CN112403181A

CN112403181A - Flue gas desulfurization and denitrification treatment system and method

Info

Publication number: CN112403181A
Application number: CN201911069849.3A
Authority: CN
Inventors: 魏进超; 康建刚; 杨本涛; 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: 2021-02-26
Anticipated expiration: 2039-11-05
Also published as: CN112403181B

Abstract

The invention discloses a flue gas desulfurization and denitration treatment system and a method, wherein the flue gas desulfurization and denitration treatment system comprises an activated carbon adsorption tower, an activated carbon desorption tower, an air mixing chamber, a hot blast stove and an SCR (selective catalytic reduction) reactor; the air mixing chamber respectively introduces hot air generated by combustion of hot blast stove fuel and part of desulfurized flue gas desulfurized by the activated carbon adsorption tower to be uniformly mixed to form a heat medium, and the heat medium is used for realizing activated carbon thermal regeneration of the heating section of the activated carbon desorption tower and heating the flue gas needing denitration of the SCR system. The system and the method have the advantages of low investment cost, simple structure, strong adaptability and practicability, high control precision and obvious flue gas desulfurization and denitrification effects.

Description

Flue gas desulfurization and denitrification treatment system and method

Technical Field

The invention relates to a flue gas desulfurization and denitration technology, in particular to a flue gas desulfurization and denitration treatment system and method, and belongs to the technical field of flue gas purification.

Background

For industrial flue gas, especially for flue gas of sintering machine in steel industry, the flue gas desulfurization and denitration technology is a flue gas purification technology applied to chemical industry for generating multi-nitrogen oxide and sulfur oxide. Nitrogen oxides and sulfur oxides are one of the main sources of air pollution. The simultaneous desulfurization and denitration technology for flue gas is mostly in research and industrial demonstration stages at present, but because the simultaneous desulfurization and denitration can be realized in one set of system, particularly along with the simultaneous desulfurization and denitration of NO_XThe control standard is becoming more and more strict, and the desulfurization and denitrification technology is receiving increasing attention from various countries.

Flue gas desulfurization refers to the removal of Sulfur Oxides (SO) from flue gas or other industrial waste gases₂And SO₃). Currently, industrially used desulfurization methods include dry desulfurization, semi-dry desulfurization or wet desulfurization. Denitration of flue gas, i.e. the removal of NO produced_XReduction to N₂Thereby removing NO in the smoke_XThe method can be divided into wet denitration and dry denitration according to treatment processes. The flue gas denitration technology mainly comprises a dry method (selective catalytic reduction flue gas denitration, selective non-catalytic reduction denitration) and a wet method.

Currently, for an activated carbon + SCR flue gas purification system, since the heating section of the desorption tower needs to maintain a regeneration temperature of 400-460 ℃, the SCR system needs high-temperature gas (about 1000 ℃) to heat the desulfurized flue gas, and then the flue gas is conveyed to the SCR treatment system. If the air gas with the temperature of 400-460 ℃ is adopted, the smoke treatment amount of the SCR system is increased greatly, and meanwhile, the size of a hot blast stove system and pipelines is increased, so that the investment is increased. Therefore, the prior flue gas purification system adopting the activated carbon and SCR method generally adopts two sets of hot blast furnace systems. The two sets of hot blast furnace systems comprise two hot blast furnaces, two sets of instruments, a control system and the like, the investment is still high, the number of control points is large, and the control performance is poor, so that an integrated analysis tower and a heating system and method of flue gas need to be developed.

In addition, in the existing flue gas treatment process, the hot blast stove burns fuel, using air as combustion-supporting gas. The hot blast stove generates a certain amount of flue gas, and the generated flue gas contains pollutants such as nitrogen dioxide, nitric oxide and the like due to the combustion of fuel in the hot blast stove; in the prior art, gas generated by the hot blast stove is directly discharged to pollute air. Meanwhile, the hot blast stove adopts normal temperature air as combustion-supporting gas, and a large amount of fuel is consumed when the part of the combustion-supporting gas is heated to the temperature (generally 400-460 ℃) required by the heat exchange medium; that is to say the fuel in the hot blast stove, a part of which is required for heating the combustion-supporting gas, results in the need to consume more fuel and at the same time produce a greater amount of flue gas containing pollutants.

Disclosure of Invention

Aiming at the defects of the prior art, the fuel is burnt by a hot blast stove to about 1000 ℃ in the presence of combustion air and then enters a wind mixing chamber, meanwhile, part of flue gas is extracted from a flue and enters the wind mixing chamber to adjust the temperature of the mixed hot air in the wind mixing chamber to 360-500 ℃, then the flow of the hot air (a heat medium generated by the wind mixing chamber) entering a desorption tower is adjusted according to the heat required by the activation of the activated carbon of the desorption tower, and the flue gas discharged from the desorption tower is uniformly mixed with other flue gas (ensuring that all the flue gas is in the temperature range required by SCR catalysis) and then enters an SCR system for denitration treatment. On the premise of ensuring the heat required by the desorption tower, the flow rates of the fuel and the combustion-supporting air are determined by the required temperature of the flue gas of the SCR system, and are generally between 120 ℃ and 400 ℃.

According to a first embodiment of the present invention, a flue gas desulfurization and denitration treatment system is provided, which comprises an activated carbon adsorption tower, an activated carbon desorption tower, a wind mixing chamber, a hot blast stove and an SCR reactor. According to the trend of the flue gas, one side of the activated carbon adsorption tower is provided with a raw flue gas inlet, and the other side of the activated carbon adsorption tower is provided with a desulfurization flue gas outlet. And the desulfurization flue gas outlet is communicated to the gas inlet of the SCR reactor through a first pipeline. And the clean flue gas discharged by the reactor is discharged from a gas outlet of the SCR reactor. And a second pipeline is led out from the first pipeline and connected to an air inlet of the air mixing chamber. And the air inlet of the air mixing chamber is also connected with the hot blast stove through a third pipeline.

Preferably, the activated carbon desorption tower is sequentially provided with a heating section, an SRG section and a cooling section from top to bottom, the heating section is provided with a heating medium inlet and a heating medium outlet, the heating medium inlet is connected with the air outlet of the air mixing chamber through a fourth pipeline, and the heating medium outlet is connected with the first pipeline through a fifth pipeline.

Preferably, a sixth pipeline is led out from the air outlet of the air mixing chamber, the tail end of the sixth pipeline is connected to a fifth pipeline, and the fifth pipeline is communicated to the first pipeline.

