CN112403179B - Shunting type flue gas desulfurization and denitrification treatment system and method - Google Patents

Shunting type flue gas desulfurization and denitrification treatment system and method Download PDF

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CN112403179B
CN112403179B CN201911069819.2A CN201911069819A CN112403179B CN 112403179 B CN112403179 B CN 112403179B CN 201911069819 A CN201911069819 A CN 201911069819A CN 112403179 B CN112403179 B CN 112403179B
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flue gas
pipeline
activated carbon
mixing chamber
air mixing
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CN112403179A (en
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刘昌齐
魏进超
叶恒棣
康建刚
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Zhongye Changtian International Engineering Co Ltd
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    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0454—Controlling adsorption
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
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    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
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    • B01D2259/00—Type of treatment
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    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
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Abstract

The invention discloses a shunting flue gas desulfurization and denitration treatment system and a method, wherein the shunting 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 uniformly mixes hot air generated by combustion of hot blast stove fuel with part of desulfurized flue gas desulfurized by the activated carbon adsorption tower 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 required to be denitrated by 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

Shunting type flue gas desulfurization and denitrification treatment system and method
Technical Field
The invention relates to a flue gas desulfurization and denitrification technology, in particular to a shunting type flue gas desulfurization and denitrification 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 denitrification technology for flue gas is mostly in research and industrial demonstration stages at present, but the simultaneous desulfurization and denitrification technology is in a set systemThe system can realize desulfurization and denitrification at the same time, especially along with NOXThe 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 producedXReduction to N2Thereby removing NO in the smokeXThe 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 combustion of 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 invention comprises the steps that fuel gas enters an air mixing chamber after being combusted to about 1000 ℃ in a hot blast stove in the presence of air, meanwhile, part of flue gas is extracted from a flue and enters the air mixing chamber, the temperature of hot air in the air mixing chamber is adjusted to 360-500 ℃, and then the flow of the hot air (a heat medium generated in the air mixing chamber) entering an analytical tower is adjusted according to the heat required by the activation of active carbon of the analytical tower; and (3) fully mixing the flue gas discharged from the desorption tower, the residual hot flue gas in the air mixing chamber and the low-temperature flue gas in the desulfurization flue gas pipeline (ensuring that the temperature of the mixed flue gas is in the temperature range required by SCR catalysis), and then conveying the mixed flue gas to an SCR system for 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 split-flow flue gas desulfurization and denitrification treatment system is provided, which includes an activated carbon adsorption tower, an activated carbon desorption tower, a hot blast stove, an air mixing chamber, 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 smoke discharged by the SCR reactor is discharged from an exhaust port of the SCR reactor. And a bypass pipeline is led out of the first pipeline to form the air mixing chamber. The air inlet of the air mixing chamber (3) is connected to the upstream position of the first pipeline, and the air outlet of the air mixing chamber is connected to the downstream position of the first pipeline.
Wherein, the active 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 mixing chamber through a third pipeline. The heating medium outlet is connected with the first pipeline through a fourth pipeline. The hot blast stove is connected with the air mixing chamber (3) through a second pipeline. The second conduit is connected to the plenum at a location upstream of the location at which the third conduit is connected to the plenum.
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 air inlet of the plenum exits the first pipe at a location upstream or downstream of the point at which the GGH heat exchanger is connected to the first pipe (L1).
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, a third fan is arranged on the fourth pipeline. 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.
Preferably, the SCR denitration device and the CO catalytic oxidation layer are arranged at intervals.
Preferably, 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 meter and a second temperature meter are arranged between the air inlet of the air mixing chamber and the GGH heat exchanger on the first pipeline. And a third temperature detector is arranged on the fourth pipeline. And a first flow regulating valve is arranged on the third pipeline, a second flow regulating valve is arranged on the fuel pipe, and a third flow regulating valve is arranged at the air inlet of the air mixing chamber.
