the sintering flue gas is corroded.

In the present application, by providing an air bypass on the sixth pipe, air can be introduced into the sixth pipe, thereby adjusting the temperature of the heat medium gas. The amount of air mixed is adjusted by the first control valve.

In this application, the heat medium that is passed into the sixth pipeline is the clean flue gas in the first pipeline.

In the application, the flow rate, the concentration of sulfur dioxide and the concentration of nitrogen oxide of the flue gas in the second pipeline are monitored; and monitoring the concentration of the escaped ammonia in the first pipeline, and adjusting the delivery amount of the ammonia in the fifth pipeline.

In this application, the flow of the heating medium in the sixth pipe is regulated and controlled by means of a third control valve in the sixth pipe. Through fourth control valve and fifth control valve, can adjust the volume of the ammonia that gets into the second pipeline through first ammonia nozzle.

In this application, can adjust the volume of the ammonia that gets into former flue gas pipeline through the fifth control valve.

In this application, the heat medium and air are mixed into the ammonia air mixing chamber to provide motive power through the dilution fan.

In this application, the raw flue gas pipeline is divided into an eighth pipeline and is communicated with a fourth pipeline. The eighth pipeline and the original flue gas pipeline form a flue gas conveying pipeline matched with the main and standby pipelines. When the eighth pipeline is blocked or leaks gas, the sintering flue gas can directly enter the adsorption tower through the original flue gas pipeline without stopping, and the maintenance cost of an enterprise is saved.

In this application, the upper portion of eighth pipeline access adsorption tower can make the sintering flue gas more abundant sneak into the adsorption tower, improves the adsorption efficiency of adsorption tower.

In this application, be provided with a plurality of SCR denitrification facility and a plurality of CO catalytic oxidation layer to make the purification of sintering flue gas more accurate.

The application also provides a method for stopping the ammonia spraying system for flue gas treatment, which comprises the following steps: the second control valve is closed, then the first control valve is opened and the third control valve is closed, and the hot air pipeline is purged by air. The pipeline and the equipment on the pipeline are prevented from being corroded, and finally the dilution fan is shut down.

It needs to be further explained that the beneficial effects of the scheme include:

1) the system has strong adjustability, and ammonia can be sprayed into the inlet of the adsorption tower to realize ultralow emission and strengthen the desulfurization and denitrification effects if the concentration of nitrogen oxides in the flue gas is high, or the denitration efficiency of the SCR catalyst is low due to poisoning, or the desulfurization efficiency is insufficient due to high concentration fluctuation of sulfur dioxide in the flue gas;

2) the influence of SO2 on the reaction of NH3 and NOx can be reduced;

3) the reaction effectively utilizes the clean flue gas with a certain temperature, saves energy consumption and simultaneously prevents pollutants in the clean flue gas from corroding a pipeline system;

4) the ammonia escape can be effectively reduced, and the denitration rate is ensured.

Compared with the prior art, the utility model discloses following beneficial effect has:

1. according to the technical scheme provided by the application, the desulfurization and denitrification efficiency of the system can be effectively improved, the usage amount of the catalyst can be reduced, and the production cost of an enterprise is reduced;

2. according to the technical scheme, the ammonia gas can be prevented from being mixed into the sintering flue gas, so that the flue gas conveying pipeline is prevented from being exploded and corroded;

3. the application provides a technical scheme, can reduce the SOx/NOx control in-process, extra heat supply to reduction in production cost.

Drawings

FIG. 1 is a schematic view of the overall structure of a flue gas treatment ammonia injection system of the present invention;

fig. 2 is a schematic structural diagram of the ammonia gas mixing type in the flue gas treatment ammonia spraying system of the present invention.

