CN108096989B - Flue gas purification method and device comprising flue gas temperature control - Google Patents

Flue gas purification method and device comprising flue gas temperature control Download PDF

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CN108096989B
CN108096989B CN201810135593.0A CN201810135593A CN108096989B CN 108096989 B CN108096989 B CN 108096989B CN 201810135593 A CN201810135593 A CN 201810135593A CN 108096989 B CN108096989 B CN 108096989B
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flue gas
temperature
bypass
pipeline
water
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CN108096989A (en
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魏进超
叶恒棣
杨本涛
李勇
刘昌齐
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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
    • 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
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/30—Technologies for a more efficient combustion or heat usage
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/25—Process efficiency

Abstract

A flue gas purification method with flue gas temperature control comprises the following steps of 1) enabling an original flue gas conveying pipeline to be divided into bypass flue gas pipelines, 2) ① enabling waste water to be sprayed into the bypass flue gas pipelines through an atomizer to exchange heat with flue gas entering the bypass flue gas pipelines to form mixed gas of the flue gas and the waste water, ② introducing cold air into the original flue gas conveying pipeline at the downstream of the position, where the original flue gas conveying pipeline is divided into the bypass flue gas pipelines to adjust the temperature of the flue gas, ③ enabling the mixed gas of the flue gas and the waste water in the bypass flue gas pipelines to be mixed with the flue gas, temperature of which is controlled by the cold air, in the original flue gas conveying pipeline, enabling the mixed flue gas to enter an adsorption tower, adjusting the temperature of the flue gas at an inlet of the adsorption tower within a specified range, and 3) enabling the mixed flue gas to enter an activated carbon adsorption tower, enabling the flue gas to be adsorbed by activated carbon in the adsorption tower to be discharged after being adsorbed and purified, enabling the activated carbon, which is adsorbed pollutants in the flue.

Description

Flue gas purification method and device comprising flue gas temperature control
Technical Field
The invention relates to a flue gas purification technology adopting an activated carbon adsorption tower, in particular to a flue gas purification method and a flue gas purification device comprising flue gas temperature control, and belongs to the field of sintering flue gas treatment.
Background
For industrial flue gas, especially sintering machine flue gas in the steel industry, it is desirable to adopt a large-scale dry desulfurization and denitrification device and process comprising an activated carbon adsorption tower and an analysis tower. The activated carbon flue gas purification technology has the characteristics of simultaneous desulfurization and denitrification, realization of byproduct recycling, recyclable adsorbent, high desulfurization and denitrification efficiency and the like, and is a desulfurization and denitrification integrated technology with great development prospect. In a desulfurization and denitration apparatus including an activated carbon adsorption tower for adsorbing pollutants including sulfur oxides, nitrogen oxides, and dioxins from sintering flue gas or exhaust gas (particularly sintering flue gas of a sintering machine in the steel industry) and a desorption tower (or regeneration tower) for thermal regeneration of activated carbon.
However, the flue gas purification technology by the activated carbon method has high requirements on the control of the temperature of raw flue gas, the temperature of the raw flue gas after passing through a booster fan is often above 150 ℃ (for example, the temperature of flue gas at the inlet of an adsorption tower without being subjected to cooling treatment can reach 150-. In general, the normal temperature of the activated carbon bed layer in the activated carbon adsorption tower is 100-160 ℃, and is preferably controlled at 110-150 ℃.
In one aspect, the activated carbon bed temperature is strictly controlled to be below 165 deg.C, preferably below 160 deg.C, in order to prevent combustion of the activated carbon in the bed. This is because, although the ignition point of activated carbon is around 430 ℃, the chemical reaction occurring on the surface of activated carbon is generally an exothermic reaction, and the dust in flue gas contains a small amount of combustible, combustion-supporting substances, and the activated carbon itself also entrains combustible dust. If the temperature in the adsorption tower is not strictly controlled, the existence of the inflammable substances or inflammable dust can cause safety hazards at any time, the spontaneous combustion of the activated carbon in the adsorption tower with the height of dozens of meters can be caused if the temperature is light, and the dust explosion can be caused if the temperature is serious, and the two accidents are disastrous to a large-scale desulfurization and denitrification tower device. Therefore, for safety, the alarm temperature of the activated carbon bed is generally set to 165 ℃. The temperature of the sintering raw flue gas is generally 90-200 ℃ after being pressurized by a booster fan, preferably 100-180 ℃, the oxygen content in the sintering flue gas is high, and the temperature of a bed layer after the surface of active carbon in the tower is oxidized is 5-15 ℃ higher than that of inlet flue gas, so that the temperature of the flue gas entering the adsorption tower needs to be controlled in order to ensure the safe operation of the desulfurization and denitrification device, and the alarm temperature is generally set to 145 ℃. In addition, before the adsorption tower is stopped, the temperature of the activated carbon bed layer in the adsorption tower needs to be kept lower than 90 ℃, and at the moment, the activated carbon bed layer needs to be cooled, so that the temperature of the activated carbon bed layer also needs to be controlled in order to ensure safe stop.
On the other hand, when the activated carbon flue gas purification system is in normal operation, the temperature of the flue gas entering the adsorption tower needs to be strictly controlled to be higher than or not lower than 100 ℃, and preferably higher than or not lower than 110 ℃. This is because, if the flue gas temperature is lower than 100 ℃, the temperature of the water vapor contained in the sintering flue gas entering the bed is close to the dew point (or condensation point), and it is very easy to become water and react with sulfur oxides to become a strongly corrosive acid, resulting in severe corrosion of the apparatus and severely reducing the desulfurization and denitrification effects.
The traditional flue gas cooling method is to directly spray water mist into flue gas to realize flue gas cooling. This cooling method cannot use waste water (e.g., waste water generated from a washing system in an activated carbon method) as a water source because harmful elements in the waste water are cyclically concentrated in the system and corrode system equipment.
Disclosure of Invention
In view of the above-mentioned deficiencies of the prior art, it is an object of the present invention to provide a method and apparatus for flue gas purification including flue gas temperature control. On the basis of the prior art, the invention adopts the original flue gas conveying pipeline to divide a bypass flue gas pipeline, the bypass flue gas is sprayed into the waste water to cool, and the waste water is dedusted, so that the reasonable treatment of the waste water can be ensured, and the accurate control of the flue gas temperature can be realized.
According to a first embodiment of the invention, there is provided a flue gas purification process comprising flue gas temperature control:
a method of flue gas purification including flue gas temperature control, the method comprising the steps of:
1) a bypass flue gas pipeline is divided from an original flue gas conveying pipeline for conveying high-temperature flue gas to the activated carbon adsorption tower, and the flue gas enters the adsorption tower through the original flue gas conveying pipeline and the bypass flue gas pipeline;
2) the method comprises a flue gas temperature control step or a flue gas temperature regulation step, wherein the flue gas temperature regulation step comprises the following substeps:
① temperature control of the flue gas in the bypass flue gas pipeline, wherein the bypass flue gas pipeline is provided with an atomizer, the waste water is atomized by the atomizer and then mixed with the flue gas in the bypass flue gas pipeline, and the waste water exchanges heat with the flue gas entering the bypass flue gas pipeline to form a mixed gas of the flue gas and the waste water;
② controlling temperature of the flue gas in the original flue gas conveying pipeline by introducing cold air into the original flue gas conveying pipeline at the downstream of the bypass flue gas pipeline;
③ mixing the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline to the original flue gas conveying pipeline, mixing with the flue gas in the original flue gas conveying pipeline after temperature control or temperature regulation by cold air, and entering the adsorption tower, wherein the flue gas temperature at the inlet of the adsorption tower is regulated within a specified range;
3) the mixed flue gas enters an activated carbon adsorption tower, is adsorbed and purified by activated carbon in the adsorption tower and then is discharged, and the activated carbon adsorbing pollutants in the flue gas is discharged from the bottom of the adsorption tower.
In the substep ①, the flue gas and wastewater mixed gas means that when the wastewater exchanges heat with the flue gas entering the bypass flue gas pipeline, the wastewater is evaporated to become gaseous water, and the evaporated gaseous water is mixed with the flue gas, i.e. the flue gas and wastewater mixed gas.
Preferably, in sub-step ① of the method, the wastewater is passed from the wastewater storage tank to the atomizer along a wastewater inlet line.
Preferably, in sub-step ② of the method, the cool air is delivered from an air duct to a raw flue gas delivery duct.
Preferably, in step 2) of the method, a first temperature measuring point is arranged upstream of the position of the raw flue gas conveying pipeline where the bypass flue gas pipeline is branched. And a second temperature measuring point is arranged between the position of the cold air introduced into the original flue gas conveying pipeline and the position of the bypass flue gas pipeline merged to the original flue gas conveying pipeline. And a third temperature measuring point is arranged on the bypass flue gas pipeline and is positioned at the downstream of the dust remover. And a fourth temperature measuring point is arranged on the original flue gas conveying pipeline and at the downstream of the position where the bypass flue gas pipeline is combined to the original flue gas conveying pipeline. The first temperature measuring point detects the flue gas temperature T1 in the flue at the corresponding position on line. The second temperature measuring point detects the flue gas temperature T2 in the flue at the corresponding position on line. The third temperature measuring point detects the corresponding position on lineThe temperature of the flue gas in the flue T3. And the fourth temperature measuring point detects the flue gas temperature T4 in the flue at the corresponding position on line. Wherein the target or set temperature value at the fourth temperature measurement point is T4Is provided with。
According to the heat Q released by the flue gas entering the bypass flue gas pipelineCigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas ductWater (W)And equalising, calculating and adjusting the amount of flue gas entering the bypass flue gas duct in sub-step ① further dependent on the heat Q released by the flue gas entering the adsorption tower through the raw flue gas ductCigarette 2The heat Q absorbed by cold air introduced into the raw flue gas conveying pipelineQi (Qi)And (3) equally calculating and adjusting the amount of cold air introduced into the raw flue gas duct in the substep ② the temperature T4 at the fourth temperature measurement point is adjusted or controlled to be T4 by adjusting the amount of flue gas entering the bypass flue gas duct and the amount of cold air introduced into the raw flue gas ductIs provided withA temperature range of + -t deg.C, wherein t deg.C is in the range of 1-5 deg.C.
Preferably, the target or set value of the temperature at the fourth temperature measuring point T4Is provided withThe temperature is 100-145 ℃, preferably 110-140 ℃; i.e. the temperature of the flue gas at the inlet of the adsorption column is adjusted within a specified range, for example within the range of 100 ℃ and 145 ℃, preferably within the range of 110 ℃ and 140 ℃.
