CN108939808A - A kind of active carbon processing system and its application method improving utilization rate of waste heat and denitrification rate - Google Patents

A kind of active carbon processing system and its application method improving utilization rate of waste heat and denitrification rate Download PDF

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CN108939808A
CN108939808A CN201810762472.9A CN201810762472A CN108939808A CN 108939808 A CN108939808 A CN 108939808A CN 201810762472 A CN201810762472 A CN 201810762472A CN 108939808 A CN108939808 A CN 108939808A
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gas
active carbon
heat
resolver
flue gas
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CN108939808B (en
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李俊杰
魏进超
康建刚
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Zhongye Changtian International Engineering Co Ltd
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Zhongye Changtian International Engineering Co Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
    • F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/4002—Production
    • B01D2259/40022—Production with two sub-steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Treating Waste Gases (AREA)

Abstract

The present invention provides a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate, by the way that heat exchanger is respectively set before flue gas inputs first order adsorption tower and second level adsorption tower, control flue gas enters temperature when first order adsorption tower and second level adsorption tower, to ensure that the temperature of desulfurization and denitration.The present invention utilizes the high-temperature flue gas (about 150-170 DEG C) after main exhaust fan, and by the way of heat exchange, artificial control enters the flue-gas temperature of first stage tower, second level tower, improves SO2, NOx place to go efficiency device.The high-temperature flue gas utilization efficiency after main exhaust fan is improved, and desulfurizing tower, denitrating tower flue-gas temperature are entered using control, improves denitrification efficiency.