Reference numerals:

1: a denitration tower; 101: an SCR denitration device; 102: a CO catalytic oxidation layer; 2: an adsorption tower; 3: an ammonia injection device; 301: a first ammonia spraying port; 302: an ammonia-air mixing chamber; 303: a dilution fan;

l0: an original flue gas pipeline; l1: a first conduit; l2: a second conduit; l3: a third pipeline; l4: a fourth conduit; l5: a fifth pipeline; l6: a sixth pipeline; l7: an air bypass; l8: an eighth conduit;

k1: a first control valve; k2: a second control valve; k3: a third control valve; k4: a fourth control valve; k5: a fifth control valve; q1: a flue gas flow monitoring sensor; c1: a sulfur dioxide concentration monitoring sensor; c2: a nitrogen oxide concentration monitoring sensor; q2: an ammonia gas flow monitoring sensor; c3: an escaping ammonia gas concentration monitoring sensor; q3: and a heat medium flow monitoring sensor.

Detailed Description

an ammonia injection system for flue gas treatment, the system comprising: the device comprises a denitration tower 1, an adsorption tower 2 and an ammonia spraying device 3; the sintering flue gas enters the adsorption tower 2 through an original flue gas pipeline L0; flue gas discharged from the adsorption tower 2 enters the denitration tower 1 through a second pipeline L2; the denitration tower 1 discharges flue gas through a first pipeline L1; the first ammonia injection port 301 of the ammonia injection device 3 is arranged on the second pipeline L2; the ammonia gas is communicated with the first ammonia spraying port 301 through a third pipeline L3; the third pipeline L3 is branched into a fourth pipeline L4, and the fourth pipeline L4 is communicated with the original smoke pipeline L0.

Preferably, the ammonia injection device 3 further includes: an ammonia-air mixing chamber 302; the exhaust port of the ammonia-air mixing chamber 302 communicates with the third pipe L3; an ammonia gas inlet of the ammonia-air mixing chamber 302 is communicated with a fifth pipeline L5, and ammonia gas is introduced into a fifth pipeline L5; the heat medium inlet of the ammonia-air mixing chamber 302 is connected to a sixth line L6, and a heat medium is introduced into the sixth line L6.

Preferably, an air bypass L7 is connected upstream of the sixth conduit L6; the air bypass L7 is provided with a first control valve K1.

Preferably, a front end of the sixth duct L6 is connected to the first duct L1.

Preferably, the system further comprises: a flue gas flow monitoring sensor Q1, a sulfur dioxide concentration monitoring sensor C1, a nitrogen oxide concentration monitoring sensor C2, an ammonia gas flow monitoring sensor Q2, an escaping ammonia gas concentration monitoring sensor C3 and a second control valve K2; a flue gas flow monitoring sensor Q1, a sulfur dioxide concentration monitoring sensor C1 and a nitrogen oxide concentration monitoring sensor C2 are all arranged on an original flue gas pipeline L0; the ammonia gas flow monitoring sensor Q2 and the second control valve K2 are both arranged on the fifth pipeline L5; the escaped ammonia gas concentration monitoring sensor C3 is arranged on the first pipeline L1; the flue gas flow monitoring sensor Q1 detects the flow of the original flue gas, and is marked as Q_{Flue gas}(ii) a The sulfur dioxide concentration monitoring sensor C1 detects the content of sulfur dioxide in the original flue gas, and is marked as C_{Sulfur dioxide}And (c); the content of the nitrogen oxide in the original smoke of the nitrogen oxide concentration monitoring sensor C2 is marked as C_{Nitrogen oxides}And (c); the escaped ammonia concentration monitoring sensor C3 detects the escaped amount of ammonia in the first pipeline L1, which is marked as C_{Ammonia slip}And (c); the delivery Q in the fifth line L5 is regulated by means of a second control valve K2_{Ammonia gas}Comprises the following steps:

Preferably, the sixth line L6 is provided with a third control valve K3 and a heat medium flow rate monitoring sensorQ3, and the third control valve K3 is located upstream of the heat medium flow monitoring sensor Q3; the flow rate Q of the hot medium in the sixth pipeline L6 is regulated by a third control valve K3_{Heat generation}Comprises the following steps:

Q_{heat generation}＝Q_{Ammonia gas}/c；

Wherein: c is 1% to 20%, preferably 1.5% to 10%, more preferably 2% to 5%.