Preferably, said heat Q released according to the flue gas entering the bypass flue gas duct isCigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas ductWater (W)And (3) equally, calculating and adjusting the amount of the flue gas entering the bypass flue gas pipeline in the substep ①, specifically:
the first temperature measuring point detects the original flue gas temperature as T1, and the temperature of the mixed gas of the flue gas and the waste water at the third temperature measuring point is set as T3Is provided withWherein: t3Is provided withThe temperature is 100-160 ℃, and the value is preferably within the range of 110-140 ℃;
a) calculating the heat required by wastewater treatment: a liquid level meter is arranged in the waste water storage tank, and the quantity of waste water to be treated in the waste water storage tank is M according to the quantity of the waste water obtained by the liquid level meterWater (W)Detecting the initial temperature of the wastewater as TWater (W)Whereby the amount of heat Q to be absorbed for treating the waste water in the waste water storage tankWater (W)Comprises the following steps:
Qwater (W)＝MWater (W)rWater (W)+CWater vapourMWater (W)ΔTWater (W)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (1)，
In the formula (1), rWater (W)Is the heat of vaporization of the waste water, CWater vapourThe specific heat capacity of water vapor;
b) calculating the required flue gas amount of a bypass flue gas pipeline: setting the amount of the flue gas entering the bypass flue gas pipeline as M1Whereby the heat Q released by the flue gas entering the bypass flue gas ductCigarette 1Comprises the following steps:
Qcigarette 1＝CCigarette with heating meansM1ΔTCigarette 1＝CCigarette with heating meansM1(T1-T3Is provided with) (2)，
C in formula (2)Cigarette with heating meansThe specific heat capacity of the flue gas;
heat Q released by flue gas entering the bypass flue gas ductCigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas ductWater (W)Equality, we can get:
Ccigarette with heating meansM1(T1-T3Is provided with)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (3)，
Obtaining the following components:
M1＝Mwater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W)))/(CCigarette with heating means(T1-T3Is provided with)) (4)；
Adjusting the opening degree of a bypass valve on the bypass flue gas pipeline to ensure that the amount of the flue gas entering the bypass flue gas pipeline is M1。
In the invention, the temperature T3 of the mixed gas of the flue gas and the waste water after the heat exchange of the flue gas and the waste water is generally set according to specific conditionsIs provided with. For example, T3 is usually set in view of minimizing the load and wear on the atomizer and the dust catcher upstream of the third temperature measurement point as much as possibleIs provided withIs T4Is provided withOf (e.g. T3)Is provided with＝105℃。
In addition, the waste water exchanges heat with the flue gasThe waste water is evaporated to absorb heat, and the heat absorbed by water evaporation is generally calculated by two parts, one part is initial temperature TWater (W)Is evaporated to a temperature TWater (W)Water vapor of (2) having a heat absorption of MWater (W)rWater (W)The other part is at a temperature TWater (W)Is heated to a temperature of T3Is provided withWater vapor of (2), heat absorption capacity is CWater vapourMWater (W)ΔTWater (W)。
Preferably, the heat Q released by the flue gas entering the adsorption tower through the raw flue gas conveying pipeline is further determinedCigarette 2The heat Q absorbed by cold air introduced into the raw flue gas conveying pipelineQi (Qi)And (3) equality, calculating and adjusting the amount of cold air introduced into the original flue gas conveying pipeline in the substep ②, specifically:
the total amount of the smoke measured by the flowmeter at the upstream of the first temperature measuring point is M0The temperature of the original smoke detected by the first temperature measuring point is T1, and the temperature of the mixed gas of the smoke and the cold air at the position of the second temperature measuring point is set to be T2Is provided withWherein: t2Is provided withThe temperature is 100-160 ℃, and the value is preferably within the range of 110-140 ℃;
a) calculating the heat quantity to be released by the original flue gas in the original flue gas conveying pipeline: the amount of flue gas entering the adsorption tower through the raw flue gas conveying pipeline is (M)0-M1) The heat Q released by the flue gas entering the adsorption tower through the raw flue gas conveying pipelineCigarette 2Comprises the following steps:
Qcigarette 2＝CCigarette with heating means(M0-M1)ΔTCigarette 2＝CCigarette with heating means(M0-M1)(T1-T2Is provided with) (5)，
b) Calculating the amount of cold air introduced into the original flue gas conveying pipeline: the quantity of cold air introduced into the original flue gas conveying pipeline is set to be MQi (Qi)Measuring the initial temperature of the cold air as TQi (Qi)Whereby the cold air passing into the raw flue gas duct absorbs heat QQi (Qi)Comprises the following steps:
Qqi (Qi)＝CQi (Qi)MQi (Qi)ΔTQi (Qi)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (6)，
C in formula (6)Qi (Qi)Is the specific heat capacity of the cold air;
heat Q released by flue gas entering the adsorption column through the raw flue gas ductCigarette 2The heat Q absorbed by cold air introduced into the raw flue gas conveying pipelineQi (Qi)Equality, we can get:
Ccigarette with heating means(M0-M1)(T1-T2Is provided with)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (7)；
Obtaining the following components:
Mqi (Qi)＝CCigarette with heating means(M0-M1)(T1-T2Is provided with)/(CQi (Qi)(T2Is provided with-TQi (Qi))) (8)；
The opening degree of a cold air valve on the air pipeline is adjusted, so that the amount of cold air introduced into the original flue gas conveying pipeline is MQi (Qi)。
Preferably, the temperature T4 of the fourth temperature measuring point is adjusted or controlled at T4 by adjusting the amount of flue gas entering the bypass flue gas duct and the amount of cold air introduced into the raw flue gas conveying ductIs provided withThe range of +/-t ℃ is as follows:
the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline is mixed with the mixed gas of the flue gas and the cold air in the original flue gas conveying pipeline after the temperature of the flue gas and the waste water is controlled or regulated by the cold air, after the two paths of gas are subjected to heat exchange, the temperature T4 of a fourth temperature measuring point (P4) is regulated or controlled at T4Is provided withThe range of +/-t ℃. The heat Q absorbed (or released) by the mixed gas of the flue gas and the waste water in the bypass flue gas pipelineSmoke and waterThe heat Q released (or absorbed) by the mixed gas of the flue gas and the cold air in the raw flue gas conveying pipelineSmoke and gasEqual, i.e.:
Qsmoke and water＝QSmoke and gas(9)，
Namely: c1(M1+MWater (W))(T4Is provided with-T3Is provided with)＝C2(M0-M1+MQi (Qi))(T2Is provided with-T4Is provided with) (10)，
C in formula (10)1The specific heat capacity of the mixed gas of the flue gas and the waste water; c2Is the specific heat capacity of the mixed gas of the flue gas and the cold air.
Preferably, T2Is provided with＝T3Is provided with＝T4Is provided with。
In the invention, in order to make the flue gas temperature after the two flue gases in the bypass flue gas pipeline and the original flue gas conveying pipeline are mixed (i.e. the flue gas temperature T4 in the flue at the position corresponding to the fourth temperature measuring point) be controlled at T4 more easilyIs provided withThe temperature of the flue gas before the two paths of flue gas are mixed is set or controlled to be T4 within the range of +/-T DEG CIs provided withI.e. T3Is provided with＝T4Is provided with，T2Is provided with＝T4Is provided with。
Preferably, the flue gas temperature T2 in the flue at the corresponding position is detected on line according to the second temperature measuring point. If T2 equals T2Is provided withContinuing to operate; t2 not equal to T2Is provided withAdjusting the amount of cold air introduced into the original flue gas conveying pipe so that T2 is equal to T2Is provided with。
T2 is greater than T2Is provided withDuring the process, the opening degree of a cold air valve on the air pipeline is adjusted to increase the amount of cold air introduced into the original flue gas conveying pipeline, so that T2 is equal to T2Is provided with(ii) a T2 less than T2Is provided withDuring the process, the opening degree of a cold air valve on the air pipeline is reduced, so that the amount of cold air introduced into the original flue gas conveying pipeline is reduced, and T2 is equal to T2Is provided with。
And detecting the flue gas temperature T3 in the flue at the corresponding position on line according to the third temperature measuring point. If T3 equals T3Is provided withContinuing to operate; t3 not equal to T3Is provided withAdjusting the amount of flue gas entering the bypass flue gas duct such that T3 equals T3Is provided with。
T3 is greater than T3Is provided withAt this time, the opening of the bypass valve on the bypass flue gas duct is reduced to reduce the amount of flue gas entering the bypass flue gas duct so that T3 is equal to T3Is provided with(ii) a T3 less than T3Is provided withAt this time, the opening of the bypass valve on the bypass flue gas duct is increased to increase the amount of flue gas entering the bypass flue gas duct so that T3 is equal to T3Is provided with。
And detecting the flue gas temperature T4 in the flue at the corresponding position on line according to the fourth temperature measuring point. If T4 equals T4Is provided withContinuing to operate; t4 not equal to T4Is provided withAdjusting the cold air introduced into the original flue gas conveying pipelineThe amount of gas and the amount of flue gas entering the bypass flue gas duct are such that T4 equals T4Is provided with。
T4 is greater than T4Is provided withDuring the process, the opening degree of a cold air valve on the air pipeline is adjusted to increase the amount of cold air introduced into the original flue gas conveying pipeline, and the opening degree of a bypass valve on the bypass flue gas pipeline is adjusted to decrease the amount of flue gas entering the bypass flue gas pipeline, so that T4 is equal to T4Is provided with(ii) a T4 less than T4Is provided withDuring the process, the opening degree of a cold air valve on the air pipeline is reduced, so that the amount of cold air introduced into the original flue gas conveying pipeline is reduced, meanwhile, the opening degree of a bypass valve on the bypass flue gas pipeline is increased, so that the amount of flue gas entering the bypass flue gas pipeline is increased, and T4 is equal to T4Is provided with。
Preferably, in step 3) of the above method, the flue gas adsorbed and purified by the activated carbon in the adsorption tower is discharged through a chimney.
According to a second embodiment of the invention, there is provided a flue gas cleaning device comprising a flue gas temperature control:
a flue gas purification device comprising flue gas temperature control or a flue gas purification device used for the method comprises an adsorption tower, wherein an adsorption tower flue gas inlet is arranged on the adsorption tower. The flue gas inlet of the adsorption tower is connected with the original flue gas conveying pipeline. The original flue gas conveying pipeline is divided into bypass flue gas pipelines. An atomizer and a dust remover are sequentially arranged on the bypass flue gas pipeline. The atomizer is provided with a flue gas inlet, a flue gas outlet and a waste water inlet. The dust remover is provided with a gas inlet, a gas outlet and a solid outlet. The bypass flue gas pipeline passes through the atomizer and the dust remover and then is combined to the original flue gas conveying pipeline. The atomizer is disposed upstream of the dust separator.
A first booster fan is arranged on the original flue gas conveying pipeline. The first booster fan is arranged at the downstream of the position where the bypass flue gas pipeline is merged to the original flue gas conveying pipeline.
The original flue gas conveying pipeline is connected with an air pipeline. The air pipeline is connected between the position of the bypass flue gas pipeline separated from the original flue gas conveying pipeline and the position of the bypass flue gas pipeline combined to the original flue gas conveying pipeline.
Preferably, the apparatus further comprises a bypass valve disposed on the bypass flue gas duct. The bypass valve is located upstream of the atomizer.