Preferably, the system further comprises a GGH heat exchanger. And the air outlet of the SCR reactor is connected with an exhaust pipeline. The GGH heat exchanger is respectively connected with the first pipeline and the exhaust pipeline. And the flue gas desulfurized by the activated carbon adsorption tower is subjected to heat exchange by the GGH heat exchanger and then is conveyed to the air inlet of the SCR reactor. And the clean flue gas discharged by the SCR reactor is subjected to heat exchange by the GGH heat exchanger and then discharged through an exhaust pipeline. The position of the second pipeline leading out from the first pipeline is positioned at the upstream or the downstream of the connecting position of the GGH heat exchanger and the first pipeline.

Preferably, the activated carbon outlet of the activated carbon desorption tower is connected with the activated carbon inlet of the activated carbon adsorption tower through the first activated carbon conveying device according to the trend of the activated carbon. And an active carbon outlet of the active carbon adsorption tower is connected with an active carbon inlet of the active carbon desorption tower through a second active carbon conveying device. And/or

Preferably, the second pipeline is provided with a second fan, and the fifth pipeline is provided with a third fan. And/or

Preferably, the hot blast stove is further provided with a fuel pipe and a combustion-supporting air pipe.

Preferably, m SCR denitration devices and n CO catalytic oxidation layers are arranged in the SCR reactor, 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.

Preferably, the activated carbon desorption column is provided at an activated carbon inlet with a first flow rate detector and a first temperature detector. And a second flow rate detector and a second temperature detector are arranged on the first pipeline and between the second pipeline and the GGH heat exchanger. And a third temperature detector is arranged on the fifth pipeline. And a first flow regulating valve is arranged on the second pipeline, and a second flow regulating valve is arranged on the fuel pipe.

According to a second embodiment of the present invention, there is provided a flue gas desulfurization and denitration treatment method using the flue gas desulfurization and denitration treatment system according to the first embodiment, the method including the steps of:

1) according to the trend of flue gas, raw flue gas enters the activated carbon adsorption tower from raw flue gas entry via the admission line and carries out desulfurization treatment, and the desulfurization flue gas after the desulfurization is discharged from desulfurization flue gas outlet and is carried to the GGH heat exchanger through first pipeline and carries out the heat transfer intensification, and the desulfurization flue gas after accomplishing the heat transfer intensification carries to carry out denitration treatment in the SCR reactor, and the clean flue gas after accomplishing denitration treatment carries to the heat transfer cooling of GGH heat exchanger and then discharges through exhaust duct.

2) A second pipeline is led out from the first pipeline, part of smoke is led to the air mixing chamber through a second fan, the air mixing chamber is connected with the hot blast stove through a third pipeline, and the part of smoke led in from the first pipeline and hot air formed by burning of the hot blast stove are uniformly mixed in the air mixing chamber to form a hot medium.

3) The activated carbon desorption tower is sequentially provided with a heating section, an SRG section and a cooling section from top to bottom, the heating section is provided with a heating medium inlet and a heating medium outlet, the heating medium inlet is connected to the air mixing chamber through a fourth pipeline, the heating medium outlet is connected to the downstream of the first pipeline through a fifth pipeline, the heating medium in the air mixing chamber is conveyed to the first pipeline through the heating section under the action of a third fan to heat residual flue gas, and finally the heated flue gas is conveyed to the SCR reactor to be subjected to denitration treatment.

Preferably, the method further comprises a step 4): a sixth pipeline is led out from the air mixing chamber and connected with the fifth pipeline, part of the heat medium in the air mixing chamber is conveyed back to the first pipeline to heat the flue gas, and then the heated flue gas is conveyed to an SCR reactor (7) to be subjected to denitration treatment.

Preferably, the method further comprises step 5): and detecting the flow rate of the activated carbon at the activated carbon inlet of the activated carbon desorption tower by using a first flow detector to be q1, L/s. The temperature of the activated carbon at the activated carbon inlet of the activated carbon desorption tower is detected to be t1 and DEG C by the first temperature detector. And detecting the flow of the flue gas subjected to heat exchange by the GGH heat exchanger in the first pipeline as q2 and L/s by using a second flow detector. And detecting the temperature of the flue gas subjected to heat exchange by the GGH heat exchanger in the first pipeline to be t2 and DEG C by using a second temperature detector. The temperature required for the analysis of the activated carbon in the analysis tower is set to t3 and DEG C. The temperature required for denitration of the catalyst in the SCR reactor is set to t4 and DEG C. According to the heat balance principle, the heat required by the activated carbon desorption tower and the heat required by the temperature rise of the flue gas of the SCR reactor are both from the combustion of fuel in the hot blast stove:

q_{burning device}△H_{Burning device}Formula I.. formula I: C1 × q1(t3-t1) + C2 × q2(t4-t2).

Wherein: q. q.s_{Burning device}The input amount of fuel is L/s. Delta H_{Burning device}Is the heat of combustion of the fuel, J/L. C1 is the specific heat capacity of the activated carbon, J/(kg ℃). C2 is the specific heat capacity of the flue gas in the first pipeline, and J/(kg ℃).

Formula I is converted to:

q_{burning device}＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/△H_{Burning device}.., formula II.

By controlling the second flow regulating valve on the fuel pipe, the quantity of fuel delivered to the hot blast stove through the fuel pipe is q_{Burning device}。

Preferably, the temperature required for the heat medium in the air-mix chamber is set to t5℃. And a first flow regulating valve is arranged on the second pipeline, and the flow of flue gas in the second pipeline is regulated to q3 and L/s. A second flow regulating valve is arranged on the fuel pipe and used for regulating the input amount of fuel to be q_{Burning device}L/s. According to the heat balance principle, the heat required by the temperature rise of the flue gas entering the air mixing chamber through the second pipeline to t5 is derived from the heat released by the combustion of the fuel in the hot blast stove:

q_{burning device}△H_{Burning device}Formula III, C2 × q3(t5-t2).

In combination with formula I and formula III:

q3 ═ C1 q1(t3-t1) + C2 q2(t4-t2) ]/[ C2(t5-t2) ].

The first flow regulating valve is regulated, so that the smoke quantity of the smoke entering the air mixing chamber through the second pipeline is q 3.

Preferably, the fifth pipeline is provided with a third temperature detector, and the third temperature detector detects that the temperature of the flue gas in the fifth pipeline is t6 and DEG C. According to the heat balance principle, the heat required by the activated carbon desorption tower comes from the air mixing chamber and is conveyed to the heating medium in the desorption tower through a fourth pipeline:

c1 q1(t3-t1) C3 q4(t5-t6) … formula V.

Wherein: c3 is the specific heat capacity of the heating medium entering the fourth pipeline after being mixed in the air mixing chamber, and J/(kg) DEG C. q4 is the flow rate of the heating medium in the fourth pipe.