Preferably, the third line L3 is provided with a fourth control valve K4, and the fourth control valve K4 is located downstream of the position where the third line L3 branches off the fourth line L4; a fifth control valve K5 is provided on the fourth line L4.

Preferably, the fourth control valve K4 is adjusted so that the amount Q of the ammonia gas and the heat medium delivered to the first ammonia injection port 301 via the third pipe L3_DenitrationComprises the following steps:

the fifth control valve K5 is adjusted so that the amount Q of ammonia gas and heat medium delivered into the raw flue gas pipe L0 via the fourth pipe L4_{Desulfurization of}Comprises the following steps:

preferably, the system further comprises: a dilution fan 303; the dilution fan 303 is disposed in the sixth conduit L6 downstream of the connection point of the sixth conduit L6 and the air bypass L7.

Preferably, the communication between the fourth pipeline L4 and the raw flue gas pipeline L0 is: an eighth pipeline L8 branched from the original flue gas pipeline L0 is connected to the adsorption tower 2, and a fourth pipeline L4 is communicated with the eighth pipeline L8.

Preferably, the position where the eighth line L8 joins the adsorption column 2 is located at the upper part of the adsorption column 2.

Preferably, in the SCR denitration device of the denitration tower 1, the adsorption tower 2 is an activated carbon adsorption tower.

Preferably, m SCR denitration devices 101 and n CO catalytic oxidation layers 102 are arranged in the denitration tower 1, and the SCR denitration devices 101 and the CO catalytic oxidation layers 102 are arranged at intervals; wherein: m and n are each independently 1 to 5, preferably 2 to 4.

Example 1

Example 2

Example 1 was repeated except that the ammonia injection apparatus 3 further included: an ammonia-air mixing chamber 302; the exhaust port of the ammonia-air mixing chamber 302 communicates with the third pipe L3; an ammonia gas inlet of the ammonia-air mixing chamber 302 is communicated with a fifth pipeline L5, and ammonia gas is introduced into a fifth pipeline L5; the heat medium inlet of the ammonia-air mixing chamber 302 is connected to a sixth line L6, and a heat medium is introduced into the sixth line L6.

Example 3

Example 2 was repeated except that an air bypass L7 was connected upstream of the sixth conduit L6; the air bypass L7 is provided with a first control valve K1.

Example 4

Embodiment 3 is repeated except that the front end of the sixth pipeline L6 is connected to the first pipeline L1.

Example 5

Example 4 was repeated except that the system further included: a flue gas flow monitoring sensor Q1, a sulfur dioxide concentration monitoring sensor C1, a nitrogen oxide concentration monitoring sensor C2, an ammonia gas flow monitoring sensor Q2, an escaping ammonia gas concentration monitoring sensor C3 and a second control valve K2; a flue gas flow monitoring sensor Q1, a sulfur dioxide concentration monitoring sensor C1 and a nitrogen oxide concentration monitoring sensor C2 are all arranged on an original flue gas pipeline L0; the ammonia gas flow monitoring sensor Q2 and the second control valve K2 are both arranged on the fifth pipeline L5; the escaped ammonia gas concentration monitoring sensor C3 is arranged on the first pipeline L1;the flue gas flow monitoring sensor Q1 detects the flow of the original flue gas, and is marked as Q_{Flue gas}(ii) a The sulfur dioxide concentration monitoring sensor C1 detects the content of sulfur dioxide in the original flue gas, and is marked as C_{Sulfur dioxide}And (c); the content of the nitrogen oxide in the original smoke of the nitrogen oxide concentration monitoring sensor C2 is marked as C_{Nitrogen oxides}And (c); the escaped ammonia concentration monitoring sensor C3 detects the escaped amount of ammonia in the first pipeline L1, which is marked as C_{Ammonia slip}And (c); the delivery Q in the fifth line L5 is regulated by means of a second control valve K2_{Ammonia gas}Comprises the following steps:

Example 6

Example 5 was repeated except that the sixth line L6 was provided with the third control valve K3 and the heat medium flow rate monitor sensor Q3, and the third control valve K3 was located upstream of the heat medium flow rate monitor sensor Q3; the flow rate Q of the hot medium in the sixth pipeline L6 is regulated by a third control valve K3_{Heat generation}Comprises the following steps:

Q_{heat generation}＝Q_{Ammonia gas}/c；

Wherein: c is 1% to 20%, preferably 1.5% to 10%, more preferably 2% to 5%.