Preferably, the device further comprises a cold air valve arranged on the air duct. In the invention, a first temperature measuring point is arranged at the upstream of the position of the bypass flue gas pipeline separated from the original flue gas conveying pipeline. And a second temperature measuring point is arranged between the position where the original flue gas conveying pipeline is connected with the air pipeline and the position where the bypass flue gas pipeline is combined to the original flue gas conveying pipeline. And a third temperature measuring point is arranged on the bypass flue gas pipeline and is positioned at the downstream of the dust remover. And a fourth temperature measuring point is arranged on the original flue gas conveying pipeline and at the downstream of the position where the bypass flue gas pipeline is combined to the original flue gas conveying pipeline.
Preferably, the apparatus further comprises a waste water storage tank. The waste water storage tank is connected to the waste water inlet of the atomizer through a waste water input pipeline. Preferably, a waste water pump is arranged on the waste water input pipeline. Preferably, a waste water temperature detection device is arranged in the waste water storage tank.
Preferably, the air duct is provided with an air temperature detecting device.
Preferably, a flow meter is arranged on the raw flue gas conveying pipeline and upstream of the first temperature measuring point.
Preferably, the bypass flue gas pipeline is provided with a second booster fan, and the second booster fan is arranged at the downstream of the dust remover.
Preferably, the apparatus further comprises a chimney. The adsorption tower is provided with an adsorption tower smoke outlet, and the adsorption tower smoke outlet is connected to a chimney through a raw smoke conveying pipeline.
In the invention, the first booster fan is arranged on the raw flue gas conveying pipeline. The first booster fan is arranged to enable the flue gas to flow along the flue gas pipeline and enter the adsorption tower to provide power. Therefore, the specific position of the first booster fan arranged on the original flue gas conveying pipeline is not limited, and the requirement that the flue gas enters the adsorption tower to provide power can be met. For example, a first booster fan may be provided downstream of the location where the bypass flue gas duct merges into the raw flue gas delivery duct; or may be provided upstream of the point at which the raw flue gas duct merges into the raw flue gas duct.
In the invention, the second booster fan is arranged on a bypass flue gas pipeline which is branched from the original flue gas conveying pipeline. The second booster fan is arranged to provide power for the flue gas to enter the bypass flue gas pipeline. Correspondingly, the specific position of the second booster fan arranged on the bypass flue gas pipeline is not limited, and the requirement that power is provided for flue gas entering the bypass flue gas pipeline can be met. For example, a second booster fan may be provided downstream of the atomizer; or may be located upstream of the atomizer.
The invention relates to a flue gas purification method comprising flue gas temperature control, which comprises the following steps of firstly, according to the fact that the heat released by flue gas is equal to the heat absorbed by waste water when the flue gas and the waste water in a bypass flue gas pipeline exchange heat, calculating the amount of the flue gas which needs to enter the bypass flue gas pipeline under the condition of treating corresponding waste water amount by a formula (3); then, the heat released by the flue gas is equal to the heat absorbed by the cold air when the heat exchange is carried out between the flue gas and the cold air in the original flue gas conveying pipeline, namely, the amount of the cold air required to be introduced into the original flue gas conveying pipeline is calculated by the formula (7); finally, the temperature T4 of the fourth temperature measuring point (namely the flue gas temperature at the inlet of the adsorption tower) is controlled to be at the target temperature T4 by adjusting the amount of the flue gas entering the bypass flue gas pipeline and the amount of the cold air introduced into the original flue gas conveying pipelineIs provided withThe range of + -t ℃, i.e. at 100 ℃ and 145 ℃, preferably at 110 ℃ and 140 ℃.
In the present invention, the specific heat capacity of each substance in the temperature range in the corresponding pipe is as follows:
specific heat capacity C of flue gasCigarette with heating means1.005-1.026 kJ/(kg ℃); heat of vaporization r of waste waterWater (W)2307.8-2457.7 kJ/kg; specific heat capacity of water vapor CWater vapour1.864-1.930 kJ/(kg. DEG C); specific heat capacity C of cold airQi (Qi)1.005-1.009 kJ/(kg. DEG C); specific heat capacity C of mixed gas of flue gas and waste water11.009-1.032 kJ/(kg. DEG C); specific heat capacity C of mixed gas of flue gas and cold air2＝1.009～1.017kJ/(kg·℃)。
In the invention, the dust remover is arranged at the downstream of the atomizer, and harmful substances in the wastewater can be discharged out of the whole device through the dust remover after being converted into salt substances, so that the harmful elements in the wastewater can be effectively prevented from corroding system equipment, and the problem that the wastewater can not be used as a water source for cooling flue gas in the prior art is solved.
In the invention, in the industries of steel, electric power, nonferrous metal, petrifaction, chemical industry or building materials and the like, because the used raw materials are various, the flue gas containing various pollutants is often generated, and the flue gas contains SO2NOx, dust, VOCs, heavy metals, and the like. The multi-pollutant flue gas is subjected to adsorption treatment, and an adsorbent (such as activated carbon) adsorbing the multi-pollutants is subjected to desorption treatment and is recycled; in the process of desorption, the generated desorption gas is washed, a large amount of wastewater is generated in the washing process, and the desorption gas washing wastewater is not effectively treated, so that the environment is seriously polluted. The invention utilizes the heat of the original flue gas (such as the original sintering flue gas) to treat the waste water generated in the processes of desorption, desorption gas treatment and the like. The method has the advantages of synergistic treatment of flue gas and wastewater, low operation cost, less equipment investment, clean treatment and effective control of secondary pollution, and realizes zero discharge of wastewater.
In the invention, all the wastewater to be treated is evaporated by the waste heat of the original flue gas, then is dedusted and is conveyed to the adsorption tower for treatment, thereby realizing zero discharge of the wastewater. The waste water is conveyed to an original flue gas conveying pipeline for treatment, but if all the original flue gas is mixed with the waste water, the waste water contains impurities such as metal ions, chloride ions, fluoride ions, sulfate ions and the like; the waste water and the flue gas can generate crystals after being mixed, and the crystals can be conveyed to an adsorption tower only after being subjected to dust removal treatment; otherwise, the flue gas of mixing this type of waste water will seriously influence the performance of active carbon in the adsorption tower for adsorption effect discounts greatly, will seriously make active carbon thoroughly inactivate, causes the waste of resource. If waste water and all flue gases are mixed and then undergo the dust removal process, the amount of the flue gases to be treated is large, so that the dust removal work in the whole process flow is greatly increased, the cost is increased, the investment of dust removal equipment is large, and the loss is larger.
Therefore, the invention divides the original flue gas conveying pipeline for conveying the high-temperature flue gas into the bypass flue gas pipeline, guides one part of the original flue gas into the bypass flue gas pipeline, dries and crystallizes the waste water through the flue gas in the bypass flue gas pipeline, and then conveys the mixed gas of the flue gas and the waste water after mixing the part of the waste water and the flue gas to the adsorption tower for subsequent treatment through dust removal treatment. According to the technical scheme, only part of flue gas used for mixing the wastewater and the mixed gas after the wastewater is atomized are treated, and the rest of flue gas which does not pass through the bypass flue gas pipeline does not need to be subjected to dust removal treatment, so that the workload of dust removal is greatly reduced, the energy is saved, and the investment is reduced.
According to the waste water amount to be treated, the amount of the flue gas entering the bypass flue gas pipeline is accurately controlled, so that the flue gas entering the bypass flue gas pipeline can just treat the part of waste water. If the flue gas introduced into the bypass flue gas pipeline is too little, the wastewater treatment is incomplete, and the significance of the invention is lost; if the flue gas that introduces bypass flue gas pipeline is too much, will make the flue gas in the bypass flue gas pipeline surplus, handle waste water and need not surplus flue gas, because the flue gas in the bypass flue gas pipeline all need handle through the dust remover, consequently, the too much work load that will increase the dust removal of flue gas that introduces bypass flue gas pipeline, and is also stricter to the requirement of dust remover, has increased the input cost. According to the invention, the amount of the flue gas introduced into the bypass flue gas pipeline is accurately controlled, so that the part of the flue gas can just treat the wastewater to be treated, and the extra workload of dust removal is not increased. And removing the flue gas introduced into the bypass flue gas pipeline, and directly conveying the residual part of the flue gas to the adsorption tower through the original flue gas conveying pipeline, wherein the part of the flue gas is cooled by adding cold air, so that the temperature of the flue gas at the inlet of the adsorption tower is regulated within a specified range.
If the temperature of the flue gas input into the adsorption tower is too low, the temperature condition of removing pollutants by the activated carbon cannot be achieved, so that the adsorption effect of the activated carbon is poor, and the aim of purifying the flue gas cannot be achieved; if the temperature of the flue gas input into the adsorption tower is too high, the activated carbon in the adsorption tower is inactivated due to high temperature, and the adsorption function is lost. Therefore, it is important to accurately control the flue gas temperature at the inlet of the adsorption tower. According to the invention, the temperature of the flue gas entering the adsorption tower is ensured to be adjusted within a proper range by accurately controlling the temperature of the flue gas of the bypass flue gas pipeline and the temperature of the flue gas of the original flue gas conveying pipeline.
In the invention, the original flue gas conveying pipeline for conveying the high-temperature flue gas is divided into the bypass flue gas pipeline, and the flue gas enters the adsorption tower through the original flue gas conveying pipeline and the bypass flue gas pipeline. The waste water is mixed with the flue gas in the bypass flue gas pipeline, so that the waste water is mixed with the flue gas to form flue gas and waste water mixed gas; the purpose of treating the wastewater is achieved. Because the wastewater contains metal ions, chloride ions, fluoride ions, sulfate ions and other substances, after the wastewater is conveyed to the bypass flue gas pipeline, the wastewater can be dried by utilizing the flue gas in the bypass flue gas pipeline, so that ions in the wastewater form crystal salt; such as chloride, fluoride, sulfate, and the like; in the mixed gas of the flue gas and the waste water after mixing, because ions are contained in the waste water before forming crystallized salt, the crystallized salt is discharged from a solid outlet of a dust remover through dust removal treatment; the crystallized salt is recovered and can be sold or used for other purposes, resulting in economic value. Therefore, the technical scheme of the invention not only treats the wastewater containing impurities, but also can recover by-product crystalline salt to generate economic value; in addition, the waste water sprayed into the bypass flue gas pipeline also plays a role in regulating the temperature of the flue gas entering the adsorption tower, so that the flue gas entering the adsorption tower is controlled within a temperature range suitable for activated carbon adsorption treatment. The flue gas in the original flue gas conveying pipeline is subjected to temperature regulation by adding cold air, so that the flue gas entering the adsorption tower is controlled within a temperature range suitable for activated carbon adsorption treatment.
In the invention, the heat quantity required by the wastewater treatment is calculated according to the quantity of the wastewater to be treated and the temperature of the flue gas entering the adsorption tower. The heat required by the wastewater treatment is provided by the flue gas in the bypass flue gas pipeline, and the amount of the flue gas entering the bypass flue gas pipeline can be accurately calculated according to the temperature of the original flue gas; therefore, through adjustment and control, the amount of the flue gas entering the bypass flue gas pipeline can just completely treat the wastewater, and the surplus condition can not exist, so that the load of dust removal treatment can not be additionally increased; in addition, through accurate control, the temperature of the flue gas entering the adsorption tower can be controlled within a temperature range suitable for activated carbon adsorption treatment.