According to a second embodiment of the present invention, there is provided a flue gas desulfurization and denitration treatment method using the split-flow 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 bypass pipeline is led out of the first pipeline to form an air mixing chamber, the air mixing chamber is connected with a hot blast stove through a second pipeline, and flue gas introduced from the first pipeline and hot air introduced from 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; a heating medium inlet and a heating medium outlet are arranged on the heating section, and the heating medium inlet is connected to the air mixing chamber through a third pipeline; the heating medium outlet is connected to the downstream of the first pipeline through a fourth pipeline, and the heating medium in the air mixing chamber is conveyed into the first pipeline after passing through the heating section under the action of a third fan.
Preferably, the method further comprises a step 4): the air inlet of the air mixing chamber is connected to the upstream position of the first pipeline, and the air outlet of the air mixing chamber is connected to the downstream position of the first pipeline. And the residual heat medium in the air mixing chamber and the heat medium from the fourth pipeline are conveyed back into the first pipeline to heat the residual low-temperature flue gas.
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.A second flow regulating valve on the fuel pipe regulates the input amount of fuel to be qBurning deviceL/s. 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:
qburning device△HBurning deviceFormula I.. formula I: C1 × q1(t3-t1) + C2 × q2(t4-t2).
Wherein: delta HBurning deviceIs 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 ℃).
Preferably, formula I is converted to:
qburning device＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/△HBurning 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 qBurning device。
Preferably, the temperature required for the heat medium in the air-mix chamber is set to t5℃. And the third flow regulating valve regulates the flow of flue gas entering the air mixing chamber to be q3, 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:
qburning device△HBurning deviceFormula III, C2 × q3(t5-t2).
Preferably, formula I and formula III are combined:
q3 ═ C1 q1(t3-t1) + C2 q2(t4-t2) ]/[ C2(t5-t2) ].
And adjusting the third flow adjusting valve to enable the flow of the flue gas delivered to the air mixing chamber by the first pipeline to be q 3.
Preferably, a third temperature detector is arranged on the fourth pipeline, and the third temperature detector detects that the temperature of the flue gas in the fourth 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 third pipeline:
c1 q1(t3-t1) ═ C3 q4(t5-t6) … formula V.
Wherein: c3 is the specific heat capacity of the heating medium entering the third pipeline after being mixed in the air mixing chamber, and J/(kg) degree. q4 is the flow rate of the heating medium in the third pipeline;
preferably, formula V is converted to:
q4 ═ C1 q1(t3-t1) ]/[ C3(t5-t6) ] … formula VI.
The first flow rate adjustment valve is adjusted so that the flow rate of the heating medium in the third pipe is q 4.
Preferably, in the hot blast furnace, the heat loss coefficient of fuel combustion is set to K1, and formula I is converted into:
K1*qburning device△HBurning deviceFormula VII, C1 q1(t3-t1) + C2 q2(t4-t2).
Preferably, formula II is converted to:
qburning device＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/[K1*△HBurning device].., formula XIII.
Preferably, in the air mixing chamber, the mixed heat loss coefficient of the hot air generated by the hot-blast stove and the flue gas distributed to the air mixing chamber is set to be K2, and then the formula III is converted into:
K2*K1*qburning device△HBurning device＝C2*q3(t5-t2)...IX。
Preferably, formula IV is converted to:
q3 ═ K2 × K1 [ C1 × q1(t3-t1) + C2 × q2(t4-t2) ]/[ C2(t5-t2) ].
Preferably, in the heating section of the activated carbon desorption tower, when the heat exchange coefficient between the heat medium and the activated carbon is set to 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 1 × (C3 (t5-t6) ] … formula XII.