Example 7

Example 6 was repeated except that the third line L3 was provided with the fourth control valve K4 and the fourth control valve K4 was located downstream of the point where the third line L3 branched off the fourth line L4; a fifth control valve K5 is provided on the fourth line L4.

Example 8

Example 7 was repeated except that the fourth control valve K4 was adjusted so that the amount Q of the ammonia gas and the heat medium delivered to the first ammonia injection port 301 via the third line L3_DenitrationComprises the following steps:

example 9

Example 8 is repeated except that the system further comprises: a dilution fan 303; the dilution fan 303 is disposed in the sixth conduit L6 downstream of the connection point of the sixth conduit L6 and the air bypass L7.

Example 10

Example 9 is repeated, except that the communication between the fourth pipeline L4 and the raw flue gas pipeline L0 is specifically as follows: an eighth pipeline L8 branched from the original flue gas pipeline L0 is connected to the adsorption tower 2, and a fourth pipeline L4 is communicated with the eighth pipeline L8. The position where the eighth line L8 joins the adsorption column 2 is located at the upper part of the adsorption column 2.

Example 11

Example 10 was repeated except that the SCR denitration apparatus of the denitration tower 1 and the adsorption tower 2 were an activated carbon adsorption tower.

Example 12

Example 11 is repeated, except that m SCR denitration devices 101 and n CO catalytic oxidation layers 102 are arranged in the denitration tower 1, and the SCR denitration devices 101 and the CO catalytic oxidation layers 102 are arranged at intervals; wherein: m and n are each independently 1 to 5, preferably 2 to 4.

Claims

1. The utility model provides a flue gas is handled and is spouted ammonia system which characterized in that: the system comprises: the device comprises a denitration tower (1), an adsorption tower (2) and an ammonia spraying device (3);

the sintering flue gas enters the adsorption tower (2) through an original flue gas pipeline (L0); flue gas discharged by the adsorption tower (2) enters the denitration tower (1) through a second pipeline (L2); the denitration tower (1) discharges flue gas through a first pipeline (L1);

a first ammonia spraying opening (301) of the ammonia spraying device (3) is arranged on the second pipeline (L2); the ammonia gas is communicated with the first ammonia spraying port (301) through a third pipeline (L3);

the third pipeline (L3) is divided into a branch and is a fourth pipeline (L4), and the fourth pipeline (L4) is communicated with the original smoke pipeline (L0).

2. The flue gas treatment ammonia injection system of claim 1, wherein: the ammonia injection device (3) further comprises: an ammonia-air mixing chamber (302);

the exhaust port of the ammonia-air mixing chamber (302) is communicated with a third pipeline (L3);

an ammonia gas inlet of the ammonia-air mixing chamber (302) is communicated with a fifth pipeline (L5), and ammonia gas is introduced into the fifth pipeline (L5);

the heat medium inlet of the ammonia-air mixing chamber (302) is communicated with a sixth pipeline (L6), and the heat medium is introduced into the sixth pipeline (L6).

3. The flue gas treatment ammonia injection system of claim 2, wherein: an air bypass (L7) is connected to the upstream of the sixth pipeline (L6); a first control valve (K1) is arranged on the air bypass (L7); and/or

The front end of the sixth duct (L6) is connected to the first duct (L1).