In the invention, the raw flue gas is divided into two parts, and one part is used for treating wastewater through the bypass flue gas pipeline; the other part is conveyed to the adsorption tower through a raw flue gas conveying pipeline. The temperature of the flue gas entering the adsorption tower is controlled by the temperature of the flue gas conveyed by the original flue gas conveying pipeline, and the temperature of the flue gas is adjusted by adding cold air. According to the technical scheme, the heat quantity to be released by the part of flue gas can be calculated according to the temperature of the original flue gas, the flue gas quantity in the pipeline and the temperature of the flue gas entering the adsorption tower. The released heat is treated by the added cold air, and the amount of the cold air needing to be added can be accurately calculated according to the temperature of the cold air, so that the temperature of the flue gas entering the adsorption tower is controlled within the temperature range suitable for the adsorption treatment of the activated carbon. If too much cold air is added, the temperature of the flue gas entering the adsorption tower is too low, and the adsorption effect is influenced; if the added cold air is too little, the temperature of the flue gas entering the adsorption tower is too high, and the activated carbon in the adsorption tower is inactivated due to high temperature, even loses the adsorption function. Therefore, the amount of the added cold air needs to be accurately controlled, and the stability, the high efficiency and the smoothness of the subsequent process can be ensured.
In the invention, the amount of flue gas entering the bypass flue gas pipeline can be adaptively adjusted according to the amount of the wastewater to be treated. Meanwhile, the amount of added cold air and the amount of flue gas entering the bypass flue gas pipeline can be adaptively adjusted according to the temperature of the flue gas entering the adsorption tower.
In the invention, the temperature of the mixed gas of the flue gas and the waste water after the waste water and the flue gas in the bypass flue gas pipeline are mixed can be set to the temperature required by the flue gas entering the adsorption tower, the temperature of the mixed gas of the flue gas and the cold air after the flue gas and the cold air in the original flue gas conveying pipeline are also set to the temperature required by the flue gas entering the adsorption tower, and the two paths of gases are mixed, the temperature is unchanged and are conveyed to the adsorption tower, so that the temperature of the flue gas entering the adsorption tower is controlled within the temperature range suitable for the adsorption treatment of the activated carbon. It can also be: setting the temperature of the mixed gas of the waste water and the waste water after the waste water and the flue gas are mixed in the bypass flue gas pipeline to be lower than the temperature required by the flue gas entering the adsorption tower, and setting the original flue gas conveying pipelineThe temperature of the mixed gas of the flue gas and the cold air after the inner flue gas and the cold air are mixed is higher than the temperature required by the flue gas entering the adsorption tower, and then the temperature is calculated by the formula (10) according to the flue gas amount in the two flue gas pipelines, so that the temperature of the flue gas entering the adsorption tower is controlled within the temperature range suitable for the adsorption treatment of the active carbon after the flue gas in the two flue gas pipelines is mixed. The method can also be as follows: the temperature of the flue gas and the waste water mixed gas after the waste water and the flue gas are mixed in the bypass flue gas pipeline is set to be higher than the temperature required by the flue gas entering the adsorption tower, the temperature of the flue gas and the cold air mixed gas after the flue gas and the cold air are mixed in the original flue gas conveying pipeline is set to be lower than the temperature required by the flue gas entering the adsorption tower, calculation is carried out according to the flue gas amount in the two flue gas pipelines by the formula (10), and after the flue gas in the two flue gas pipelines is mixed, the temperature of the flue gas entering the adsorption tower is controlled within the temperature range suitable for active carbon adsorption treatment. In addition, according to the technical scheme of the invention, on the premise of completely treating the wastewater, T2 is adjusted according to the smoke volume in the bypass smoke pipeline and the smoke volume in the original smoke conveying pipelineIs provided withAnd T3Is provided withThe temperature value ensures that the temperature of the flue gas entering the adsorption tower is controlled within the temperature range suitable for the adsorption treatment of the activated carbon after the two paths of flue gas are mixed, namely T4 is regulated or controlled at T4Is provided withThe range of +/-t ℃.
In the invention, the flue gas temperature T2 in the flue at the corresponding position is detected to be higher than T2 on line according to the second temperature measuring pointIs provided withIncreasing the amount of cold air introduced into the original flue gas conveying pipeline; if T2 is lower than T2Is provided withThe amount of cold air introduced into the raw flue gas duct is reduced. Detecting that the temperature T3 of the flue gas in the flue at the corresponding position is higher than T3 on line according to the third temperature measuring pointIs provided withThe amount of flue gas entering the bypass flue gas pipeline is reduced; if T3 is lower than T3Is provided withThe amount of flue gas entering the bypass flue gas duct is increased. Detecting that the temperature T4 of the flue gas in the flue at the corresponding position is higher than T4 on line according to the fourth temperature measuring pointIs provided withIncreasing the amount of cold air introduced into the original flue gas conveying pipeline, and/or reducing the amount of flue gas entering the bypass flue gas pipeline on the premise of completely treating wastewater; if T4 is lower than T4Is provided withThe amount of cold air introduced into the original flue gas conveying pipeline is reduced, and/or the amount of flue gas entering the bypass flue gas pipeline is properly increased on the premise that wastewater can be completely treated.
In the invention, the amount of the flue gas entering the bypass flue gas pipeline is calculated according to the amount of the wastewater to be treated. In an actual operation process, the flue gas and the waste water of the bypass flue gas pipeline are often synchronously conveyed to the bypass flue gas pipeline; according to the amount of the waste water and the amount of the flue gas entering the bypass flue gas pipeline, the speed of the waste water entering the bypass flue gas pipeline and the speed of the flue gas entering the bypass flue gas pipeline are adjusted, so that the flue gas entering the bypass flue gas pipeline can just completely treat the waste water, and zero discharge of the waste water is realized. The speed of the waste water input into the bypass flue gas pipeline is controlled by a waste water pump. The rate of flue gas entering the bypass flue gas duct is controlled by a bypass valve.
In the present application, "upstream" and "downstream" are set according to the direction of the flow of the flue gas in the duct. The "bottom" is set according to the height direction of the apparatus or device.
Compared with the prior art, the invention has the following beneficial effects:
1. according to the method and the device, the original flue gas conveying pipeline is adopted to divide the bypass flue gas pipeline, all the waste water is sprayed into the bypass flue gas pipeline to cool the bypass flue gas, and the waste water is dedusted, so that the waste water which is difficult to treat at ordinary times is reasonably treated, and the flue gas temperature control can be realized;
2. according to the invention, flue gas in the bypass flue gas pipeline is sprayed into waste water to be cooled, flue gas in the original flue gas conveying pipeline is cooled by introducing cold air, two paths of flue gas after being cooled are mixed, and the flue gas temperature is accurately controlled finally according to the condition that the heat absorbed by low-temperature substances is equal to the heat emitted by high-temperature substances in the heat exchange processes for several times;
3. the flue gas has high temperature, and can be purified only after being cooled by supplementing a large amount of air, the flue gas bypass cooling device sprays the bypass flue gas into the waste water to cool, and the waste water is evaporated by utilizing the waste heat of the flue gas, so that the energy waste is reduced; the wastewater is reasonably treated, and the cost input of wastewater treatment is reduced; meanwhile, the amount of supplemented air is reduced, and the operating cost of the flue gas purification device is reduced;
4. the method and the device are simple to operate, complex pipeline equipment and reaction devices are not required to be invested, the whole device is stable to operate, and the investment cost is low.
Drawings
FIG. 1 is a flow chart of a process for cooling flue gas in the prior art;
FIG. 2 is a process flow diagram of a flue gas purification method including flue gas temperature control according to the present invention;
fig. 3 is a schematic diagram of a flue gas cleaning apparatus including flue gas temperature control according to the present invention.
Reference numerals: 1: an adsorption tower; 101: a flue gas inlet of the adsorption tower; 102: a flue gas outlet of the adsorption tower; 2: an atomizer; 201: a flue gas inlet; 202: a flue gas outlet; 203: a wastewater inlet; 3: a dust remover; 301: a gas inlet; 302: a gas outlet; 303: a solids outlet; 4: a waste water storage tank; 5: a waste water pump; 6: a bypass valve; 7: a flow meter; 8: a cold air valve; 9: a chimney; 10: a first booster fan; 11: a wastewater temperature detection device; 12: an air temperature detection device; 13: a second booster fan;
l1: an original flue gas conveying pipeline; l2: a bypass flue gas duct; l3: a wastewater input pipeline; l4: an air duct;
p1: a first temperature measuring point; p2: a second temperature measurement point; p3: a third temperature measurement point; p4: and a fourth temperature measuring point.
Detailed Description
According to a first embodiment of the invention, there is provided a flue gas purification process comprising flue gas temperature control:
a method of flue gas purification including flue gas temperature control, the method comprising the steps of:
1) a raw flue gas conveying pipeline L1 for conveying high-temperature flue gas to the activated carbon adsorption tower 1 is divided into a bypass flue gas pipeline L2, and the flue gas enters the adsorption tower 1 through the raw flue gas conveying pipeline L1 and the bypass flue gas pipeline L2;
2) the method comprises a flue gas temperature control step or a flue gas temperature regulation step, wherein the flue gas temperature regulation step comprises the following substeps:
① temperature control of flue gas of a bypass flue gas pipeline L2, wherein an atomizer 2 is arranged on a bypass flue gas pipeline L2, wastewater is atomized by the atomizer 2 and then mixed with the flue gas in the bypass flue gas pipeline L2, and the wastewater exchanges heat with the flue gas entering the bypass flue gas pipeline L2 to form a mixed gas of the flue gas and the wastewater, preferably, the mixed gas of the flue gas and the wastewater is dedusted by a deduster 3, and impurities in the mixed gas of the flue gas and the wastewater are discharged from a solid outlet 303 of the deduster 3;
② temperature control of flue gas in the original flue gas conveying pipeline L1, namely, introducing cold air into the original flue gas conveying pipeline L1 to regulate the temperature of the flue gas in the original flue gas conveying pipeline L1 at the downstream of the position where the original flue gas conveying pipeline L1 branches out of the bypass flue gas pipeline L2;
③ the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline L2 is merged to the original flue gas conveying pipeline L1, and is mixed with the flue gas in the original flue gas conveying pipeline L1 after the temperature is controlled or adjusted by cold air, and then the mixed gas enters the adsorption tower 1, wherein the temperature of the flue gas at the inlet of the adsorption tower 1 is adjusted in a specified range;
3) the mixed flue gas enters the activated carbon adsorption tower 1, is adsorbed and purified by the activated carbon in the adsorption tower 1 and then is discharged, and the activated carbon adsorbing pollutants in the flue gas is discharged from the bottom of the adsorption tower 1.
