CN112403182A - Analytic tower and flue gas heating system - Google Patents

Analytic tower and flue gas heating system Download PDF

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Publication number
CN112403182A
CN112403182A CN201911070006.5A CN201911070006A CN112403182A CN 112403182 A CN112403182 A CN 112403182A CN 201911070006 A CN201911070006 A CN 201911070006A CN 112403182 A CN112403182 A CN 112403182A
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flue gas
activated carbon
pipeline
flue
formula
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CN112403182B (en
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魏进超
康建刚
何凯琳
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Zhongye Changtian International Engineering Co Ltd
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Zhongye Changtian International Engineering Co Ltd
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    • 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
    • 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
    • B01D53/0454—Controlling adsorption
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8628—Processes characterised by a specific catalyst
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

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  • Environmental & Geological Engineering (AREA)
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Abstract

The invention discloses an analytic tower and a flue gas heating system and a method, wherein the analytic tower and the flue gas heating system comprise an active carbon adsorption tower, an active carbon analytic tower, an inner flue, a hot blast stove and an SCR reactor; the hot air generated by the combustion of the fuel introduced into the hot blast stove by the inner flue is uniformly mixed with part of the desulfurized flue gas distributed into the inner flue to form a heat medium, and the heat medium is used for realizing the heat regeneration of the activated carbon in 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

Analytic tower and flue gas heating system
Technical Field
The invention relates to a flue gas desulfurization and denitration technology, in particular to a centralized heating 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 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 introduces fuel gas into an inner flue after the fuel gas is combusted to about 1000 ℃ in a hot blast stove in the presence of combustion air, uniformly mixes the fuel gas with flue gas in the inner flue, adjusts the temperature of hot air to 360-500 ℃, then adjusts the flow of the hot air (heat medium generated by the inner flue) entering the desorption tower according to the heat required by the activation of the activated carbon of the desorption tower, and then uniformly mixes the flue gas discharged from the desorption tower with other flue gas (ensuring that all the flue gas is in the temperature range required by SCR catalysis) and 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 invention, the system comprises an activated carbon adsorption tower, an activated carbon desorption tower, an inner flue, 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 SCR reactor through a first pipeline. And the clean flue gas discharged by the SCR reactor is discharged through a gas outlet of the SCR reactor. An inner flue is arranged in the first pipeline. And an air outlet of the hot blast stove is communicated to the inner flue through a second 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 inner flue through a third pipeline, and the position where the third pipeline is communicated with the inner flue is located at the downstream of the position where the second pipeline is communicated with the inner flue. The heating medium outlet is communicated to the first pipeline through a fourth pipeline and is positioned at the upstream or the downstream of the inner flue position.
Preferably, the upper end of the inner flue is provided with a flow baffle. The size of the flue gas flow entering the inner flue is controlled by controlling the distance between the flow baffle and the exhaust port of the inner flue.
Preferably, the system further comprises a GGH heat exchanger. 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 inner flue is positioned at 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, a second 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. 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 detection meter and a second temperature detection meter are arranged on the first pipeline and between the inner flue and the GGH heat exchanger. And a first flow regulating valve is arranged on the fuel pipe. And a third temperature detector is arranged on the fourth pipeline.
According to a second aspect of the present invention, there is provided a desorption tower and a flue gas heating method using the desorption tower and the flue gas heating system according to the first aspect, wherein: the method comprises the following steps:
1) according to the trend of the flue gas, the raw flue gas enters the activated carbon adsorption tower from the raw flue gas inlet through the gas inlet pipeline for desulfurization treatment. And the desulfurized flue gas is discharged from a desulfurized flue gas outlet and is conveyed to the GGH heat exchanger through a first pipeline for heat exchange and temperature rise. And conveying the desulfurized flue gas subjected to heat exchange and temperature rise to the SCR reactor for denitration treatment. And conveying the purified flue gas subjected to denitration treatment to a GGH heat exchanger for heat exchange and temperature reduction, and then discharging the purified flue gas through an exhaust pipeline.