Formula V is converted to:

q4 ═ C1 q1(t3-t1) ]/[ C3(t5-t6) ] … formula VI.

The third fan is controlled so that the flow rate of the heating medium in the fourth pipe is q 4.

Preferably, in the hot blast furnace, the system heat loss coefficient is set to K1, and formula I is converted to:

K1*q_{burning device}△H_{Burning device}Formula VII, C1 × q1(t3-t1) + C2 × q2(t4-t2).

Formula II converts to:

q_{burning device}＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/[K1*△H_{Burning device}].., formula VIII.

In the air mixing chamber, the mixed heat loss coefficient of the hot air generated by the hot blast stove and the flue gas conveyed by the second pipeline is set to be K2, and then the formula III is converted into the following formula:

K2*K1*q_{burning device}△H_{Burning device}Formula IX (IX) C2 × q3(t5-t2).

Formula IV converts to:

q3 ═ K2 × K1 [ -C1 × q1(t3-t1) + C2 × q2(t4-t2) ]/[ C2(t5-t2) ].

In the heating section of the activated carbon desorption tower, the heat exchange coefficient of the heat medium and the activated carbon is set to be K3, and then the formula V is converted into:

c1 × q1(t3-t1) ═ K3 × K2 × K1 × C3 × q4(t5-t6) … formula XI.

Formula VI is converted to:

q4 ═ C1 q1(t3-t1) ]/[ K3K 2K 1C 3(t5-t6) ] … formula XII.

Wherein, K1 takes on the value: 90% -99%; k2 is 95-99%; k3 takes a value of 85% -95%.

In an actual working condition, after the active carbon in the active carbon adsorption tower finishes the treatment (mainly adsorption desulfurization) of the original flue gas, the active carbon adsorbing pollutants needs to be sent to the active carbon desorption tower for heating regeneration, the active carbon is recovered, and then the active carbon is continuously sent to the active carbon adsorption tower for adsorption desulfurization, and the process is circulated. The activated carbon desorption tower is sequentially divided into a heating section, an SRG section and a cooling section from top to bottom, the activated carbon adsorbing pollutants is mainly heated and regenerated in the heating section, and in order to achieve the optimal regeneration effect, the temperature of the heating section needs to be maintained at about 400-460 ℃ (the activated carbon burns due to overhigh temperature, further safety accidents occur, and the purpose of regenerating the activated carbon cannot be achieved due to insufficient temperature). Generally, the desulfurized flue gas obtained by subjecting the raw flue gas to desulfurization treatment by the activated carbon adsorption tower is further conveyed to the SCR reactor for denitration treatment, and the optimum temperature range of the denitration unit in the SCR reactor for denitration treatment of the desulfurized flue gas is about 120-400 ℃. The prior art generally adopts that a set of hot blast furnace system is connected to the outside of the heating section of the activated carbon desorption tower to provide heat for the heat regeneration of the activated carbon, and a set of hot blast furnace system is externally connected to heat the desulfurized flue gas before the desulfurized flue gas enters the SCR reactor. In the invention, a wind mixing chamber is arranged, and all hot air generated by fuel combustion in a hot air furnace and part of desulfurized flue gas are respectively introduced into the wind mixing chamber and are fully and uniformly mixed to form a new heat medium (the temperature range is about 400-. Then, conveying the residual heat medium in the air mixing chamber and the heat medium from the heating section of the activated carbon desorption tower to a desulfurization flue gas pipeline to be mixed with the residual desulfurization flue gas, and adjusting the temperature of the mixed flue gas to be in the optimal temperature range of denitration treatment; or part of the heat medium in the air mixing chamber is conveyed to the heating section of the activated carbon desorption tower to complete the heat regeneration of the activated carbon; and then conveying the part of heat medium from the heating section of the activated carbon desorption tower back to the desulfurization flue gas pipeline, and simultaneously leading out a branch pipeline from the air mixing chamber, and under the premise of ensuring the heat medium flow required by the heat regeneration of the activated carbon conveyed to the activated carbon desorption tower, completely conveying the rest heat medium and the heat medium after the heat regeneration of the activated carbon to the desulfurization flue gas pipeline (downstream position) to be mixed with the rest desulfurization flue gas, and adjusting the temperature of the mixed flue gas to be in the optimal temperature range of the denitration treatment. According to the method, heat sources do not need to be respectively and independently arranged on the active carbon desorption tower and the SCR reactor (namely, a plurality of independent hot blast furnace systems do not need to be arranged), so that the investment cost is greatly reduced, the number of control points is reduced, and the control performance of the system is improved.

In addition, the gas generated by the hot blast stove is high-temperature gas, generally about 1000 ℃, and then the high-temperature gas generated by the hot blast stove is mixed with the desulfurization flue gas to the temperature required by the analysis of the active carbon. Compared with the prior art, the combustion-supporting gas required by the hot blast stove is greatly reduced, the desulfurized flue gas is used as a part of the mixed gas, the heat in the desulfurized flue gas is fully utilized by utilizing the temperature condition that the desulfurized flue gas has the temperature of more than 120 ℃, and therefore the use of fuel is reduced.

More outstanding effect is that, by adopting the technical scheme of the invention, the flue gas generated by the fuel burned in the hot blast stove is mixed with the desulfurization flue gas through the air mixing chamber, and then is conveyed to the heating section of the activated carbon desorption tower to heat the activated carbon, and is conveyed back to the desulfurization flue gas conveying pipeline after being used for activated carbon desorption. According to the technical scheme, the desulfurized flue gas is used as the mixed heating medium, and the part needs to be treated by the SCR reactor. Firstly, the high-temperature condition of the flue gas after heat exchange is utilized for heating the temperature of the flue gas before entering the SCR treatment system (namely the desulfurized flue gas), so that heat resources are fully utilized; secondly, the method comprises the following steps: flue gas that produces in the hot-blast furnace passes through SCR processing system, and nitrogen oxide in the flue gas obtains the desorption through SCR system treatment back, utilizes the SCR processing system that itself has, handles the pollutant in the hot-blast furnace production flue gas simultaneously, has avoided the defect that hot-blast furnace produced the direct emission of flue gas among the prior art, has reduced the pollution to the environment.