4. The flue gas treatment ammonia injection system of claim 2 or 3, wherein: the system further comprises: a flue gas flow monitoring sensor (Q1), a sulfur dioxide concentration monitoring sensor (C1), a nitrogen oxide concentration monitoring sensor (C2), an ammonia gas flow monitoring sensor (Q2), an escaping ammonia gas concentration monitoring sensor (C3) and a second control valve (K2);

the flue gas flow monitoring sensor (Q1), the sulfur dioxide concentration monitoring sensor (C1) and the nitrogen oxide concentration monitoring sensor (C2) are all arranged on the original flue gas pipeline (L0); the ammonia gas flow monitoring sensor (Q2) and the second control valve (K2) are both arranged on the fifth pipeline (L5); the escaped ammonia gas concentration monitoring sensor (C3) is arranged on the first pipeline (L1);

the smoke flow monitoring sensor (Q1) detects the flow of the original smoke and is marked as Q_{Flue gas}(ii) a A sulfur dioxide concentration monitoring sensor (C1) detects the content of sulfur dioxide in the original flue gas, and is marked as C_{Sulfur dioxide}And (c); the content of nitrogen oxide in the raw smoke of the nitrogen oxide concentration monitoring sensor (C2) is marked as C_{Nitrogen oxides}And (c); the escaped ammonia concentration monitoring sensor (C3) detects the escaped amount of ammonia in the first pipeline (L1), which is marked as C_{Ammonia slip}And (c); the delivery quantity Q in the fifth line (L5) is regulated by a second control valve (K2)_{Ammonia gas}Comprises the following steps:

Wherein: a is the reaction coefficient of sulfur dioxide in the flue gas to consume ammonia, and the value of a is 0.1-0.6; b is the reaction coefficient of nitrogen oxide in the flue gas to consume ammonia, and the value of b is 0.5-2.

5. The flue gas treatment ammonia injection system of claim 4, wherein: the value of a is 0.15-0.5; the value of b is 0.6-1.5.

6. The flue gas treatment ammonia injection system of claim 4, wherein: the value of a is 0.1-0.4; the value of b is 0.7-1.2.

7. The flue gas treatment ammonia injection system of claim 4, wherein: a third control valve (K3) and a heat medium flow monitoring sensor (Q3) are arranged on the sixth pipeline (L6), and the third control valve (K3) is positioned at the upstream of the heat medium flow monitoring sensor (Q3); the flow rate Q of the hot medium in the sixth pipeline (L6) is adjusted by a third control valve (K3)_{Heat generation}Comprises the following steps:

Q_{heat generation}＝Q_{Ammonia gas}C; wherein: c is 1 to 20 percent.

8. The flue gas treatment ammonia injection system of claim 5 or 6, wherein: a third control valve (K3) and a heat medium flow monitoring sensor (Q3) are arranged on the sixth pipeline (L6), and the third control valve (K3) is positioned at the upstream of the heat medium flow monitoring sensor (Q3); by third controlThe valve (K3) regulates the flow rate Q of the heat medium in the sixth pipeline (L6)_{Heat generation}Comprises the following steps:

Q_{heat generation}＝Q_{Ammonia gas}C; wherein: c is 1 to 20 percent.

9. The flue gas treatment ammonia injection system of claim 7, wherein: c is 1.5 to 10 percent.

10. The flue gas treatment ammonia injection system of claim 8, wherein: c is 1.5 to 10 percent.

11. The flue gas treatment ammonia injection system of claim 9 or 10, wherein: c is 2 to 5 percent.

12. The flue gas treatment ammonia injection system of any one of claims 7, 9-10, wherein: a fourth control valve (K4) is arranged on the third pipeline (L3), and the fourth control valve (K4) is positioned at the position, downstream of the position, where the third pipeline (L3) is divided into the fourth pipeline (L4); a fifth control valve (K5) is arranged on the fourth pipeline (L4).

13. The flue gas treatment ammonia injection system of claim 8, wherein: a fourth control valve (K4) is arranged on the third pipeline (L3), and the fourth control valve (K4) is positioned at the position, downstream of the position, where the third pipeline (L3) is divided into the fourth pipeline (L4); a fifth control valve (K5) is arranged on the fourth pipeline (L4).