Preferably, K1 takes the values: 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, 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 back to the desulfurization flue gas pipeline to be mixed with the residual desulfurization flue gas, and adjusting and mixing to enable the temperature of the flue gas to be in the optimal temperature range of denitration treatment; namely, on the premise of ensuring the flow of the heat medium required by the thermal regeneration of the activated carbon conveyed to the activated carbon desorption tower, the residual heat medium and the heat medium after the thermal regeneration of the activated carbon are all conveyed back to the desulfurization flue gas pipeline (downstream position) together to be mixed with the residual desulfurization flue gas, and the temperature of the mixed flue gas is adjusted to be in the optimal temperature range of the denitration treatment. According to the method, a heat source does not need to be separately arranged for the active carbon desorption tower and the SCR reactor (namely, a plurality of independent hot blast stoves 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 meter and a second temperature meter are arranged on the first pipeline and between the air inlet of the air mixing chamber and the GGH heat exchanger. The air inlet of the air mixing chamber 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:
qburning device△HBurning deviceFormula I.. formula I: C1 × q1(t3-t1) + C2 × q2(t4-t2).
Wherein: q. q.sBurning deviceL/s is the input amount of fuel. Delta HBurning deviceIs 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:
qburning device＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/△HBurning device.., formula II.
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 IIBurning 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 convertedCooling with cold air to form a thermal medium with the temperature of 400-500 ℃, considering the aim of heating and denitrating the desulfurized flue gas after being desulfurized by the activated carbon adsorption tower in the follow-up process, therefore, the hot air output by the hot blast stove is cooled and exchanged with heat in a way of mixing the desulfurized flue gas (cooling medium) and the hot air output by the hot blast stove in the air mixing chamber to form a heat medium (the original low-temperature desulfurized flue gas is used as the cooling medium, the flow of the flue gas which needs to be heated subsequently is reduced, a new air source is not introduced, the processing load of a subsequent SCR reactor is reduced, and the consumption of fuel is further greatly reduced), because the input amount of the fuel in the hot blast stove is fixed, the heat quantity generated in the hot blast stove can be calculated, therefore, the amount of the low-temperature desulfurization flue gas introduced into the air mixing chamber needs to be accurately controlled to ensure that the temperature range of the generated heat medium is about 400-500 ℃; meanwhile, considering 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 the actual working condition, 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-; the air inlet of the air mixing chamber is provided with a third flow regulating valve for regulating the flow of flue gas entering the air mixing chamber to be q3, L/s; a second flow regulating valve is arranged on the fuel pipe and used for regulating the input amount of fuel to be qBurning deviceL/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 air inlet of the air mixing chamber to t5 is derived from the heat released by the combustion of the fuel in the hot blast stove:
qburning device△HBurning deviceFormula 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 third 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 air inlet of the air mixing chamber is the calculated value q3 of formula IV.
In the invention, on the premise of ensuring the quantity of the heat medium required by the thermal regeneration of the activated carbon in the activated carbon desorption tower, the residual heat medium in the air mixing chamber is conveyed back to the desulfurization flue gas pipeline through the air outlet of the air mixing chamber to heat the desulfurization flue gas by 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 thermal regeneration of the activated carbon in the activated carbon desorption tower; 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 fourth pipeline, and the temperature of the smoke in the fourth pipeline detected by the third temperature detector is t6 and DEG C. The third branch line is provided with a first flow rate adjustment valve M1 for adjusting the flow rate of the heat medium supplied into the activated carbon desorption column via the third branch line to q4, L/s. 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 third pipeline after being mixed in the air mixing chamber, and J/(kg) degree. q4 is the flow rate of the heating medium in the third conduit.
Formula V is converted to:
q4 ═ C1 q1(t3-t1) ]/[ C3(t5-t6) ] … formula VI.
The first flow regulating valve M1 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 third 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 back to the desulfurization flue gas pipeline through an external discharge pipeline.
In the invention, because system heat losses exist in the system hot blast stove fuel combustion, 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 losses of the heat 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 is actually obtainedThere is actually a certain heat loss, i.e. the fuel input q is calculated by the formula IIBurning deviceAnd 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 calculated by the formula IV and the actual desulfurization flue gas amount to be introduced, and between the flow rate q4 of the heat medium conveyed to the heating section of the analysis tower calculated by the formula VI and the actual flow rate of the heat medium to be conveyed. Therefore, considering the heat loss of the system, in the hot blast stove, the heat loss coefficient of fuel combustion is set to K1 (then formula I is converted into:
K1*qburning device△HBurning deviceFormula VII, C1 q1(t3-t1) + C2 q2(t4-t2).