In the invention, the GGH heat exchanger is arranged between the gas outlet of the SCR reactor and the clean flue gas exhaust pipeline, and the GGH heat exchanger is respectively connected with the desulfurization flue gas pipeline and the clean flue gas exhaust pipeline. And the flue gas desulfurized by the activated carbon adsorption tower is subjected to heat exchange and temperature rise by the GGH heat exchanger and then is conveyed to the air inlet of the SCR reactor. And the clean flue gas discharged by the SCR reactor is subjected to heat exchange by the GGH heat exchanger and then discharged through an exhaust pipeline. Generally, the clean flue gas after denitration by the SCR reactor has a high temperature (generally about 150-. According to the invention, the GGH heat exchanger is arranged, so that most of heat of the clean flue gas can be exchanged to the low-temperature desulfurized flue gas to improve the temperature of the desulfurized flue gas, and firstly, the emission temperature of the clean flue gas can be further reduced, and the environmental pollution is reduced; meanwhile, after the temperature of the desulfurized flue gas is increased, the consumption and time of fuel required by heating the desulfurized flue gas to the optimal temperature for SCR denitration treatment are reduced, and the heat is fully utilized.

In the invention, a first flow rate detector and a first temperature detector are arranged at an activated carbon inlet of the activated carbon desorption tower. And a second flow rate detector and a second temperature detector are arranged on the first pipeline and between the second pipeline and the GGH heat exchanger. The second pipeline is provided with a first flow regulating valve (for regulating and controlling the flow of the flue gas entering the air mixing chamber), and the fuel pipe is provided with a second flow regulating valve (for regulating the flow of the total fuel required by the system). The system aims to monitor the working state of each position point in real time, ensure the safe and stable operation of the system, simultaneously automatically and accurately control the feeding of fuel and the distribution of hot media in a wind mixing chamber after being calculated by a formula according to the data value monitored by each position point, and greatly improve the system efficiency on the premise of ensuring the stable and effective operation of the system.

In the flue gas desulfurization and denitration system, the optimal working states of the heating section of the desorption tower and the SCR reactor are ensured by adding an external heat source to supplement heat, namely, the regeneration of the activated carbon in the heating section of the activated carbon desorption tower needs to be carried out by introducing a heat medium to heat the activated carbon, and the low-temperature desulfurization flue gas needs to be heated to the optimal denitration temperature in the SCR denitration process, so that the heat required by the two working sections is the heat needed to be supplemented by the whole external heat source (namely, the heat generated by fuel combustion in an external hot blast stove). In the prior art, hot blast furnace systems are respectively arranged outside two working sections, so that the investment cost is high, the operation intensity is high, and the energy consumption is high. Therefore, in the present invention, in order to achieve the purpose of saving energy and prevent the heat generated by the external heat source from overflowing, which may threaten the system safety, the heat output by the external heat source needs to be regulated, that is, the input amount of the fuel in the hot blast stove needs to be strictly controlled: detecting the flow of the activated carbon at an activated carbon inlet of the activated carbon desorption tower by using a first flow detector to be q1, L/s; detecting the temperature of the activated carbon at an activated carbon inlet of the activated carbon desorption tower by a first temperature detector to be t1℃; detecting the flow of the flue gas subjected to heat exchange by the GGH heat exchanger in the first pipeline to be q2, L/s by using a second flow detector; detecting the temperature of the flue gas in the first pipeline after heat exchange of the GGH heat exchanger by using a second temperature detector to be t2℃; setting the temperature required by the analysis of the activated carbon in the analysis tower to t3 (about 400-; setting the temperature required by the denitration of the catalyst in the SCR reactor to t4 (about 120 ℃ C.), ° C; according to the heat balance principle, the heat required by the activated carbon desorption tower and the heat required by the temperature rise of the flue gas of the SCR reactor are both from the combustion of fuel in the hot blast stove:

Wherein: q. q.s_{Burning device}The input amount of fuel is L/s. Delta H_{Burning device}As heat of combustion of fuelJ/L. C1 is the specific heat capacity of the activated carbon, J/(kg ℃). C2 is the specific heat capacity of the flue gas in the first pipeline, and J/(kg ℃).

Formula I is converted to:

The second flow control valve on the fuel line can then be adjusted in real time by the calculated value of formula II such that the amount of fuel delivered through the fuel line to the hot blast stove is the calculated value q of formula II_{Burning device}。

In the invention, under the normal condition, the temperature of hot air heat output by the hot blast stove is as high as about 1000 ℃, the regeneration temperature of the activated carbon in the activated carbon desorption tower only needs about 400-460 ℃, the desorption tower can be damaged when the temperature is too high, and the purpose of the activated carbon thermal regeneration can not be achieved when the temperature is not enough. Therefore, the hot air output by the hot blast stove needs to be blended with cold air to reduce the temperature to form a heat medium with the temperature of 400- Left and right; meanwhile, in consideration of the fact that the input quantity of combustion air of the hot blast stove is far smaller than the quantity of low-temperature desulfurization flue gas input into the air mixing chamber in actual working conditions, the heat consumed when the combustion air is heated to the temperature of the heat medium is negligible, and therefore the required temperature of the heat medium in the air mixing chamber is set to t5 (about 400-; a first flow regulating valve is arranged on the second pipeline, and the flow of flue gas in the second pipeline is regulated to q3, L/s; the fuelThe material pipe is provided with a second flow regulating valve for regulating the input amount of fuel to q_{Burning device}L/s; according to the heat balance principle, the heat required by the temperature rise of the flue gas entering the air mixing chamber through the second pipeline to t5 is derived from the heat released by the combustion of the fuel in the hot blast stove:

q_{burning device}△H_{Burning device}Formula III, C2 × q3(t5-t2).

In combination with formula I and formula III:

q3 ═ C1 q1(t3-t1) + C2 q2(t4-t2) ]/[ C2(t5-t2) ].

The first flow regulating valve can then be further regulated in real time by the calculated value of formula IV, so that the desulfurized flue gas amount of the flue gas entering the air mixing chamber through the second pipeline is the calculated value q3 of formula IV.

In the invention, considering that the total flow of the heat medium in the air mixing chamber is far greater than the total flow of the heat medium required by the heat regeneration of the activated carbon in the activated carbon desorption tower, the residual heat medium is conveyed into the desulfurization flue gas pipeline through the external discharge pipeline (the sixth pipeline) on the premise of ensuring the amount of the heat medium required by the heat regeneration of the activated carbon in the activated carbon desorption tower to heat the desulfurization flue gas by leading out the branch external discharge pipeline (the sixth pipeline) on the air mixing chamber; accomplish the hot medium of exhaust behind the hot regeneration of active carbon in the active carbon desorption tower, because its temperature is far greater than desulfurization flue gas temperature, the principal ingredients of this part hot medium derives from desulfurization flue gas simultaneously, consequently this part hot medium need carry back to desulfurization flue gas pipeline in the heating low temperature desulfurization flue gas back reentrant SCR reactor carries out denitration treatment again. In order to reasonably distribute the heat medium in the air mixing chamber, the third temperature detector is arranged on the fifth pipeline, and the temperature of the smoke in the fifth pipeline detected by the third temperature detector is t6 and DEG C. According to the heat balance principle, the heat required by the activated carbon desorption tower comes from the air mixing chamber and is conveyed to the heating medium in the desorption tower through a fourth pipeline:

c1 q1(t3-t1) C3 q4(t5-t6) … formula V.