2) An inner flue is arranged in the first pipeline. The hot blast stove is communicated to the inner flue through a second pipeline, and hot gas formed by combustion of the hot blast stove is introduced into the inner flue and is uniformly mixed with flue gas to form a hot medium.
3) 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 inner flue is connected to the heating medium inlet through a third pipeline, the heating medium outlet is connected with the first pipeline through a fourth pipeline, and the heating medium in the inner flue is conveyed back to the first pipeline through the heating section under the action of the second fan to heat the flue gas.
Preferably, the method further comprises a step 4): and a flow baffle is arranged at the upper end of the inner flue. The flow of the flue gas entering the inner flue is adjusted by controlling the distance between the flow baffle and the air outlet of the inner flue.
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. Detecting the temperature of the activated carbon at the activated carbon inlet of the activated carbon desorption tower by a first temperature detectorT1, DEG C. And detecting the total flow of the flue gas in the first pipeline to be q2 by the second flow detection meter. And detecting the temperature of the flue gas 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 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 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 deviceThe input amount of fuel is L/s. 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.
The amount of fuel delivered to the furnace through the fuel line is q by controlling the first flow regulating valve on the fuel lineBurning device。
Preferably, the temperature of the medium supplied to the activated carbon desorption tower is set to t5℃ (i.e., the temperature required for the heating medium in the inner flue is t5℃). The distance between the flow baffle and the inner flue gas outlet is h and m; the flue gas flow rate entering the inner flue 3 at this time is q3, L/s. According to the heat balance principle, the heat required by heating the flue gas entering the inner flue to t5 comes from the heat released by fuel combustion 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 distance between the flow baffle and the inner flue gas outlet to be h, so that the flue gas volume of the flue gas entering the inner flue is 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 heating medium which is conveyed into the desorption tower through the third pipeline from the inner flue:
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 inner flue, and J/(kg ℃). q4 is the flow rate of the heating medium in the third conduit.
Preferably, formula V is converted to:
q4 ═ C1 q1(t3-t1) ]/[ C3(t5-t6) ] … formula VI.
The second fan is controlled so that the flow rate of the heating medium delivered from the inner flue to the activated carbon desorption tower via the third duct 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 VIII.
Preferably, in the inner flue, the mixed heat loss coefficient of the hot air generated by the hot-blast stove and the flue gas distributed to the inner flue 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 1C 3(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, an inner flue is arranged in a desulfurization flue gas pipeline, all hot air generated by fuel combustion in a hot blast stove is introduced into the inner flue and is fully and uniformly mixed with part of desulfurization flue gas to form a new heat medium (the temperature range is about 400-. Then conveying the residual heat medium of the inner flue 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 the temperature of the mixed 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 in the inner flue and the heat medium after the thermal regeneration of the activated carbon are all conveyed back to the desulfurization flue gas pipeline (downstream position) 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, 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 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 detection meter and a second temperature detection meter are arranged on the first pipeline and between the inner flue gas inlet and the GGH heat exchanger. The top end of the inner flue is provided with a flow baffle (for adjusting and controlling the flow of the flue gas entering the inner flue), and the fuel pipe is provided with a first flow adjusting valve (for adjusting the flow of the total fuel needed 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 an inner flue after being calculated according to 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, the purpose of energy saving is achieved. Meanwhile, in order to prevent the heat generated by the external heat source from overflowing, and thus possibly threatening the system safety, the heat output by the external heat source needs to be regulated, that is, the input amount of 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 deviceThe input amount of fuel is L/s. 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.