Formula II converts to:
qburning device＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/[K1*△HBurning 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 distributed to the air mixing chamber is set to be K2, and then the formula III is converted into the following formula:
K2*K1*qburning device△HBurning 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 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 1 × (C3 (t5-t6) ] … formula XII.
Then the fuel input quantity q actually to be input into the hot blast stove can be accurately calculated in real time through the formula VIIIBurning deviceThen, the flow q3 of the desulfurized flue gas to be conveyed to the air mixing chamber can be accurately calculated in real time through the formula X. 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 invention, the height of the activated carbon adsorption tower is 50-70 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 divided-flow flue gas desulfurization and denitrification treatment system;
fig. 2 is a structural diagram of a shunting type flue gas desulfurization and denitrification treatment system provided with 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 second activated carbon delivery device; l6: a first activated carbon delivery device; f1: a first fan; f2: a second fan; f3: a third 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; m3: and a third 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 shunting flue gas desulfurization and denitration treatment system comprises an activated carbon adsorption tower 1, an activated carbon desorption tower 2, a hot blast stove 4, an air mixing chamber 3 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 by the SCR reactor 7 is discharged from an exhaust port of the SCR reactor 7. A bypass pipeline is led out from the first pipeline L1 to form the air mixing chamber 3, the air inlet of the air mixing chamber 3 is connected at the upstream position of the first pipeline L1, and the air outlet of the air mixing chamber 3 is connected at the downstream position of the first pipeline L1.
Wherein, 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 provided in the heating section 201. The heating medium inlet 20101 is connected to the air-mixing chamber 3 through a third pipe L3. The heating medium outlet 20102 is connected to the first pipe L1 through a fourth pipe L4. The hot blast stove 4 is connected with the air mixing chamber 3 through a second pipeline L2. The position at which the second pipe L2 is connected to the air-mixing chamber 3 is upstream of the position at which the third pipe L3 is connected to the air-mixing chamber 3.
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 air inlet of the plenum 3 is led out 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 L6 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 L5. And/or
Preferably, a third fan F3 is disposed on the fourth duct L4. 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 provided in the SCR reactor 7. The SCR denitration device 701 and the CO catalytic oxidation layer 702 are arranged at intervals.
Preferably, 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. And a second flow meter Q2 and a second temperature meter T2 are arranged on the first pipeline L1 between the air inlet of the air mixing chamber 3 and the GGH heat exchanger 5. And a third temperature detector T3 is arranged on the fourth pipeline L4. A first flow regulating valve M1 is arranged on the third pipeline L3, a second flow regulating valve M2 is arranged on the fuel pipe 401, and a third flow regulating valve M3 is arranged at the air inlet of the air mixing chamber 3.
Example 1
As shown in fig. 1, a split-flow flue gas desulfurization and denitration treatment system includes an activated carbon adsorption tower 1, an activated carbon desorption tower 2, a hot blast stove 4, a wind mixing chamber 3 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 by the SCR reactor 7 is discharged from an exhaust port of the SCR reactor 7. A bypass pipeline is led out from the first pipeline L1 to form the air mixing chamber 3, the air inlet of the air mixing chamber 3 is connected at the upstream position of the first pipeline L1, and the air outlet of the air mixing chamber 3 is connected at the downstream position of the first pipeline L1.
Wherein, 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 provided in the heating section 201. The heating medium inlet 20101 is connected to the air-mixing chamber 3 through a third pipe L3. The heating medium outlet 20102 is connected to the first pipe L1 through a fourth pipe L4. The hot blast stove 4 is connected with the air mixing chamber 3 through a second pipeline L2. The position at which the second pipe L2 is connected to the air-mixing chamber 3 is upstream of the position at which the third pipe L3 is connected to the air-mixing chamber 3.
Example 2
Example 1 was repeated except that the system further included 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 air inlet of the plenum 3 leads from the first pipe L1 is downstream of the position where the GGH heat exchanger 5 is connected to the first pipe L1.