Formula V is converted to:

q4 ═ C1 q1(t3-t1) ]/[ C3(t5-t6) ] … formula VI.

The third fan may then be further adjusted in real time by the calculated value of formula VI such that the flow rate of the heating medium in the fourth conduit that is delivered to the heating section of the activated carbon desorption tower is the calculated value q4 of formula VI. And the residual heat medium in the air mixing chamber is conveyed to the desulfurization flue gas pipeline through an external discharge pipeline (a sixth pipeline).

In the invention, because system heat losses exist in the fuel combustion of the system hot blast stove, the mixing of high-temperature hot air and low-temperature flue gas in the air mixing chamber into a heat medium, the heat exchange between the heat medium and the activated carbon in the heating section of the desorption tower and the like, the heat losses can be obtained by calculation according to the actual working conditions, and therefore, the heat released by the fuel combustion in the hot blast stove actually has certain heat losses, namely the fuel input q calculated by the formula II_{Burning device}And certain errors exist between the actual fuel input amount, between the desulfurization flue gas amount q3 of the flue gas entering the air mixing chamber through the second pipeline and the actual desulfurization flue gas amount to be introduced, which are calculated by the formula IV, and between the flow rate q4 of the heat medium conveyed to the heating section of the analysis tower and the actual flow rate of the heat medium to be conveyed, which are calculated by the formula VI. Therefore, under the premise of considering the system heat loss, in the hot blast stove, the coefficient of heat loss of fuel combustion is set to be K1, and the formula I is converted into:

K1*q_{burning device}△H_{Burning device}Formula VII, (VII) C1 q1(t3-t1) + C2 q2(t4-t 2);

formula II converts to:

K2*K1*q_{burning device}△H_{Burning device}＝C2*q3(t5-t2)...IX。

Formula IV converts to:

q3 ═ K2 × K1 [ -C1 × q1(t3-t1) + C2 × q2(t4-t2) ]/[ C2(t5-t2) ].

c1 × q1(t3-t1) ═ K3 × K2 × K1 × C3 × q4(t5-t6) … formula XI.

Formula VI is converted to:

q4 ═ C1 q1(t3-t1) ]/[ K3K 2K 1C 3(t5-t6) ] … formula XII.

Then the actual fuel input quantity q to be put into the hot blast stove can be accurately calculated in real time through the formula VIII_{Burning device}Then accurately calculating the flow of the desulfurized flue gas to be conveyed to the air mixing chamber as q3 by a formula X in real time; the flow rate of the heat medium to be fed to the desorption column is precisely calculated as q4 by formula XII in real time.

In a preferred embodiment of the present invention, the SCR reactor comprises an SCR denitration device and a CO catalytic oxidation layer. Carbon monoxide components existing in (or containing) the flue gas are utilized, carbon dioxide is generated by utilizing the reaction of the carbon monoxide and oxygen, the exothermic reaction is realized, the carbon monoxide in the flue gas is converted into the carbon dioxide through a carbon monoxide treatment system, and the heat released by the reaction is used for heating the flue gas, so that the effect of heating the flue gas after desulfurization is realized; meanwhile, the carbon monoxide in the flue gas is removed, and the pollution of the carbon monoxide in the flue gas to the environment is avoided.

In the invention, the desulfurized flue gas is treated by the CO catalytic oxidation layer, carbon monoxide in the desulfurized flue gas is subjected to conversion reaction (namely, the carbon monoxide is combusted to generate carbon dioxide), and the released heat is directly absorbed by the flue gas, so that the effect of temperature rise is achieved, the subsequent denitration reaction is facilitated, and the denitration efficiency is improved. The method fully utilizes the carbon monoxide in the flue gas, utilizes the heat emitted in the process of converting the carbon monoxide into the carbon dioxide to achieve the purpose of raising the temperature of the flue gas for subsequent second denitration treatment, saves the use of fuel, treats the carbon monoxide in the flue gas, reduces the pollution of the flue gas to the environment, and weakens or even avoids the secondary pollution in the flue gas treatment process.

In the present invention, the height of the activated carbon adsorption column is 50 to 70 m.

In the present invention, the height of the activated carbon desorption column is 40 to 60 m.

In the present invention, the height of the SCR reactor is 30 to 40 m.

Compared with the prior art, the invention has the following beneficial technical effects:

1) the heating system and the method for heating and denitrating the activated carbon in the heating section of the integrated activated carbon desorption tower and the desulfurization flue gas of the SCR reactor are developed, the number of hot blast furnace systems, corresponding instrument control systems and the like are reduced, the number of control points is reduced, the investment cost is reduced, and the capability of accurately controlling the systems is improved.

2) The method can accurately calculate the heat consumption of the system, further accurately control the input of the fuel, save energy, and simultaneously reasonably control the supplement amount of the heat of the external heat source, effectively ensure the safety of the system and improve the production efficiency.

3) The system and the method have the advantages of low investment cost, simple structure, strong adaptability and practicability, high control precision and obvious flue gas desulfurization and denitrification effects.

Drawings

FIG. 1 is a structural diagram of a flue gas desulfurization and denitrification treatment system;

FIG. 2 is a structural diagram of a flue gas desulfurization and denitrification treatment system with an external discharge branch pipe of a mixed air chamber;

FIG. 3 is a structural diagram of a flue gas desulfurization and denitrification treatment system provided with a detection device;

FIG. 4 is a structural diagram of a flue gas desulfurization and denitrification treatment system with an air mixing chamber external discharge branch pipe and a detection device.

Reference numerals: 1: an activated carbon adsorption tower; 101: a raw flue gas inlet; 102: a desulfurized flue gas outlet; 2: an activated carbon desorption tower; 201: a heating section; 202: an SRG segment; 203: a cooling section; 20101: a heating medium inlet; 20102: a heating medium outlet; 3: a wind mixing chamber; 4: a hot blast stove; 401: a fuel tube; 402: a combustion-supporting air duct; 5: a GGH heat exchanger; 6: an exhaust duct; 7: an SCR reactor; 701: an SCR denitration device; 702: a CO catalytic oxidation layer; 8: an air intake duct; 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: a second activated carbon delivery device; l8: a first activated carbon delivery device; f1: a first fan; f2: a second fan; f3: a third fan; f4: a fourth fan; q1: a first flow detector; q2: a second flow rate detector; t1: a first temperature detector; t2: a second temperature detector; t3: a third temperature detector; m1: a first flow regulating valve; m2: a second flow regulating valve.