Then can pass through the meter of the formula II in real timeThe calculation further adjusts the first flow control valve on the fuel line such that the amount of fuel delivered through the fuel line to the hot blast stove is a calculated value q of formula IIBurning device。
In the invention, under normal conditions, the heat temperature of hot air output by the hot blast stove is as high as about 1000 ℃, the regeneration temperature of activated carbon in the activated carbon desorption tower only needs about 400-, the processing load of a subsequent SCR reactor is reduced, and further, the fuel consumption is greatly reduced), because the input amount of the fuel in the hot blast stove is certain, the heat generated in the hot blast stove can be calculated, and therefore, the amount of the low-temperature desulfurization flue gas introduced into the inner flue needs to be accurately controlled to ensure that the temperature range of the generated heat medium is about 400-; 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 inner flue 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 inner flue is set to t5 (about 400-; a flow baffle is arranged at the top end of the inner flue, the height of the flow baffle from the upper end of the inner flue is adjusted to be h, and the flow of flue gas entering the inner flue is controlled to be q 3L/s; a first 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 regulating the temperature of the flue gas entering the inner flue to t5 through the flow baffle 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) ].
And then, the distance between the baffle plate and the top end of the inner flue can be further adjusted to be h by the calculated value of the formula IV in real time, so that the desulfurized flue gas volume of the flue gas entering the inner flue is adjusted to be the calculated value q3 of the formula IV by the baffle plate.
In the invention, considering that the total flow of the heat medium in the mixed inner flue 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, the residual heat medium is conveyed back to the desulfurization flue gas pipeline through the air outlet of the inner flue to heat the desulfurization flue gas on the premise of ensuring the amount of the heat medium required by the thermal regeneration of the activated carbon in the activated carbon desorption tower; and 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 again and heat reentrant SCR reactor behind the low temperature desulfurization flue gas and carry out denitration treatment. In order to reasonably distribute the heat medium in the inner flue, the third temperature detector is arranged on the fourth pipeline, and the temperature of the flue gas in the fourth 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 heating medium which is conveyed into the desorption tower through the third pipeline from the inner flue:
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 the mixture of the inner flue and J/(kg ℃). 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 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 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 inner flue is conveyed back to the desulfurization flue gas pipeline through the air outlet of the inner flue.
In the invention, because the system heat loss exists in the fuel combustion of the system hot blast stove, the mixing of high-temperature hot air and low-temperature flue gas in the inner flue into a heat medium, the heat exchange between the heat medium and the active carbon in the heating section of the desorption tower and the like, the loss of the heat can be obtained by calculation according to the actual working condition, so that the heat released by the fuel combustion in the hot blast stove actually has certain heat loss, namely the fuel input q calculated by the formula IIBurning deviceAnd the actual fuel input amount, the desulfurization flue gas amount q3 of the flue gas entering the inner flue through the baffle plate and calculated by the formula IV and the actual introduced desulfurization flue gas amount, and the flow rate q4 of the heat medium conveyed to the heating section of the analysis tower and the actual conveyed heat medium amount have certain errors. Therefore, on the premise of considering the heat loss of the system, 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 the following formula:
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 inner flue, the mixed heat loss coefficient of the hot air generated by the hot-blast stove and the flue gas distributed to the inner flue 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 1C 3(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 device(ii) a Then accurately calculating the flow q3 of the low-temperature desulfurized flue gas to be distributed and conveyed to the inner flue in real time by the formula X; the flow rate q4 of the heat medium to be distributed to the heating section of the desorption tower can be accurately calculated by formula XII.
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 block diagram of a desorption tower and flue gas heating system;
fig. 2 is a structure diagram of the desorption tower and the flue gas heating system 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: an inner flue; 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 first activated carbon delivery device; l6: a second activated carbon delivery device; f1: a first fan; f2: a second 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.
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.
An active carbon adsorption tower 1, an active carbon desorption tower 2, an inner flue 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 connected to the SCR reactor 7 via a first duct L1. And the clean flue gas discharged from the SCR reactor 7 is discharged from a gas outlet of the SCR reactor 7. An inner flue 3 is provided in the first duct L1. The air outlet of the hot blast stove 4 is communicated to the inner flue 3 through a second pipeline L2.