Example 3
Example 2 was repeated, and the activated carbon outlet of the activated carbon desorption tower 2 was connected to the activated carbon inlet of the activated carbon adsorption tower 1 through the first activated carbon delivery device L6 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 L5.
Example 4
Example 3 is repeated except that the fourth duct L4 is provided with a third fan F3.
Example 5
Example 4 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 6
Example 5 was repeated except that 2 SCR denitration devices 701 and 3 CO catalytic oxidation layers 702 were provided in the SCR reactor 7.
Example 7
Example 6 was repeated except that the SCR denitration device 701 and the CO catalytic oxidation layer 702 were disposed at intervals.
Example 8
Example 7 was repeated except that the activated carbon desorption column 2 was provided at the activated carbon inlet with a first flow rate meter Q1 and a first temperature meter T1. And a second flow meter Q2 and a second temperature meter T2 are arranged on the first pipeline L1 between the air inlet of the air mixing chamber 3 and the GGH heat exchanger 5. And a third temperature detector T3 is arranged on the fourth pipeline L4.
Example 9
Example 8 was repeated except that the third line L3 was provided with the first flow rate adjustment valve M1.
Example 10
Example 9 is repeated except that the fuel pipe 401 is provided with a second flow rate adjustment valve M2.
Example 11
Example 11 was repeated except that the air inlet of the air-mixing chamber 3 was provided with a third flow rate adjusting valve M3.
Effect example 1
The flue gas desulfurization and denitration treatment system in the embodiment 11 is adopted to perform desulfurization and denitration treatment on flue gas, and the amount of raw flue gas to be treated is 185.33 ten thousand meters under the condition of no shutdown for 24 hours by taking sintering flue gas as an example3The gas consumption is 1.30 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 (14)

1. The utility model provides a reposition of redundant personnel formula 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), a hot blast stove (4), an air mixing chamber (3) 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 by the SCR reactor (7) is discharged from an exhaust port of the SCR reactor (7); a bypass pipeline is led out from the first pipeline (L1) to form the air mixing chamber (3), the air inlet of the air mixing chamber (3) is connected at the upstream position of the first pipeline (L1), and the air outlet of the air mixing chamber (3) is connected at the downstream position of the first pipeline (L1);
wherein 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 the air mixing chamber (3) through a third pipeline (L3); the heating medium outlet (20102) is connected with the first pipeline (L1) through a fourth pipeline (L4); the hot blast stove (4) is connected with the air mixing chamber (3) through a second pipeline (L2); the second pipe (L2) is connected to the air mixing chamber (3) at a position upstream of the position at which the third pipe (L3) is connected to the air mixing chamber (3).
2. The system of claim 1, 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 air inlet of the air mixing chamber (3) is led out from the first pipeline (L1) is positioned at the upstream or downstream of the position where the GGH heat exchanger (5) is connected with the first pipeline (L1).
3. The system according to claim 1 or 2, characterized in that: 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 (L6); 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 (L5); and/or
A third fan (F3) is arranged on the fourth pipeline (L4); and/or
The hot blast stove (4) is also provided with a fuel pipe (401) and a combustion-supporting air pipe (402).
4. The system according to claim 1 or 2, characterized in that: 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.
5. The system of claim 3, 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.
6. The system of claim 4, wherein: m and n are each independently 2 to 4.
7. The system of claim 5, wherein: m and n are each independently 2 to 4.
8. The system of claim 3, 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 meter (Q2) and a second temperature meter (T2) are arranged on the first pipeline (L1) between the air inlet of the air mixing chamber (3) and the GGH heat exchanger (5); a third temperature detector (T3) is arranged on the fourth pipeline (L4); a first flow regulating valve (M1) is arranged on the third pipeline (L3), a second flow regulating valve (M2) is arranged on the fuel pipe (401), and a third flow regulating valve (M3) is arranged at an air inlet of the air mixing chamber (3).