Detailed Description

The technical solution of the present invention is illustrated below, and the claimed scope of the present invention includes, but is not limited to, the following examples.

A flue gas desulfurization and denitration treatment system comprises an activated carbon adsorption tower 1, an activated carbon desorption tower 2, a wind mixing chamber 3, a hot blast stove 4 and an SCR reactor 7. According to the trend of the flue gas, one side of the activated carbon adsorption tower 1 is provided with a raw flue gas inlet 101, and the other side is provided with a desulfurization flue gas outlet 102. The sweet flue gas outlet 102 is communicated to the air inlet of the SCR reactor 7 through a first pipeline L1. And the clean flue gas discharged from the SCR reactor 7 is discharged from a gas outlet of the SCR reactor 7. The first pipeline L1 is led out from the second pipeline L2 and is connected to the air inlet of the air mixing chamber 3. The air inlet of the air mixing chamber 3 is also connected with the hot blast stove 4 through a third pipeline L3.

Preferably, the activated carbon desorption tower 2 is sequentially provided with a heating section 201, an SRG section 202 and a cooling section 203 from top to bottom, the heating section 201 is provided with a heating medium inlet 20101 and a heating medium outlet 20102, the heating medium inlet 20101 is connected with the air outlet of the air mixing chamber 3 through a fourth pipeline L4, and the heating medium outlet 20102 is connected with the first pipeline L1 through a fifth pipeline L5.

Preferably, the air outlet of the air mixing chamber 3 is led out by a sixth pipeline L6, the end of the sixth pipeline L6 is connected to a fifth pipeline L5, and the fifth pipeline L5 is communicated to the first pipeline L1.

Preferably, the system further comprises a GGH heat exchanger 5. The air outlet of the SCR reactor 7 is connected with an exhaust pipeline 6. The GGH heat exchanger 5 is connected to the first pipe L1 and the exhaust pipe 6, respectively. The flue gas desulfurized by the activated carbon adsorption tower 1 is subjected to heat exchange by the GGH heat exchanger 5 and then is conveyed to the air inlet of the SCR reactor 7. And the clean flue gas discharged from the SCR reactor 7 is subjected to heat exchange by the GGH heat exchanger 5 and then discharged through the exhaust pipeline 6. The position where the second pipe L2 exits from the first pipe L1 is upstream or downstream of the position where the GGH heat exchanger 5 is connected to the first pipe L1.

Preferably, the activated carbon outlet of the activated carbon desorption tower 2 is connected to the activated carbon inlet of the activated carbon adsorption tower 1 through the first activated carbon transfer device L8 according to the trend of the activated carbon. And an activated carbon outlet of the activated carbon adsorption tower 1 is connected with an activated carbon inlet of the activated carbon desorption tower 2 through a second activated carbon conveying device L7. And/or

Preferably, a second fan F2 is disposed on the second pipeline L2, and a third fan F3 is disposed on the fifth pipeline L5. And/or

Preferably, the hot blast stove 4 is further provided with a fuel pipe 401 and a combustion-supporting air pipe 402.

Preferably, m SCR denitration devices 701 and n CO catalytic oxidation layers 702 are arranged in the SCR reactor 7, and the SCR denitration devices 701 and the CO catalytic oxidation layers 702 are arranged at intervals. Wherein: m and n are each independently 1 to 5, preferably 2 to 4.

Preferably, a first flow rate meter Q1 and a first temperature meter T1 are provided at an activated carbon inlet of the activated carbon desorption column 2. A second flow rate meter Q2 and a second temperature meter T2 are provided on the first pipeline L1 between the second pipeline L2 and the GGH heat exchanger 5. And a third temperature detector T3 is arranged on the fifth pipeline L5. A first flow regulating valve M1 is provided on the second pipe L2, and a second flow regulating valve M2 is provided on the fuel pipe 401.

Example 1

As shown in fig. 1, a flue gas desulfurization and denitration treatment system comprises an activated carbon adsorption tower 1, an activated carbon desorption tower 2, a wind mixing chamber 3, a hot blast stove 4 and an SCR reactor 7. According to the trend of the flue gas, one side of the activated carbon adsorption tower 1 is provided with a raw flue gas inlet 101, and the other side is provided with a desulfurization flue gas outlet 102. The sweet flue gas outlet 102 is communicated to the air inlet of the SCR reactor 7 through a first pipeline L1. And the clean flue gas discharged from the SCR reactor 7 is discharged from a gas outlet of the SCR reactor 7. The first pipeline L1 is led out from the second pipeline L2 and is connected to the air inlet of the air mixing chamber 3. The air inlet of the air mixing chamber 3 is also connected with the hot blast stove 4 through a third pipeline L3.

The activated carbon desorption tower 2 is sequentially provided with a heating section 201, an SRG section 202 and a cooling section 203 from top to bottom, the heating section 201 is provided with a heating medium inlet 20101 and a heating medium outlet 20102, the heating medium inlet 20101 is connected with an air outlet of the air mixing chamber 3 through a fourth pipeline L4, and the heating medium outlet 20102 is connected with a first pipeline L1 through a fifth pipeline L5.

Example 2

Example 1 is repeated, as shown in fig. 2, except that a sixth pipeline L6 is further led out from the air outlet of the air mixing chamber 3, the end of the sixth pipeline L6 is connected to a fifth pipeline L5, and the fifth pipeline L5 is connected to the first pipeline L1.

Example 3

Example 2 is repeated except that the system further comprises a GGH heat exchanger 5. The air outlet of the SCR reactor 7 is connected with an exhaust pipeline 6. The GGH heat exchanger 5 is connected to the first pipe L1 and the exhaust pipe 6, respectively. The flue gas desulfurized by the activated carbon adsorption tower 1 is subjected to heat exchange by the GGH heat exchanger 5 and then is conveyed to the air inlet of the SCR reactor 7. And the clean flue gas discharged from the SCR reactor 7 is subjected to heat exchange by the GGH heat exchanger 5 and then discharged through the exhaust pipeline 6. The position where the second pipe L2 exits from the first pipe L1 is downstream of the position where the GGH heat exchanger 5 is connected to the first pipe L1.