Preferably, in sub-step ① of the above method, the wastewater is fed from the wastewater tank 4 to the atomizer 2 along the wastewater inlet line L3. preferably, the wastewater in the wastewater tank 4 is neutral or alkaline. preferably, the wastewater inlet line L3 is provided with a wastewater pump 5, and the wastewater pump 5 powers the wastewater into the atomizer 2.
Preferably, in sub-step ② of the above method, the cool air is delivered from the air duct L4 to the raw flue gas delivery duct L1.
Preferably, in step 2) of the method, the first temperature measurement point P1 is provided upstream of the point at which the raw flue gas duct L1 branches off the bypass flue gas duct L2. A second temperature measurement point P2 is provided between the point at which the raw flue gas duct L1 is fed with cold air and the point at which the bypass flue gas duct L2 merges into the raw flue gas duct L1. On the bypass flue gas duct L2 and downstream of the dust separator 3A third temperature measurement point P3 is set. A fourth temperature measuring point P4 is provided on the raw flue gas duct L1 downstream of the point where the bypass flue gas duct L2 merges into the raw flue gas duct L1. The first temperature measuring point P1 detects the flue gas temperature T1 in the flue at the corresponding position on line. The second temperature measuring point P2 detects the flue gas temperature T2 in the flue at the corresponding position on line. The third temperature measuring point P3 detects the flue gas temperature T3 in the flue at the corresponding position on line. The fourth temperature measuring point P4 detects the flue gas temperature T4 in the flue at the corresponding position on line. Wherein the target or set temperature value at the fourth temperature measurement point P4 is T4Is provided with。
According to the heat Q released by the flue gas entering the bypass flue gas pipeline L2Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct L2Water (W)And equalising, calculating and adjusting the amount of flue gas entering the bypass flue gas duct L2 in sub-step ①, further dependent on the heat Q released by the flue gas entering the adsorption tower 1 through the raw flue gas duct L1Cigarette 2Heat Q absorbed by cold air introduced into the raw flue gas duct L1Qi (Qi)And equally, calculating and adjusting the amount of cold air introduced into the raw flue gas conveying pipeline L1 in the substep ②, adjusting or controlling the temperature T4 of the fourth temperature measuring point P4 to be T4 by adjusting the amount of flue gas entering the bypass flue gas pipeline L2 and the amount of cold air introduced into the raw flue gas conveying pipeline L1Is provided withA temperature range of + -t deg.C, wherein t deg.C is in the range of 1-5 deg.C.
Preferably, the target or set temperature value T4 at the fourth temperature measuring point P4Is provided withThe temperature is 100-145 ℃, preferably 110-140 ℃; i.e., the temperature of the flue gas at the inlet of the adsorption column 1 is adjusted within a prescribed range, for example, within the range of 100 ℃ and 145 ℃, preferably within the range of 110 ℃ and 140 ℃.
Preferably, said heat Q released according to the fumes entering the bypass fume duct L2Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct L2Water (W)And (3) equally, calculating and adjusting the amount of the flue gas entering the bypass flue gas pipeline L2 in the substep ①, specifically:
the first temperature measuring point P1 detects the temperature of the original flue gas as T1, and the temperature of the mixed gas of the flue gas and the waste water at the position of the third temperature measuring point P3 is set as T3Is provided withWherein:T3is provided withThe temperature is 100-160 ℃, and the value is preferably within the range of 110-140 ℃;
a) calculating the heat required by wastewater treatment: a liquid level meter is arranged in the waste water storage tank 4, and the waste water quantity M to be treated in the waste water storage tank 4 is obtained according to the liquid level meterWater (W)Detecting the initial temperature of the wastewater as TWater (W)Whereby the amount of heat Q to be absorbed for treating the waste water in the waste water tank 4Water (W)Comprises the following steps:
Qwater (W)＝MWater (W)rWater (W)+CWater vapourMWater (W)ΔTWater (W)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (1)，
In the formula (1), rWater (W)Is the heat of vaporization of the waste water, CWater vapourThe specific heat capacity of water vapor;
b) the required flue gas volume of the bypass flue gas pipeline L2 is calculated: the amount of the flue gas entering the bypass flue gas pipeline L2 is set as M1Whereby the heat Q released by the flue gas entering the bypass flue gas duct L2Cigarette 1Comprises the following steps:
Qcigarette 1＝CCigarette with heating meansM1ΔTCigarette 1＝CCigarette with heating meansM1(T1-T3Is provided with) (2)，
C in formula (2)Cigarette with heating meansThe specific heat capacity of the flue gas;
heat Q released by the flue gas entering the bypass flue gas duct L2Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct L2Water (W)Equality, we can get:
Ccigarette with heating meansM1(T1-T3Is provided with)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (3)，
Obtaining the following components:
M1＝Mwater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W)))/(CCigarette with heating means(T1-T3Is provided with)) (4)；
The opening degree of the bypass valve 6 on the bypass flue gas pipeline L2 is adjusted so that the amount of the flue gas entering the bypass flue gas pipeline L2 is M1。
Preferably, the further oneAccording to the heat Q released by the flue gas entering the adsorption tower 1 through the raw flue gas conveying pipeline L1Cigarette 2Heat Q absorbed by cold air introduced into the raw flue gas duct L1Qi (Qi)And (3) equally, calculating and adjusting the amount of cold air introduced into the original flue gas conveying pipeline L1 in the substep ②, specifically:
the flow meter 7 upstream of the first temperature measurement point P1 measures the total amount of flue gas as M0The first temperature measuring point P1 detects the temperature of the original smoke as T1, and the temperature of the mixed gas of the smoke and the cold air at the position of the second temperature measuring point P2 is set as T2Is provided withWherein: t2Is provided withThe temperature is 100-160 ℃, and the value is preferably within the range of 110-140 ℃;
a) calculating the heat quantity required to be released by the raw flue gas in the raw flue gas conveying pipeline L1: the amount of the flue gas introduced into the adsorption tower 1 through the raw flue gas transfer duct L1 is (M)0-M1) The heat Q released by the flue gas entering the adsorption tower 1 through the raw flue gas duct L1Cigarette 2Comprises the following steps:
Qcigarette 2＝CCigarette with heating means(M0-M1)ΔTCigarette 2＝CCigarette with heating means(M0-M1)(T1-T2Is provided with) (5)，
b) The amount of cold air introduced into the original flue gas conveying pipeline L1 is calculated: the quantity of cold air introduced into the original flue gas conveying pipeline L1 is set as MQi (Qi)Measuring the initial temperature of the cold air as TQi (Qi)Accordingly, the heat Q absorbed by the cold air introduced into the raw flue gas duct L1Qi (Qi)Comprises the following steps:
Qqi (Qi)＝CQi (Qi)MQi (Qi)ΔTQi (Qi)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (6)，
C in formula (6)Qi (Qi)Is the specific heat capacity of the cold air;
the heat Q released by the flue gas entering the adsorption column 1 through the raw flue gas duct L1Cigarette 2Heat Q absorbed by cold air introduced into the raw flue gas duct L1Qi (Qi)Equality, we can get:
Ccigarette with heating means(M0-M1)(T1-T2Is provided with)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (7)；
Obtaining the following components:
Mqi (Qi)＝CCigarette with heating means(M0-M1)(T1-T2Is provided with)/(CQi (Qi)(T2Is provided with-TQi (Qi))) (8)；
The opening degree of a cold air valve 8 on the air pipeline L4 is adjusted, so that the quantity of cold air introduced into the original flue gas conveying pipeline L1 is MQi (Qi)。
Preferably, the temperature T4 of the fourth temperature measuring point P4 is adjusted or controlled at T4 by adjusting the amount of flue gas entering the bypass flue gas duct L2 and the amount of cold air passing into the raw flue gas conveying duct L1Is provided withThe range of +/-t ℃ is as follows:
the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline L2 is mixed with the mixed gas of the flue gas and the cold air in the original flue gas conveying pipeline L1 after the temperature of the flue gas and the cold air is controlled or regulated by the cold air, after the two paths of gases exchange heat, the temperature T4 of a fourth temperature measuring point P4 is regulated or controlled at T4Is provided withThe range of +/-t ℃. The heat Q absorbed (or released) by the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline L2Smoke and waterThe heat Q released (or absorbed) by the mixed gas of the flue gas and the cold air in the raw flue gas conveying pipeline L1Smoke and gasEqual, i.e.:
Qsmoke and water＝QSmoke and gas(9)，
Namely: c1(M1+MWater (W))(T4Is provided with-T3Is provided with)＝C2(M0-M1+MQi (Qi))(T2Is provided with-T4Is provided with) (10)，
C in formula (10)1The specific heat capacity of the mixed gas of the flue gas and the waste water; c2Is the specific heat capacity of the mixed gas of the flue gas and the cold air.
Preferably, T2Is provided with＝T3Is provided with＝T4Is provided with。
Preferably, the flue gas temperature T2 in the flue at the corresponding position is detected on line according to the second temperature measuring point P2. If T2 equals T2Is provided withContinuing to operate; t2 not equal to T2Is provided withThe quantity of cold air introduced into the original flue gas duct L1 is adjusted so that T2 equals T2Is provided with。
And detecting the flue gas temperature T3 in the flue at the corresponding position on line according to a third temperature measuring point P3. If T3 equals T3Is provided withContinuing to operate; t3 not equal to T3Is provided withAdjusting the amount of flue gas entering the bypass flue gas duct L2 such that T3 equals T3Is provided with。
And detecting the flue gas temperature T4 in the flue at the corresponding position on line according to a fourth temperature measuring point P4. If T4 equals T4Is provided withContinuing to operate; t4 not equal to T4Is provided withThe amount of cold air passing into the original flue gas duct L1 and the amount of flue gas entering the bypass flue gas duct L2 are adjusted so that T4 equals T4Is provided with。
Preferably, in step 3) of the above method, the flue gas adsorbed and purified by the activated carbon in the adsorption tower 1 is discharged through a chimney 9.
According to a second embodiment of the invention, there is provided a flue gas cleaning device comprising a flue gas temperature control:
a flue gas purification device comprising flue gas temperature control or a flue gas purification device used for the method comprises an adsorption tower 1, wherein an adsorption tower flue gas inlet 101 is arranged on the adsorption tower 1. The adsorption tower flue gas inlet 101 is connected with a raw flue gas conveying pipeline L1. The original flue gas conveying pipeline L1 branches into a bypass flue gas pipeline L2. The bypass flue gas pipeline L2 is sequentially provided with an atomizer 2 and a dust remover 3. The atomizer 2 is provided with a flue gas inlet 201, a flue gas outlet 202 and a waste water inlet 203. The dust remover 3 is provided with a gas inlet 301, a gas outlet 302 and a solid outlet 303. The bypass flue gas pipeline L2 passes through the atomizer 2 and the dust remover 3 and then is combined to the original flue gas conveying pipeline L1. The atomizer 2 is arranged upstream of the dust separator 3.
The original flue gas conveying pipeline L1 is provided with a first booster fan 10. The first booster fan 10 is disposed downstream of the point where the bypass flue gas duct L2 merges into the raw flue gas duct L1.