9. The flue gas desulfurization and denitration treatment method using the split-flow type flue gas desulfurization and denitration treatment system of claim 8, 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 bypass pipeline is led out from the first pipeline (L1) to form an air mixing chamber (3), the air mixing chamber (3) is connected with a hot blast stove (4) through a second pipeline (L2), and flue gas introduced from the first pipeline (L1) and hot gas introduced from 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 third pipeline (L3), the heating medium outlet (20102) is connected to the downstream of the first pipeline (L1) through a fourth pipeline (L4), and under the action of a third fan (F3), the heating medium in the air mixing chamber (3) is conveyed to the first pipeline (L1) after passing through the heating section (201).
10. The method of claim 9, wherein: the method also comprises a step 4): the air inlet of the air mixing chamber (3) is connected at the upstream position of a first pipeline (L1), and the air outlet of the air mixing chamber (3) is connected at the downstream position of a first pipeline (L1); the residual heat medium in the air mixing chamber (3) and the heat medium from the fourth pipeline (L4) are conveyed back into the first pipeline (L1) to heat the residual low-temperature flue gas.
11. The method of claim 10, wherein: 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 rate regulating valve (M2) on the fuel pipe (401) regulates the fuel input amount to qBurning deviceL/s; according to the heat balance principle, the heat required by the activated carbon desorption tower (2) and the heat required by the temperature rise of the flue gas of the SCR reactor (7) are both from the combustion of fuel in the hot blast stove:
qburning device△HBurning deviceFormula I,. C1 q1(t3-t1) + C2 q2(t4-t 2);
wherein:△Hburning deviceIs 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:
qburning device＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/△HBurning 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。
12. The method of claim 11, wherein: setting the temperature required by the hot medium in the air mixing chamber (3) to t5 and DEG C; the third flow regulating valve (M3) regulates the flow of flue gas entering the air mixing chamber (3) to be q3, L/s; according to the heat balance principle, the heat required by raising the temperature of the flue gas entering the air mixing chamber (3) through the second pipeline (L2) to t5 comes from the hot blast stove (4)
Heat released by fuel combustion:
qburning device△HBurning deviceFormula 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) ].
The third flow regulating valve (M3) is regulated, so that the flow of flue gas conveyed to the air mixing chamber (3) by the first pipeline (L1) is q 3.
13. The method of claim 12, wherein: a third temperature detector (T3) is arranged on the fourth pipeline (L4), and the third temperature detector (T3) detects that the temperature of the flue gas in the fourth pipeline (L4) is T6 and DEG C; according to the heat balance principle, the heat required by the activated carbon desorption tower (2) is sourced from a wind mixing chamber (3) and is conveyed to a heating medium in the desorption tower (2) through a third pipeline (L3):
c1 q1(t3-t1) ═ C3 q4(t5-t6) … formula V;
wherein: c3 is the specific heat capacity of the heating medium entering the third pipeline (L3) after being mixed in the air mixing chamber (3), J/(kg ℃); q4 is the flow rate of the heating medium in the third conduit (L3);
formula V is converted to:
q4 ═ C1 q1(t3-t1) ]/[ C3(t5-t6) ] … formula VI;
the first flow rate adjustment valve (M1) is adjusted so that the flow rate of the heating medium in the third pipe (L3) is q 4.
14. The method of claim 12, 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:
K1*qburning device△HBurning deviceFormula VII, (VII) C1 q1(t3-t1) + C2 q2(t4-t 2);
formula II converts to:
qburning device＝[C1*q1(t3-t1)+C2*q2(t4-t2)]/[K1*△HBurning device].., formula XIII;
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 distributed to the air mixing chamber (3) is set to be K2, and then the formula III is converted into the following formula:
K2*K1*qburning device△HBurning 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) ═ K3K 2K 1C 3 q4(t5-t6) … formula XI;
formula VI is converted to:
q4 ═ C1 q1(t3-t1) ]/[ K3K 2K 1 × (C3 (t5-t6) ] … formula XII;
wherein, K1 takes on the value: 90% -99%; k2 is 95-99%; k3 takes a value of 85% -95%.
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