Example 4

Example 3 is repeated, and the activated carbon outlet of the activated carbon desorption tower 2 is connected with the activated carbon inlet of the activated carbon adsorption tower 1 through the first activated carbon conveying device L8 according to the trend of the activated carbon. And an activated carbon outlet of the activated carbon adsorption tower 1 is connected with an activated carbon inlet of the activated carbon desorption tower 2 through a second activated carbon conveying device L7.

Example 5

Example 4 is repeated except that the second duct L2 is provided with a second fan F2.

Example 6

Example 5 is repeated except that a third fan F3 is provided on the fifth duct L5.

Example 7

Example 6 is repeated, except that the hot blast stove 4 is also provided with a fuel pipe 401 and a combustion-supporting air pipe 402.

Example 8

Example 7 is repeated, except that 2

SCR denitration devices

701 and 2 CO catalytic oxidation layers 702 are arranged in the SCR reactor 7, and the SCR denitration devices 701 and the CO catalytic oxidation layers 702 are arranged at intervals.

Example 9

Example 8 was repeated, and as shown in fig. 3, the activated carbon inlet of the activated carbon desorption column 2 was provided with a first flow rate meter Q1 and a first temperature meter T1. A second flow rate meter Q2 and a second temperature meter T2 are provided on the first pipeline L1 between the second pipeline L2 and the GGH heat exchanger 5. And a third temperature detector T3 is arranged on the fifth pipeline L5. A first flow regulating valve M1 is provided on the second pipe L2, and a second flow regulating valve M2 is provided on the fuel pipe 401.

Effect example 1

The flue gas desulfurization and denitration treatment system in embodiment 9 is adopted to perform desulfurization and denitration treatment on flue gas, and the amount of raw flue gas to be treated is 184.37 ten thousand meters under the condition of no shutdown for 24 hours by taking sintering flue gas as an example³The gas consumption is 1.28 ten thousand meters³。

Comparative example 1

The system of the double hot blast furnaces in the prior art is adopted to carry out desulfurization and denitrification treatment on the sintering flue gas from the same source in the effect example 1, and the raw flue gas treatment amount is 180.52 ten thousand meters under the condition of no shutdown for 24 hours³The gas consumption is 1.53 ten thousand meters³。

Claims

1. The utility model provides a flue gas desulfurization denitration treatment system which characterized in that: the system comprises an active carbon adsorption tower (1), an active carbon desorption tower (2), an air mixing chamber (3), a hot blast stove (4) and an SCR reactor (7); according to the trend of the flue gas, one side of the activated carbon adsorption tower (1) is provided with a raw flue gas inlet (101), and the other side is provided with a desulfurized flue gas outlet (102); the desulfurized flue gas outlet (102) is communicated to an air inlet of the SCR reactor (7) through a first pipeline (L1); the clean flue gas discharged from the SCR reactor (7) is discharged from a gas outlet of the SCR reactor (7); a second pipeline (L2) is led out of the first pipeline (L1) and is connected to an air inlet of the air mixing chamber (3); the air inlet of the air mixing chamber (3) is also connected with a hot blast stove (4) through a third pipeline (L3);

the activated carbon desorption tower (2) is sequentially provided with a heating section (201), an SRG section (202) and a cooling section (203) from top to bottom, a heating medium inlet (20101) and a heating medium outlet (20102) are arranged on the heating section (201), the heating medium inlet (20101) is connected with an air outlet of the air mixing chamber (3) through a fourth pipeline (L4), and the heating medium outlet (20102) is connected with a first pipeline (L1) through a fifth pipeline (L5).

2. The system of claim 1, wherein: a sixth pipeline (L6) is led out from the air outlet of the air mixing chamber (3), the tail end of the sixth pipeline (L6) is connected to a fifth pipeline (L5), and the fifth pipeline (L5) is communicated to the first pipeline (L1).

3. The system of claim 2, wherein: the system further comprises a GGH heat exchanger (5); the air outlet of the SCR reactor (7) is connected with an exhaust pipeline (6); the GGH heat exchanger (5) is respectively connected with a first pipeline (L1) and an exhaust pipeline (6); the flue gas desulfurized by the activated carbon adsorption tower (1) is subjected to heat exchange by the GGH heat exchanger (5) and then is conveyed to the air inlet of the SCR reactor (7); clean flue gas discharged by the SCR reactor (7) is subjected to heat exchange by the GGH heat exchanger (5) and then discharged by the exhaust pipeline (6); the position where the second pipeline (L2) is led out from the first pipeline (L1) is upstream or downstream of the position where the GGH heat exchanger (5) is connected with the first pipeline (L1).

4. The system according to any one of claims 1-3, wherein: according to the trend of the activated carbon, an activated carbon outlet of the activated carbon desorption tower (2) is connected with an activated carbon inlet of the activated carbon adsorption tower (1) through a first activated carbon conveying device (L8); an activated carbon outlet of the activated carbon adsorption tower (1) is connected with an activated carbon inlet of the activated carbon desorption tower (2) through a second activated carbon conveying device (L7); and/or

A second fan (F2) is arranged on the second pipeline (L2), and a third fan (F3) is arranged on the fifth pipeline (L5); and/or

The hot blast stove (4) is also provided with a fuel pipe (401) and a combustion-supporting air pipe (402).

5. The system according to any one of claims 1-4, wherein: m SCR denitration devices (701) and n CO catalytic oxidation layers (702) are arranged in the SCR reactor (7), and the SCR denitration devices (701) and the CO catalytic oxidation layers (702) are arranged at intervals; wherein: m and n are each independently 1 to 5, preferably 2 to 4.

6. The system according to any one of claims 3-5, wherein: a first flow rate detector (Q1) and a first temperature detector (T1) are arranged at an activated carbon inlet of the activated carbon desorption tower (2); a second flow rate detector (Q2) and a second temperature detector (T2) are arranged on the first pipeline (L1) and between the second pipeline (L2) and the GGH heat exchanger (5); a third temperature detector (T3) is arranged on the fifth pipeline (L5); and a first flow regulating valve (M1) is arranged on the second pipeline (L2), and a second flow regulating valve (M2) is arranged on the fuel pipe (401).