An air pipeline L4 is connected to the original flue gas conveying pipeline L1. The air duct L4 is connected between the point at which the raw flue gas duct L1 branches off the bypass flue gas duct L2 and the point at which the bypass flue gas duct L2 merges into the raw flue gas duct L1.
Preferably, the apparatus further comprises a bypass valve 6 disposed on the bypass flue gas duct L2. The bypass valve 6 is located upstream of the atomizer 2.
Preferably, the apparatus further comprises a cold air valve 8 provided on the air duct L4.
In the present invention, a first temperature measurement point P1 is provided upstream of the point at which the raw flue gas duct L1 branches into the bypass flue gas duct L2. A second temperature measurement point P2 is provided between the location where the raw flue gas duct L1 joins the air duct L4 and the location where the bypass flue gas duct L2 merges into the raw flue gas duct L1. A third temperature measuring point P3 is provided on the bypass flue gas duct L2 and downstream of the precipitator 3. A fourth temperature measuring point P4 is provided on the raw flue gas duct L1 downstream of the point where the bypass flue gas duct L2 merges into the raw flue gas duct L1.
Preferably, the apparatus further comprises a waste water storage tank 4. The waste water tank 4 is connected to the waste water inlet 203 of the atomizer 2 through a waste water input line L3. Preferably, a waste water pump 5 is arranged on the waste water input pipeline L3. Preferably, a waste water temperature detecting device 11 is provided in the waste water storage tank 4.
Preferably, the air duct L4 is provided with an air temperature detecting device 12.
Preferably, a flow meter 7 is provided on the raw flue gas delivery line L1 upstream of the first temperature measurement point P1.
Preferably, a second booster fan 13 is arranged on the bypass flue gas duct L2, and the second booster fan 13 is arranged downstream of the dust separator 3.
Preferably, the device further comprises a chimney 9. The adsorption tower 1 is provided with an adsorption tower flue gas outlet 102, and the adsorption tower flue gas outlet 102 is connected to the chimney 9 through an original flue gas conveying pipeline L1.
Example 1
As shown in fig. 3, a flue gas purification device including flue gas temperature control comprises an adsorption tower 1, wherein an adsorption tower flue gas inlet 101 is arranged on the adsorption tower 1. The adsorption tower flue gas inlet 101 is connected with a raw flue gas conveying pipeline L1. The original flue gas conveying pipeline L1 branches into a bypass flue gas pipeline L2. The bypass flue gas pipeline L2 is sequentially provided with an atomizer 2 and a dust remover 3. The atomizer 2 is provided with a flue gas inlet 201, a flue gas outlet 202 and a waste water inlet 203. The dust remover 3 is provided with a gas inlet 301, a gas outlet 302 and a solid outlet 303. The bypass flue gas pipeline L2 passes through the atomizer 2 and the dust remover 3 and then is combined to the original flue gas conveying pipeline L1. The atomizer 2 is arranged upstream of the dust separator 3.
The original flue gas conveying pipeline L1 is provided with a first booster fan 10. The first booster fan 10 is disposed downstream of the point where the bypass flue gas duct L2 merges into the raw flue gas duct L1.
An air pipeline L4 is connected to the original flue gas conveying pipeline L1. The air duct L4 is connected between the point at which the raw flue gas duct L1 branches off the bypass flue gas duct L2 and the point at which the bypass flue gas duct L2 merges into the raw flue gas duct L1.
The arrangement also includes a bypass valve 6 provided on the bypass flue gas duct L2. The bypass valve 6 is located upstream of the atomizer 2. The apparatus further includes a cool air valve 8 provided on the air duct L4.
A first temperature measurement point P1 is provided upstream of the point at which the raw flue gas duct L1 branches off the bypass flue gas duct L2. A second temperature measurement point P2 is provided between the location where the raw flue gas duct L1 joins the air duct L4 and the location where the bypass flue gas duct L2 merges into the raw flue gas duct L1. A third temperature measuring point P3 is provided on the bypass flue gas duct L2 and downstream of the precipitator 3. A fourth temperature measuring point P4 is provided on the raw flue gas duct L1 downstream of the point where the bypass flue gas duct L2 merges into the raw flue gas duct L1.
The apparatus also includes a waste water storage tank 4. The waste water tank 4 is connected to the waste water inlet 203 of the atomizer 2 through a waste water input line L3. A waste water pump 5 is arranged on the waste water input pipeline L3. A waste water temperature detection device 11 is arranged in the waste water storage tank 4.
The air duct L4 is provided with an air temperature detection device 12.
A flowmeter 7 is arranged on the original flue gas conveying pipeline L1 and upstream of the first temperature measuring point P1.
The bypass flue gas pipeline L2 is provided with a second booster fan 13, and the second booster fan 13 is arranged at the downstream of the dust remover 3.
The device also comprises a chimney 9. The adsorption tower 1 is provided with an adsorption tower flue gas outlet 102, and the adsorption tower flue gas outlet 102 is connected to the chimney 9 through an original flue gas conveying pipeline L1.
Example 2
A flue gas purification method including flue gas temperature control, using the apparatus of example 1, the method comprising the steps of:
1) a raw flue gas conveying pipeline L1 for conveying high-temperature flue gas to the activated carbon adsorption tower 1 is divided into a bypass flue gas pipeline L2, and the flue gas enters the adsorption tower 1 through the raw flue gas conveying pipeline L1 and the bypass flue gas pipeline L2;
2) the method comprises a flue gas temperature control step or a flue gas temperature regulation step, wherein the flue gas temperature regulation step comprises the following substeps:
① temperature control of flue gas of a bypass flue gas pipeline L2, wherein an atomizer 2 is arranged on a bypass flue gas pipeline L2, wastewater is atomized by the atomizer 2 and then mixed with the flue gas in the bypass flue gas pipeline L2, and the wastewater exchanges heat with the flue gas entering the bypass flue gas pipeline L2 to form a mixed gas of the flue gas and the wastewater, the mixed gas of the flue gas and the wastewater is dedusted by a deduster 3, and impurities in the mixed gas of the flue gas and the wastewater are discharged from a solid outlet 303 of the deduster 3;
② temperature control of flue gas in the original flue gas conveying pipeline L1, namely, introducing cold air into the original flue gas conveying pipeline L1 to regulate the temperature of the flue gas in the original flue gas conveying pipeline L1 at the downstream of the position where the original flue gas conveying pipeline L1 branches out of the bypass flue gas pipeline L2;
③ the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline L2 is merged to the original flue gas conveying pipeline L1, and is mixed with the flue gas in the original flue gas conveying pipeline L1 after temperature control or temperature regulation through cold air, and then the mixed gas enters the adsorption tower 1, wherein the temperature of the flue gas at the inlet of the adsorption tower 1 is regulated to be in the range of 100-145 ℃;
3) the mixed flue gas enters the activated carbon adsorption tower 1, is adsorbed and purified by the activated carbon in the adsorption tower 1 and then is discharged, and the activated carbon adsorbing pollutants in the flue gas is discharged from the bottom of the adsorption tower 1.
Example 3
A flue gas purification method including flue gas temperature control, using the apparatus of example 1, the method comprising the steps of:
1) a raw flue gas conveying pipeline L1 for conveying high-temperature flue gas to the activated carbon adsorption tower 1 is divided into a bypass flue gas pipeline L2, and the flue gas enters the adsorption tower 1 through the raw flue gas conveying pipeline L1 and the bypass flue gas pipeline L2;
2) the method comprises a flue gas temperature control step or a flue gas temperature regulation step, wherein the flue gas temperature regulation step comprises the following substeps:
① temperature control of flue gas bypassing flue gas duct L2:
the bypass flue gas pipeline L2 is provided with an atomizer 2, and wastewater enters the atomizer 2 from the wastewater storage tank 4 along the wastewater input pipeline L3. The wastewater in the wastewater tank 4 is alkaline. A waste water pump 5 on the waste water input line L3 powers the waste water into the atomiser 2. The waste water is atomized by the atomizer 2 and then mixed with the flue gas in the bypass flue gas pipeline L2, the waste water exchanges heat with the flue gas entering the bypass flue gas pipeline L2, the waste water is evaporated to become gaseous water, and the gaseous water is mixed with the flue gas to form mixed gas of the flue gas and the waste water; the mixed gas of the flue gas and the waste water is dedusted by the deduster 3, and impurities in the mixed gas of the flue gas and the waste water are discharged from a solid outlet 303 of the deduster 3;
② temperature control of flue gas in the original flue gas conveying pipeline L1, namely, introducing cold air into the original flue gas conveying pipeline L1 through an air pipeline L4 to regulate the temperature of the flue gas in the original flue gas conveying pipeline L1 at the downstream of the position of the bypass flue gas pipeline L2 separated from the original flue gas conveying pipeline L1;
③ the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline L2 is merged to the original flue gas conveying pipeline L1, and is mixed with the flue gas in the original flue gas conveying pipeline L1 after temperature control or temperature regulation through cold air, and then the mixed gas enters the adsorption tower 1, wherein the temperature of the flue gas at the inlet of the adsorption tower 1 is regulated to be in the range of 100-145 ℃;
wherein, a first temperature measuring point P1 is arranged at the upstream of the position of the original flue gas conveying pipeline L1 branching from the bypass flue gas pipeline L2. A second temperature measurement point P2 is provided between the point at which the raw flue gas duct L1 is fed with cold air and the point at which the bypass flue gas duct L2 merges into the raw flue gas duct L1. A third temperature measuring point P3 is provided on the bypass flue gas duct L2 and downstream of the precipitator 3. A fourth temperature measuring point P4 is provided on the raw flue gas duct L1 downstream of the point where the bypass flue gas duct L2 merges into the raw flue gas duct L1. The first temperature measuring point P1 detects the flue gas temperature T1 in the flue at the corresponding position on line. The second temperature measuring point P2 detects the temperature of the flue gas in the flue at the corresponding position on lineDegree T2. The third temperature measuring point P3 detects the flue gas temperature T3 in the flue at the corresponding position on line. The fourth temperature measuring point P4 detects the flue gas temperature T4 in the flue at the corresponding position on line. Wherein the target or set temperature value at the fourth temperature measurement point P4 is T4Is provided with＝130℃。
According to the heat Q released by the flue gas entering the bypass flue gas pipeline L2Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct L2Water (W)And equalising, calculating and adjusting the amount of flue gas entering the bypass flue gas duct L2 in sub-step ①, further dependent on the heat Q released by the flue gas entering the adsorption tower 1 through the raw flue gas duct L1Cigarette 2Heat Q absorbed by cold air introduced into the raw flue gas duct L1Qi (Qi)And equally, calculating and adjusting the amount of cold air introduced into the raw flue gas conveying pipeline L1 in the substep ②, adjusting or controlling the temperature T4 of the fourth temperature measuring point P4 to be T4 by adjusting the amount of flue gas entering the bypass flue gas pipeline L2 and the amount of cold air introduced into the raw flue gas conveying pipeline L1Is provided withRange ± t ℃, wherein t ℃ ═ 3 ℃.