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 inner tunnel 3 through a third pipe L3, and a position where the third pipe L3 communicates with the inner tunnel 3 is located downstream of a position where the second pipe L2 communicates with the inner tunnel 3. The heating medium outlet 20102 is connected to the first pipe L1 through a fourth pipe L4 and is located downstream of the position of the inner flue 3.
Preferably, a baffle plate 301 is disposed at the upper end of the inner flue 3. The size of the flue gas flow entering the inner flue 3 is controlled by controlling the distance between the baffle plate 301 and the exhaust port of the inner flue 3.
Preferably, the system further comprises a GGH heat exchanger 5. The outlet from the SCR reactor 7 is connected to an exhaust gas line 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 inner tunnel 3 is located upstream or downstream of the point 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 L5 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 L6. And/or
Preferably, a second fan F2 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. A second flow rate meter Q2 and a second temperature meter T2 are provided on the first pipe L1 between the inner tunnel 3 and the GGH heat exchanger 5. The fuel pipe 401 is provided with a first flow rate regulating valve M1. And a third temperature detector T3 is arranged on the fourth pipeline L4.
Example 1
As shown in fig. 1, the system comprises an activated carbon adsorption tower 1, an activated carbon desorption tower 2, an inner flue 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 connected to the SCR reactor 7 via a first duct L1. And the clean flue gas discharged from the SCR reactor 7 is discharged from a gas outlet of the SCR reactor 7. An inner flue 3 is provided in the first duct L1. The air outlet of the hot blast stove 4 is communicated to the inner flue 3 through a second pipeline L2. 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 inner tunnel 3 through a third pipe L3, and a position where the third pipe L3 communicates with the inner tunnel 3 is located downstream of a position where the second pipe L2 communicates with the inner tunnel 3. The heating medium outlet 20102 is connected to the first pipe L1 and located downstream of the inner flue 3 through a fourth pipe L4.
Example 2
Example 1 was repeated except that the upper end of the inner flue 3 was provided with a baffle 301. The size of the flue gas flow entering the inner flue 3 is controlled by controlling the distance between the baffle plate 301 and the exhaust port of the inner flue 3.
Example 3
Example 2 is repeated except that the system further comprises a GGH heat exchanger 5. The outlet from the SCR reactor 7 is connected to an exhaust gas line 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 inner tunnel 3 is located downstream of the point 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 L5 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 L6. And/or
Example 5
Example 4 is repeated except that the fourth duct L4 is provided with a second fan F2.
Example 6
Example 5 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 7
Example 6 was repeated except that 2 SCR denitration devices 701 and 1 CO catalytic oxidation layer 702 were provided in the SCR reactor 7. The SCR denitration device 701 and the CO catalytic oxidation layer 702 are arranged 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. A second flow rate meter Q2 and a second temperature meter T2 are provided on the first pipe L1 between the inner tunnel 3 and the GGH heat exchanger 5.
Example 9
Embodiment 8 is repeated except that the fuel pipe 401 is provided with a first flow rate adjustment valve M1.
Example 10
Example 9 was repeated except that the fourth pipe L4 was provided with a third temperature detecting gauge T3.
Effect example 1
The flue gas is subjected to desulfurization and denitrification treatment by adopting the desorption tower and the flue gas heating system in the embodiment 10, and the amount of the treated raw flue gas is 185.97 ten thousand meters under the condition of taking the sintering flue gas as an example and not stopping the machine for 24 hours3The gas consumption is 1.25 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 (12)

1. The utility model provides a desorption tower and flue gas heating system which characterized in that: the system comprises an active carbon adsorption tower (1), an active carbon desorption tower (2), an inner flue (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 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); an inner flue (3) is arranged in the first pipeline (L1); the air outlet of the hot blast stove (4) is communicated to the inner flue (3) through a second pipeline (L2);
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 formed in the heating section (201), the heating medium inlet (20101) is connected with the inner flue (3) through a third pipeline (L3), and the position where the third pipeline (L3) is communicated with the inner flue (3) is located at the downstream of the position where the second pipeline (L2) is communicated with the inner flue (3); the heating medium outlet (20102) is connected to the first pipe (L1) through a fourth pipe (L4) and is positioned at the downstream of the position of the inner flue (3).