7. The flue gas desulfurization and denitration treatment method using the flue gas desulfurization and denitration treatment system according to any one of claims 1 to 6, characterized in that: the method comprises the following steps:

1) according to the trend of flue gas, raw flue gas enters an activated carbon adsorption tower (1) from a raw flue gas inlet (101) through an air inlet pipeline (8) for desulfurization treatment, the desulfurized flue gas after desulfurization is discharged from a desulfurized flue gas outlet (102) and is conveyed to a GGH heat exchanger (5) through a first pipeline (L1) for heat exchange and temperature rise, the desulfurized flue gas after heat exchange and temperature rise is conveyed to an SCR reactor (7) for denitration treatment, and clean flue gas after denitration treatment is conveyed to the GGH heat exchanger (5) for heat exchange and temperature reduction and then is discharged through an exhaust pipeline (6);

2) a second pipeline (L2) is led out of the first pipeline (L1) and leads part of the smoke to the air mixing chamber (3) through a second fan (F2), the air mixing chamber (3) is connected with the hot blast stove (4) through a third pipeline (L3), and part of the smoke led in from the first pipeline (L1) and hot gas formed by combustion of the hot blast stove (4) are uniformly mixed in the air mixing chamber (3) to form a hot medium;

3) the activated carbon desorption tower (2) is sequentially provided with a heating section (201), an SRG section (202) and a cooling section (203) from top to bottom, a heating medium inlet (20101) and a heating medium outlet (20102) are arranged on the heating section (201), the heating medium inlet (20101) is connected to the air mixing chamber (3) through a fourth pipeline (L4), the heating medium outlet (20102) is connected to the downstream of the first pipeline (L1) through a fifth pipeline (L5), the heating medium in the air mixing chamber (3) is conveyed to the first pipeline (L1) through the heating section (201) under the action of a third fan (F3) to heat residual flue gas, and finally the heated flue gas is conveyed to the SCR reactor (7) to be subjected to denitration treatment.

8. The method of claim 7, wherein: the method also comprises a step 4): a sixth pipeline (L6) is led out from the air mixing chamber (3) and connected with a fifth pipeline (L5), part of the heat medium in the air mixing chamber (3) is conveyed back into the first pipeline (L1) to heat the flue gas, and then the heated flue gas is conveyed into the SCR reactor (7) to be denitrated.

9. The method according to claim 7 or 8, characterized in that: the method further comprises step 5): detecting the flow rate of the activated carbon at the activated carbon inlet of the activated carbon desorption tower (2) to be Q1, L/s by a first flow detector (Q1); detecting the temperature of the activated carbon at an activated carbon inlet of the activated carbon desorption tower (2) to be T1℃ by a first temperature detector (T1); detecting the flow of the flue gas subjected to heat exchange by the GGH heat exchanger (5) in the first pipeline (L1) to be Q2 and L/s by using a second flow detector (Q2); detecting the temperature of the flue gas subjected to heat exchange by the GGH heat exchanger (5) in the first pipeline (L1) to be T2 and DEG C by using a second temperature detector (T2); setting the temperature required by the analysis of the activated carbon in the analysis tower (2) to t3 and DEG C; setting the temperature t4 and DEG C required by denitration of the catalyst in the SCR reactor (7); a second flow regulating valve (M2) is arranged on the fuel pipe (401) and used for regulating the input amount of fuel to be q_{Burning device}L/s; according to the heat balance principle, the heat required by the active carbon desorption tower (2) and the temperature rise required by the flue gas of the SCR reactor (7)The heat is all from the combustion of fuel in the hot blast stove:

q_{burning device}△H_{Burning device}Formula I,. C1 × q1(t3-t1) + C2 × q2(t4-t 2);

wherein: q. q.s_{Burning device}The input amount of fuel, L/s; delta H_{Burning device}Is the heat of combustion of the fuel, J/L; c1 is the specific heat capacity of the activated carbon, J/(kg ℃); c2 is the specific heat capacity of the flue gas in the first pipeline (L1), J/(kg ℃);

formula I is converted to:

q_{burning device}＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/△H_{Burning device}.., formula II;

the amount of fuel delivered to the hot blast stove (4) through the fuel pipe (401) is q by controlling a second flow regulating valve (M2) on the fuel pipe (401)_{Burning device}。

10. The method of claim 9, wherein: setting the temperature required by the hot medium in the air mixing chamber (3) to t5 and DEG C; a first flow regulating valve (M1) is arranged on the second pipeline (L2), and the flow of flue gas in the second pipeline (L2) is regulated to be q3 and L/s; according to the heat balance principle, the heat required for raising the temperature of the flue gas entering the air mixing chamber (3) through the second pipeline (L2) to t5 is derived from the heat released by the combustion of fuel in the hot blast stove (4):

q_{burning device}△H_{Burning device}Formula III,. C2 × q3(t5-t 2);

in combination with formula I and formula III:

q3 ═ C1 q1(t3-t1) + C2 q2(t4-t2) ]/[ C2(t5-t2) ]. formula IV;

the flue gas quantity of the flue gas entering the air mixing chamber (3) through the second pipeline (L2) is q3 by adjusting the first flow regulating valve (M1).

11. The method of claim 10, wherein: a third temperature detector (T3) is arranged on the fifth pipeline (L5), and the third temperature detector (T3) detects that the temperature of the flue gas in the fifth pipeline (L5) is T6 and DEG C; according to the heat balance principle, the heat required by the activated carbon desorption tower (2) is derived from a heating medium which is conveyed into the desorption tower (2) from a wind mixing chamber (3) through a fourth pipeline (L4):

c1 q1(t3-t1) C3 q4(t5-t6) … formula V;

wherein: c3 is the specific heat capacity of the heating medium entering the fourth pipeline (L4) after being mixed in the air mixing chamber (3), J/(kg ℃); q4 is the flow rate of the heating medium in the fourth line (L4);

formula V is converted to:

q4 ═ C1 q1(t3-t1) ]/[ C3(t5-t6) ] … formula VI;

the third fan (F3) was controlled so that the flow rate of the heating medium in the fourth piping (L4) was q 4.

12. The method of claim 10, wherein: in the hot blast stove (4), the heat loss coefficient of fuel combustion is set to be K1, and the formula I is converted into the following formula:

formula II converts to:

q_{burning device}＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/[K1*△H_{Burning device}].., formula VIII;

in the air mixing chamber (3), the mixed heat loss coefficient of the hot air generated by the hot blast stove (4) and the flue gas conveyed by the second pipeline (L2) is set to be K2, and then the formula III is converted into the following formula:

K2*K1*q_{burning device}△H_{Burning device}＝C2*q3(t5-t2)...IX；

Formula IV converts to:

q3 ═ K2 × K1 [ -C1 × q1(t3-t1) + C2 × q2(t4-t2) ]/[ C2(t5-t2) ].

In the heating section (201) of the activated carbon analysis tower (2), if the heat exchange coefficient between the heat medium and the activated carbon is set to be K3, the formula V is converted into:

c1 × q1(t3-t1) ═ K3 × K2 × K1 × C3 × q4(t5-t6) … formula XI;

formula VI is converted to:

q4 ═ C1 q1(t3-t1) ]/[ K3K 2K 1C 3(t5-t6) ] … formula XII;