The heat Q released according to the flue gas entering the bypass flue gas pipeline L2Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct L2Water (W)And (3) equally, calculating and adjusting the amount of the flue gas entering the bypass flue gas pipeline L2 in the substep ①, specifically:
the first temperature measuring point P1 detects that the temperature of the original flue gas is T1-160 ℃, and the temperature of the mixed gas of the flue gas and the waste water at the third temperature measuring point P3 is set to be T3Is provided withWherein: t3Is provided with＝120℃；
a) Calculating the heat required by wastewater treatment: a liquid level meter is arranged in the waste water storage tank 4, and the waste water quantity M to be treated in the waste water storage tank 4 is obtained according to the liquid level meterWater (W)3T/h, the initial temperature of the detected waste water is TWater (W)60 ℃, whereby the amount of heat Q to be absorbed for the treatment of the waste water in the waste water tank 4 isWater (W)Comprises the following steps:
Qwater (W)＝MWater (W)rWater (W)+CWater vapourMWater (W)ΔTWater (W)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (1)，
In the formula (1), rWater (W)Is the heat of vaporization of the waste water, rWater (W)＝2358.0kJ/kg；CWater vapourSpecific heat capacity of water vapor, CWater vapour＝1.890kJ/(kg·℃)；
b) The required flue gas volume of the bypass flue gas pipeline L2 is calculated: the amount of the flue gas entering the bypass flue gas pipeline L2 is set as M1Whereby the heat Q released by the flue gas entering the bypass flue gas duct L2Cigarette 1Comprises the following steps:
Qcigarette 1＝CCigarette with heating meansM1ΔTCigarette 1＝CCigarette with heating meansM1(T1-T3Is provided with) (2)，
C in formula (2)Cigarette with heating meansIs the specific heat capacity of the flue gas, CCigarette with heating means＝1.014kJ/(kg·℃)；
Heat Q released by the flue gas entering the bypass flue gas duct L2Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct L2Water (W)Equality, we can get:
Ccigarette with heating meansM1(T1-T3Is provided with)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (3)，
Obtaining the following components:
M1＝Mwater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W)))/(CCigarette with heating means(T1-T3Is provided with))＝135000Nm3/h (4)；
The opening degree of the bypass valve 6 on the bypass flue gas pipeline L2 is adjusted so that the amount of the flue gas entering the bypass flue gas pipeline L2 is M1。
The heat Q released further according to the flue gas entering the adsorption tower 1 through the raw flue gas conveying pipeline L1Cigarette 2Heat Q absorbed by cold air introduced into the raw flue gas duct L1Qi (Qi)And (3) equally, calculating and adjusting the amount of cold air introduced into the original flue gas conveying pipeline L1 in the substep ②, specifically:
the flow meter 7 upstream of the first temperature measurement point P1 measures the total amount of flue gas as M0＝900000Nm3The first temperature measuring point P1 detects that the temperature of the original smoke is T1-160 ℃, and a second temperature measuring point is setThe temperature of the mixed gas of the flue gas and the cold air at the position P2 is T2Is provided withWherein: t2Is provided with＝132℃；
a) Calculating the heat quantity required to be released by the raw flue gas in the raw flue gas conveying pipeline L1: the amount of the flue gas introduced into the adsorption tower 1 through the raw flue gas transfer duct L1 is (M)0-M1) The heat Q released by the flue gas entering the adsorption tower 1 through the raw flue gas duct L1Cigarette 2Comprises the following steps:
Qcigarette 2＝CCigarette with heating means(M0-M1)ΔTCigarette with heating means＝CCigarette with heating means(M0-M1)(T1-T2Is provided with) (5)，
b) The amount of cold air introduced into the original flue gas conveying pipeline L1 is calculated: the quantity of cold air introduced into the original flue gas conveying pipeline L1 is set as MQi (Qi)Measuring the initial temperature of the cold air as TQi (Qi)At 20 ℃, the heat Q absorbed by the cold air passing into the raw flue gas duct L1 is thus reducedQi (Qi)Comprises the following steps:
Qqi (Qi)＝CQi (Qi)MQi (Qi)ΔTQi (Qi)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (6)，
C in formula (6)Qi (Qi)Specific heat capacity of cold air, CQi (Qi)＝1.005kJ/(kg·℃)；
The heat Q released by the flue gas entering the adsorption column 1 through the raw flue gas duct L1Cigarette 2Heat Q absorbed by cold air introduced into the raw flue gas duct L1Qi (Qi)Equality, we can get:
Ccigarette with heating means(M0-M1)(T1-T2Is provided with)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (7)；
Obtaining the following components:
Mqi (Qi)＝CCigarette with heating means(M0-M1)(T1-T2Is provided with)/(CQi (Qi)(T2Is provided with-TQi (Qi)))＝196000Nm3/h (8)；
The opening degree of a cold air valve 8 on the air pipeline L4 is adjusted, so that the quantity of cold air introduced into the original flue gas conveying pipeline L1 is MQi (Qi)。
The temperature T4 of the fourth temperature measuring point P4 is adjusted or controlled at T4 by adjusting the amount of the flue gas entering the bypass flue gas pipeline L2 and the amount of the cold air introduced into the raw flue gas conveying pipeline L1Is provided withThe range of +/-3 ℃ is as follows:
the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline L2 is mixed with the mixed gas of the flue gas and the cold air in the original flue gas conveying pipeline L1 after the temperature is controlled or adjusted by the cold air, the two paths of gases exchange heat, and the heat Q absorbed by the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline L2Smoke and waterHeat Q released from the mixed gas of the flue gas and the cold air in the raw flue gas conveying pipeline L1Smoke and gasEqual, i.e.:
Qsmoke and water＝QSmoke and gas(9)，
Namely: c1(M1+MWater (W))(T4Is provided with-T3Is provided with)＝C2(M0-M1+MQi (Qi))(T2Is provided with-T4Is provided with) (10)，
C in formula (10)1Is the specific heat capacity of the mixed gas of the flue gas and the waste water, C1＝1.009kJ/(kg·℃)；C2Is the specific heat capacity of the mixed gas of the flue gas and the cold air, C2＝1.011kJ/(kg·℃)。
And detecting the flue gas temperature T2 in the flue at the corresponding position on line according to a second temperature measuring point P2. If T2 equals T2Is provided withContinuing to operate; t2 not equal to T2Is provided withThe quantity of cold air introduced into the original flue gas duct L1 is adjusted so that T2 equals T2Is provided with。
And detecting the flue gas temperature T3 in the flue at the corresponding position on line according to a third temperature measuring point P3. If T3 equals T3Is provided withContinuing to operate; t3 not equal to T3Is provided withAdjusting the amount of flue gas entering the bypass flue gas duct L2 such that T3 equals T3Is provided with。
And detecting the flue gas temperature T4 in the flue at the corresponding position on line according to a fourth temperature measuring point P4. If T4 equals T4Is provided withContinuing to operate; t4 not equal to T4Is provided withThe amount of cold air passing into the original flue gas duct L1 and the amount of flue gas entering the bypass flue gas duct L2 are adjusted so that T4 equals T4Is provided with。
3) The mixed flue gas enters an activated carbon adsorption tower 1, is adsorbed and purified by activated carbon in the adsorption tower 1 and then is discharged through a chimney 9, and the activated carbon adsorbing pollutants in the flue gas is discharged from the bottom of the adsorption tower 1.
Example 4
Example 3 was repeated except that the temperature T3 of the mixed gas of flue gas and wastewater at the third temperature measuring point P3 was setIs provided withThe temperature T2 of the mixed gas of the smoke and the cold air at the position of the second temperature measuring point P2Is provided withEqual and equal to the target or set temperature value T4 at the location of the fourth temperature measurement point P4Is provided withI.e. T2Is provided with＝T3Is provided with＝T4Is provided with＝130℃。

Claims (12)

1. A method of flue gas purification including flue gas temperature control, the method comprising the steps of:
1) a bypass flue gas pipeline (L2) is divided from an original flue gas conveying pipeline (L1) for conveying high-temperature flue gas to the activated carbon adsorption tower (1), and the flue gas enters the adsorption tower (1) through the original flue gas conveying pipeline (L1) and the bypass flue gas pipeline (L2);
2) the method comprises a flue gas temperature control step or a flue gas temperature regulation step, wherein the flue gas temperature regulation step comprises the following substeps:
① temperature control of the flue gas of the bypass flue gas pipeline (L2), wherein an atomizer (2) is arranged on the bypass flue gas pipeline (L2), the wastewater is atomized by the atomizer (2) and then mixed with the flue gas in the bypass flue gas pipeline (L2), the wastewater exchanges heat with the flue gas entering the bypass flue gas pipeline (L2) to form a mixed gas of the flue gas and the wastewater, the mixed gas of the flue gas and the wastewater is dedusted by a deduster (3), and impurities in the mixed gas of the flue gas and the wastewater are discharged from a solid outlet (303) of the deduster (3);
② temperature control of the flue gas in the original flue gas conveying pipeline (L1), namely, introducing cold air into the original flue gas conveying pipeline (L1) to regulate the temperature of the flue gas in the original flue gas conveying pipeline (L1) at the downstream of the position of the bypass flue gas pipeline (L2) separated from the original flue gas conveying pipeline (L1);
③ the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline (L2) is merged into the original flue gas conveying pipeline (L1) and is mixed with the flue gas in the original flue gas conveying pipeline (L1) after the temperature is controlled or adjusted by cold air, and the mixed gas enters the adsorption tower (1), wherein the temperature of the flue gas at the inlet of the adsorption tower (1) is adjusted within a specified range;
3) the mixed flue gas enters an activated carbon adsorption tower (1), is adsorbed and purified by activated carbon in the adsorption tower (1) and then is discharged, and the activated carbon adsorbing pollutants in the flue gas is discharged from the bottom of the adsorption tower (1);
wherein: in the step 2), a first temperature measuring point (P1) is arranged at the upstream of the position of the bypass flue gas pipeline (L2) separated from the original flue gas conveying pipeline (L1); a second temperature measuring point (P2) is arranged between the position of the cold air introduced into the raw flue gas conveying pipeline (L1) and the position of the bypass flue gas pipeline (L2) merged to the raw flue gas conveying pipeline (L1); a third temperature measurement point (P3) is arranged on the bypass flue gas pipeline (L2) and is positioned at the downstream of the dust remover (3); a fourth temperature measuring point (P4) is arranged on the raw flue gas conveying pipeline (L1) and downstream of the position where the bypass flue gas pipeline (L2) is merged into the raw flue gas conveying pipeline (L1); a first temperature measuring point (P1) detects the flue gas temperature T1 in a flue at a corresponding position on line, a second temperature measuring point (P2) detects the flue gas temperature T2 in the flue at the corresponding position on line, a third temperature measuring point (P3) detects the flue gas temperature T3 in the flue at the corresponding position on line, and a fourth temperature measuring point (P4) detects the flue gas temperature T4 in the flue at the corresponding position on line; wherein the target or set temperature value at the fourth temperature measurement point (P4) is T4Is provided with(ii) a According to the heat Q released by the flue gas entering the bypass flue gas pipeline (L2)Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct (L2)Water (W)And equalising, calculating and adjusting the quantity of flue gas entering the by-pass flue gas duct (L2) in sub-step ①, further according to the heat Q released by the flue gas entering the adsorption tower (1) through the raw flue gas duct (L1)Cigarette 2The heat Q absorbed by the cold air introduced into the raw flue gas duct (L1)Qi (Qi)And (3) equally calculating and adjusting the amount of cold air introduced into the original flue gas conveying pipeline (L1) in the substep ②, and adjusting or controlling the temperature T4 of the fourth temperature measuring point (P4) to be T4 by adjusting the amount of flue gas entering the bypass flue gas pipeline (L2) and the amount of cold air introduced into the original flue gas conveying pipeline (L1)Is provided withA temperature range of + -t deg.C, wherein t deg.C is in the range of 1-5 deg.C.