2. The system of claim 1, wherein: the upper end of the inner flue (3) is provided with a flow baffle plate (301), and the flow of flue gas entering the inner flue (3) is controlled by controlling the distance between the flow baffle plate (301) and the exhaust port of the inner flue (3).
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 inner flue (3) is located upstream or downstream of the connection of the GGH heat exchanger (5) and 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 (L5); 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 (L6); and/or
A second fan (F2) 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).
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 1-5, 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 inner flue (3) and the GGH heat exchanger (5); a first flow regulating valve (M1) is arranged on the fuel pipe (401); and a third temperature detector (T3) is arranged on the fourth pipeline (L4).
7. The desorption tower and the flue gas heating method adopting the desorption tower and the flue gas heating system as claimed in any one of claims 1 to 6, are 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) an inner flue (3) is arranged in the first pipeline (L1), the hot blast stove (4) is communicated to the inner flue (3) through a second pipeline (L2), and hot air formed by combustion of the hot blast stove (4) is introduced into the inner flue (3) and is uniformly mixed with flue gas 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 formed in the heating section (201), the inner flue (3) is connected to the heating medium inlet (20101) through a third pipeline (L3), the heating medium outlet (20102) is connected with the first pipeline (L1) through a fourth pipeline (L4), and the heating medium in the inner flue (3) is conveyed back to the first pipeline (L1) to heat flue gas under the action of a second fan (F2) after passing through the heating section (201).
8. The method of claim 7, wherein: the method also comprises a step 4): the upper end of the inner flue (3) is provided with a flow baffle plate (301), and the flow of the flue gas entering the inner flue (3) is adjusted by controlling the distance between the flow baffle plate (301) and the gas outlet of the inner flue (3).
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 total flow of the smoke in the first pipeline (L1) as Q2 by a second flow detector (Q2); detecting the temperature of the flue gas in the first pipeline (L1) to be T2 and DEG C by 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 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: q. q.sBurning deviceThe input amount of fuel, L/s; 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 (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 first flow regulating valve (M2) on the fuel pipe (401)Burning device。
10. The method of claim 9, wherein: setting the temperature of the medium conveyed to the activated carbon desorption tower (2) to be t5 and DEG C, namely setting the temperature required by the hot medium in the inner flue (3) to be t5 and DEG C; the distance between the flow baffle (301) and the exhaust port of the inner flue (3) is h and m; at the moment, the flow rate of the flue gas entering the inner flue (3) is q3 and L/s; according to the heat balance principle, the heat required by the temperature rise of the flue gas entering the inner flue (3) to t5 comes from the heat released by the combustion of fuel in the hot blast stove (4):
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) ]. formula IV;
the distance between the flow baffle (301) and the exhaust port of the inner flue (3) is adjusted to be h, so that the flue gas volume of the flue gas entering the inner flue (3) is q 3.
11. The method of claim 10, 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 derived from the heating medium which is conveyed into the desorption tower (2) by the inner flue (3) 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 inner flue (3), and 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 second fan (F2) was controlled so that the flow rate of the heating medium delivered from the inner flue (3) to the activated carbon desorption tower (2) via the third conduit (L3) was q 4.
12. The method of claim 11, 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 VIII;
in the inner flue (3), the mixed heat loss coefficient of the hot air generated by the hot blast stove (4) and the flue gas distributed to the inner flue (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) ═ 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%.
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