14. The flue gas treatment ammonia injection system of claim 12, wherein: the fourth control valve (K4) is adjusted so that the amount Q of the ammonia gas and the heat medium delivered to the first ammonia injection port (301) via the third pipe (L3)_DenitrationComprises the following steps:

adjusting the fifth control valve (K5) so that the ammonia gas and heat transported into the raw flue gas pipeline (L0) via the fourth pipeline (L4)Quantity Q of medium_{Desulfurization of}Comprises the following steps:

15. the flue gas treatment ammonia injection system of claim 13, wherein: the fourth control valve (K4) is adjusted so that the amount Q of the ammonia gas and the heat medium delivered to the first ammonia injection port (301) via the third pipe (L3)_DenitrationComprises the following steps:

the fifth control valve (K5) is adjusted so that the amount Q of ammonia and heat medium delivered via the fourth line (L4) into the raw flue gas line (L0)_{Desulfurization of}Comprises the following steps:

16. the flue gas treatment ammonia injection system of any one of claims 7, 9-10, 13-15, wherein: the system further comprises: a dilution fan (303); the dilution fan (303) is disposed in the sixth conduit (L6) downstream of the connection of the sixth conduit (L6) to the air bypass (L7).

17. The flue gas treatment ammonia injection system of claim 8, wherein: the system further comprises: a dilution fan (303); the dilution fan (303) is disposed in the sixth conduit (L6) downstream of the connection of the sixth conduit (L6) to the air bypass (L7).

18. The flue gas treatment ammonia injection system of claim 12, wherein: the system further comprises: a dilution fan (303); the dilution fan (303) is disposed in the sixth conduit (L6) downstream of the connection of the sixth conduit (L6) to the air bypass (L7).

19. The flue gas treatment ammonia injection system of claim 14, wherein: the system further comprises: a dilution fan (303); the dilution fan (303) is disposed in the sixth conduit (L6) downstream of the connection of the sixth conduit (L6) to the air bypass (L7).

20. The flue gas treatment ammonia injection system according to any one of claims 1-3, 5-7, 9-10, 13-15, 17-19, wherein: the fourth pipeline (L4) is communicated with the original smoke pipeline (L0) and specifically comprises the following steps: an eighth pipeline (L8) branched from the original flue gas pipeline (L0) is connected into the adsorption tower (2), and the fourth pipeline (L4) is communicated with the eighth pipeline (L8).

21. The flue gas treatment ammonia injection system of claim 4, wherein: the fourth pipeline (L4) is communicated with the original smoke pipeline (L0) and specifically comprises the following steps: an eighth pipeline (L8) branched from the original flue gas pipeline (L0) is connected into the adsorption tower (2), and the fourth pipeline (L4) is communicated with the eighth pipeline (L8).

22. The flue gas treatment ammonia injection system of claim 20, wherein: the position where the eighth pipe (L8) is connected to the adsorption tower (2) is located at the upper part of the adsorption tower (2).

23. The flue gas treatment ammonia injection system of claim 21, wherein: the position where the eighth pipe (L8) is connected to the adsorption tower (2) is located at the upper part of the adsorption tower (2).

24. The flue gas treatment ammonia injection system according to any one of claims 1-3, 5-7, 9-10, 13-15, 17-19, 21-23, wherein: the SCR denitration device of the denitration tower (1) is characterized in that the adsorption tower (2) is an activated carbon adsorption tower.

25. The flue gas treatment ammonia injection system of claim 4, wherein: the SCR denitration device of the denitration tower (1) is characterized in that the adsorption tower (2) is an activated carbon adsorption tower.

26. The flue gas treatment ammonia injection system of claim 24, wherein: m SCR denitration devices (101) and n CO catalytic oxidation layers (102) are arranged in the denitration tower (1), and the SCR denitration devices (101) and the CO catalytic oxidation layers (102) are arranged at intervals; wherein: m and n are each independently 1 to 5.

27. The flue gas treatment ammonia injection system of claim 25, wherein: m SCR denitration devices (101) and n CO catalytic oxidation layers (102) are arranged in the denitration tower (1), and the SCR denitration devices (101) and the CO catalytic oxidation layers (102) are arranged at intervals; wherein: m and n are each independently 1 to 5.

28. The flue gas treatment ammonia injection system of claim 26 or 27, wherein: m and n are each independently 2 to 4.