2. The method of claim 1, wherein: wherein the target or set temperature value T4 at the fourth temperature measurement point (P4)Is provided withTaking the value within the range of 100-145 ℃; namely, the temperature of the flue gas at the inlet of the adsorption tower (1) is regulated to be in the range of 100 ℃ and 145 ℃.
3. The method of claim 1, wherein: wherein the target or set temperature value T4 at the fourth temperature measurement point (P4)Is provided withTaking the value within the range of 110-140 ℃; namely, the temperature of the flue gas at the inlet of the adsorption tower (1) is regulated within the range of 110 ℃ to 140 ℃.
4. The method according to claim 1, characterized in that in sub-step ①, the wastewater enters the atomizer (2) from the wastewater tank (4) along a wastewater inlet line (L3).
5. The method of claim 4, characterized in that the waste water in the waste water storage tank (4) is neutral or alkaline, the waste water input pipe (L3) is provided with a waste water pump (5), the waste water pump (5) provides power for the waste water to enter the atomizer (2), and in the sub-step ②, the cold air is conveyed from the air pipe (L4) to the raw flue gas conveying pipe (L1).
6. The method of claim 1, wherein: the heat Q released according to the flue gas entering the bypass flue gas duct (L2)Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct (L2)Water (W)And (3) equally, calculating and adjusting the amount of flue gas entering the bypass flue gas duct (L2) in the substep ①, specifically:
the first temperature measuring point (P1) detects the temperature of the original flue gas as T1, and the temperature of the mixed gas of the flue gas and the waste water at the position of the third temperature measuring point (P3) is set as T3Is provided withWherein: t3Is provided withTaking values within the range of 100 ℃ and 160 ℃;
a) calculating the heat required by wastewater treatment: a liquid level meter is arranged in the waste water storage tank (4), and the waste water quantity M required to be treated in the waste water storage tank (4) is obtained according to the liquid level meterWater (W)Detecting the initial temperature of the wastewater to beTWater (W)Whereby the amount of heat Q to be absorbed for treating the waste water in the waste water tank (4)Water (W)Comprises the following steps:
Qwater (W)＝MWater (W)rWater (W)+CWater vapourMWater (W)ΔTWater (W)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (1)，
In the formula (1), rWater (W)Is the heat of vaporization of the waste water, CWater vapourThe specific heat capacity of water vapor;
b) calculating the required flue gas amount of the bypass flue gas pipeline (L2): setting the amount of flue gas entering the bypass flue gas pipeline (L2) as M1Whereby the heat Q released by the flue gas entering the bypass flue gas duct (L2)Cigarette 1Comprises the following steps:
Qcigarette 1＝CCigarette with heating meansM1ΔTCigarette 1＝CCigarette with heating meansM1(T1-T3Is provided with) (2)，
C in formula (2)Cigarette with heating meansThe specific heat capacity of the flue gas;
heat Q released by the flue gas entering the bypass flue gas duct (L2)Cigarette 1With the heat Q absorbed by the waste water sprayed into the bypass flue gas duct (L2)Water (W)Equality, we can get:
Ccigarette with heating meansM1(T1-T3Is provided with)＝MWater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W))) (3)，
Obtaining the following components:
M1＝Mwater (W)(rWater (W)+CWater vapour(T3Is provided with-TWater (W)))/(CCigarette with heating means(T1-T3Is provided with)) (4)；
The opening degree of a bypass valve (6) on the bypass flue gas pipeline (L2) is adjusted so that the amount of the flue gas entering the bypass flue gas pipeline (L2) is M1。
7. The method of claim 6, wherein: t3Is provided withThe temperature is within the range of 110 ℃ and 140 ℃.
8. The method of claim 6, wherein: further according to the heat Q released by the flue gas entering the adsorption tower (1) through the raw flue gas conveying pipeline (L1)Cigarette 2The heat Q absorbed by the cold air introduced into the raw flue gas duct (L1)Qi (Qi)And (3) equally, calculating and adjusting the amount of cold air introduced into the original flue gas conveying pipeline (L1) in the substep ②, specifically:
the total amount of the smoke measured by the flowmeter (7) at the upstream of the first temperature measuring point (P1) is M0The temperature of the original smoke detected by the first temperature measuring point (P1) is T1, and the temperature of the mixed gas of the smoke and the cold air at the position of the second temperature measuring point (P2) is set to be T2Is provided withWherein: t2Is provided withTaking values within the range of 100 ℃ and 160 ℃;
a) calculating the required heat released by the raw flue gas in the raw flue gas conveying pipeline (L1): the quantity of flue gas entering the adsorption column (1) through the raw flue gas duct (L1) is (M)0-M1) The heat Q released by the flue gas entering the adsorption tower (1) through the raw flue gas conveying pipeline (L1)Cigarette 2Comprises the following steps:
Qcigarette 2＝CCigarette with heating means(M0-M1)ΔTCigarette with heating means＝CCigarette with heating means(M0-M1)(T1-T2Is provided with) (5)，
b) The amount of cold air introduced into the raw flue gas conveying pipeline (L1) is calculated: setting the quantity of cold air introduced into the original flue gas conveying pipeline (L1) as MQi (Qi)Measuring the initial temperature of the cold air as TQi (Qi)Thereby, the heat Q absorbed by the cold air introduced into the raw flue gas delivery duct (L1)Qi (Qi)Comprises the following steps:
Qqi (Qi)＝CQi (Qi)MQi (Qi)ΔTQi (Qi)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (6)，
C in formula (6)Qi (Qi)Is the specific heat capacity of the cold air;
heat Q released by the flue gas entering the adsorption column (1) through the raw flue gas duct (L1)Cigarette 2The heat Q absorbed by the cold air introduced into the raw flue gas duct (L1)Qi (Qi)Equality, we can get:
Ccigarette with heating means(M0-M1)(T1-T2Is provided with)＝CQi (Qi)MQi (Qi)(T2Is provided with-TQi (Qi)) (7)；
Obtaining the following components:
Mqi (Qi)＝CCigarette with heating means(M0-M1)(T1-T2Is provided with)/(CQi (Qi)(T2Is provided with-TQi (Qi))) (8)；
The opening degree of a cold air valve (8) on the air pipeline (L4) is adjusted, so that the quantity of cold air introduced into the original flue gas conveying pipeline (L1) is MQi (Qi)。
9. The method of claim 8, wherein: t2Is provided withThe temperature is within the range of 110 ℃ and 140 ℃.
10. The method of claim 8, wherein: the temperature T4 of the fourth temperature measuring point (P4) is adjusted or controlled at T4 by adjusting the amount of the smoke entering the bypass smoke pipeline (L2) and the amount of the cold air introduced into the raw smoke conveying pipeline (L1)Is provided withThe range of +/-t ℃ is as follows:
the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline (L2) is mixed with the mixed gas of the flue gas and the cold air in the original flue gas conveying pipeline (L1) after the temperature of the flue gas and the waste water is controlled or regulated by the cold air, after the two paths of gas are subjected to heat exchange, the temperature T4 of a fourth temperature measuring point (P4) is regulated or controlled at T4Is provided withThe range of +/-t ℃; the heat Q absorbed (or released) by the mixed gas of the flue gas and the waste water in the bypass flue gas pipeline (L2)Smoke and waterHeat Q released (or absorbed) by the mixed gas of the flue gas and the cold air in the raw flue gas conveying pipeline (L1)Smoke and gasEqual, i.e.:
Qsmoke and water＝QSmoke and gas(9)，
Namely: c1(M1+MWater (W))(T4Is provided with-T3Is provided with)＝C2(M0-M1+MQi (Qi))(T2Is provided with-T4Is provided with) (10)，
C in formula (10)1Mixing flue gas and waste waterThe specific heat capacity of the gas; c2Is the specific heat capacity of the mixed gas of the flue gas and the cold air.
11. The method of claim 10, wherein: t2Is provided with＝T3Is provided with＝T4Is provided with(ii) a Detecting the flue gas temperature T2 in the flue at the corresponding position on line according to a second temperature measuring point (P2); if T2 equals T2Is provided withContinuing to operate; t2 not equal to T2Is provided withAdjusting the quantity of cold air introduced into the raw flue gas duct (L1) so that T2 equals T2Is provided with；
Detecting the flue gas temperature T3 in the flue at the corresponding position on line according to a third temperature measuring point (P3); if T3 equals T3Is provided withContinuing to operate; t3 not equal to T3Is provided withAdjusting the amount of flue gas entering the bypass flue gas duct (L2) such that T3 equals T3Is provided with；
Detecting the flue gas temperature T4 in the flue at the corresponding position on line according to a fourth temperature measuring point (P4); if T4 equals T4Is provided withContinuing to operate; t4 not equal to T4Is provided withAdjusting the amount of cold air passing into the original flue gas conveying pipe (L1) and the amount of flue gas entering the bypass flue gas pipe (L2) so that T4 is equal to T4Is provided with。
12. The method according to any one of claims 1-11, wherein: in the step 3), the flue gas absorbed and purified by the activated carbon in the absorption tower (1) is discharged through a chimney (9).
CN201810135593.0A 2018-02-09 2018-02-09 Flue gas purification method and device comprising flue gas temperature control Active CN108096989B (en)

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CN105688626A (en) * 2014-11-28 2016-06-22 中冶长天国际工程有限责任公司 A flue gas desulphurization denitration method including flue gas temperature control and a device therefor
CN105879542A (en) * 2016-03-07 2016-08-24 上海龙净环保科技工程有限公司 Power plant desulfurization wastewater bypass treatment system and method and flue gas treatment system and method

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* Cited by examiner, † Cited by third party
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CN105688626A (en) * 2014-11-28 2016-06-22 中冶长天国际工程有限责任公司 A flue gas desulphurization denitration method including flue gas temperature control and a device therefor
CN105879542A (en) * 2016-03-07 2016-08-24 上海龙净环保科技工程有限公司 Power plant desulfurization wastewater bypass treatment system and method and flue gas treatment system and method

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