Description

A kind of active carbon processing system and its use improving utilization rate of waste heat and denitrification rate Method
Technical field
The present invention relates to a kind of active carbon processing systems, and in particular to a kind of processing for improving utilization rate of waste heat and denitrification rate Flue gas desulfurization and denitrification system, belongs to filed of flue gas purification.
Background technique
For sintering flue gas after main exhaust fan between about 110-170 DEG C of exhaust temperature, SO is contained in the inside2、NOx, dust, two The multiple pollutants such as English, heavy metal are disliked, and active carbon flue gases purification is suitable for that sintering flue gas temperature discharges section just, it can be real The collaboration high-efficient purification of existing multi-pollutant, can remove multiple pollutant simultaneously on a set of equipment, realize by-product SO2Resource Change and utilize, and the technology has pollutant removing high-efficient, does not consume water resource substantially, it is without secondary pollution to wait a little.Activity Charcoal flue gas purification device is provided with multiple subsystems such as adsorption system, resolution system, acid making system, and flue gas passes through activated carbon adsorption Unit after-purification, active carbon particle circulate between absorbing unit and resolution unit, realize " absorption pollutant -> heating solution Analysis activation (escaping pollutant) -> cooling -> absorption pollutant " recycles.
Activated carbon adsorption is divided into single stage adsorption at present and twin-stage adsorbs two ways, and single stage adsorption is in an adsorption tower Multiple pollutant is adsorbed simultaneously, and ammonia is added in adsorption column inlet, this kind of method can achieve SO2Removal efficiency > 98%, denitration Rate about 50%, dust outlet concentration are less than 20mg/Nm3.With the raising of environmental requirement, part iron factory is adsorbed using twin-stage, Wherein first stage tower carries out desulfurization, dedusting etc., and second level tower carries out denitration, this kind of method treatment effect: SO2Removal efficiency > 98% takes off Nitre rate is greater than 80%, and dust outlet concentration is less than 10mg/Nm3。
It is well known that temperature has important shadow to pollutant removal using activated carbon method flue gas desulfurization and denitration technique It rings, favors low temperature is in desulphurization reaction, and high temperature facilitates denitration reaction, therefore to improve multi-pollutant removal efficiency, at second level In science and engineering skill, it is therefore desirable to level-one, second level tower entrance flue gas temperature are controlled respectively, wherein meeting (120 DEG C > t > 100 of a grade low-temp DEG C), second level high temperature (155 DEG C > t > 140 DEG C).
The process flow of the prior art is as follows: the flue-gas temperature after main exhaust fan is excessively high (110-170 DEG C), Bu Nengzhi It taps into desulfurizing tower, therefore cooling air need to be filled into, control enters the flue-gas temperature of desulfurizing tower between (100-120 DEG C), contains The former flue gas of multiple pollutant carries out desulfurization and dedusting by desulfurizing tower, carries out denitration, NH subsequently into denitrating tower3Enter in denitrating tower Mouth is added.Active carbon is sent to second level tower after Analytic Tower is parsed, and the active carbon after second level tower denitration passes through delivery system System is sent to first stage tower, and the transportation system that the first stage tower active carbon after adsorbing desulfurization and dedusting passes through again is sent to Analytic Tower, completes one Secondary complete Matter Transfer.
In the prior art using the technique for being blended into cold wind or cold water into former flue gas, so that former flue gas cool-down, then defeated Enter desulfurizing tower, the high-temperature flue gas heat after main exhaust fan cannot be made full use of, to guarantee to enter the flue-gas temperature of desulfurizing tower, needs It additionally to be blended into cold wind, cause the loss of high-temperature flue gas.However, low temperature facilitates desulfurization, high temperature facilitates denitration；It is blended into cold After wind, the temperature requirement of desulfurizing tower is adapted to, but after desulfurization, flue-gas temperature is low, into after the out of stock tower of next step, denitration Effect is poor.It directlys adopt and converts the mode of cooling wind and be difficult to for SO2、NOxCharacterization of adsorption, cannot effectively improve desulphurization denitration effect Rate causes heat and denitration reaction product NH3Waste.
In addition, active carbon resolution system is by fuel such as Combustion of Hot Air Furnace blast furnace gas, coke-stove gas in Analytic Tower Active carbon carries out indirect heating, so that active carbon parses regeneration in Analytic Tower；Therefore the high-temperature gas in hot-blast stove after burning In contain about 100ppm SO2Gas, temperature is about at 300 DEG C or so.The high-temperature gas after the burning is mostly used at present Hot air circulation, for reducing the application of blast furnace gas, coke-stove gas or other fuel, while in order to keep in hot air circulating system Pressure and oxygen content are stablized, which needs the moment to discharge a part into flue, and capacity is about outside this part The 10% of internal circulating load, about 300 DEG C of temperature or so.
The gas direct emission of outlet in the prior art, there are micro SO in the heat gas of discharge2Outlet, to environment It impacts, and the heat of outlet can not be made full use of, cause the waste of heat.Therefore, this portion discharged into flue The heat of exceptionally capacity is not fully used, and energy waste is caused.Moreover, capacity contains SO outside this part2 Gas, direct outlet pollute surrounding enviroment.
Furthermore the active carbon for having adsorbed pollutant is parsed using Analytic Tower.The purpose of desorption system is to having adsorbed dirt The active carbon for contaminating object carries out high temperature parsing regeneration, produces and contains high concentration SO in gas2, the multiple pollutants such as large quantity of moisture (SRG), SRG gas is sent to acid making system relieving haperacidity.
Due to the characterization of adsorption of active carbon, SO in sintering flue gas2And other objectionable impurities almost all are enriched to SRG gas In.Therefore, the harmful components almost not detected in sintered net flue gas have all reached very high concentration, SRG cigarette in SRG flue gas Gas has the following characteristics that (1) flow is small, temperature is high, about 400 DEG C of flue gas mean temperature, 600m2Sintering machine SRG flue gas flow is (dry Base) it is 2000m3/ h or so；(2) flue gas SO2Concentration is high, SO in SRG flue gas2Mass fraction is up to 25% (butt)；(3) flue gas Middle water content is high, and highest water content can reach 33%；(4) content of CO in smoke is high, mass fraction about 0.5%；(5) ammonia in flue gas, The harmful constituents such as fluorine, chlorine, mercury content is high, and average mass fraction is respectively 3.1%/0.1%/1.6%/51mg/Nm3；(6) flue gas Dust content is high, and dirt is average in 2g/m3Left and right；Flue dust main component is active carbon, accounts for the 65-85% of total dust.It can be seen that Water content is big in SRG gas, and temperature is high, has high temperature high corrosion property, therefore relieving haperacidity process is glass steel material, glass steel Confrontation temperature requirement is very high, general to require to run at 100 DEG C or less, but SRG measurement of moisture content of gas is high, and it is following unfavorable to will cause It influences: (1) in order to handle the pollutant in SRG, consuming a large amount of water, result in waste of resources；(2) since the specific heat capacity of water is larger, In order to handle SRG gas in the acid making system of glass steel material, it is necessary to water is added in SRG gas and achievees the purpose that cooling, Due to moisture content weight, temperature is relatively high after cooling, impacts to the glass steel material service life；(3) a large amount of Wastes are generated Water.
Summary of the invention
When being handled for flue gas in the prior art using active carbon processing system, heating efficiency is low, and denitration effect is poor The problems such as, the present invention provides a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate, by flue gas input the Heat exchanger is respectively set before primary adsorption tower and second level adsorption tower, control flue gas enters first order adsorption tower and the second level is inhaled Temperature when attached tower improves the efficiency of desulphurization denitration to ensure that the temperature of desulfurization and denitration, improves fume afterheat and utilizes Rate.
The present invention utilizes the high-temperature flue gas (about 150-170 DEG C) after main exhaust fan, by the way of heat exchange, artificially Control enters the flue-gas temperature of first stage tower, second level tower, improves SO2, NOx place to go efficiency device and method.It realizes and improves master High-temperature flue gas utilization efficiency after exhaust blower, and the method into desulfurizing tower, denitrating tower flue-gas temperature is controlled, it is de- to improve desulfurization The purpose of nitre efficiency.
Second object of the present invention is: preventing SO contained in the hot air circulation gas for parsing2Direct outlet, To solve this problem, the present invention, which provides one kind, can remove outlet SO2The flue gas purification device of concentration.The device will with wait solve The outer thermal wind exhausting of a part after analysing active carbon heat exchange introduces the smoke inlet of secondary absorption tower, on the one hand removes outlet SO2Concentration, The flue gas of secondary absorption tower inlet is heated simultaneously, and flue-gas temperature is improved.In general, secondary absorption tower inlet flue gas SO2Concentration is lower, and temperature correspondinglys increase, and denitrification rate is higher.Therefore, the device is in removal outlet SO2While concentration, also Improve denitration efficiency and utilization rate of waste heat.
Third object of the present invention is: for moisture content weight in SRG gas in the prior art, being unfavorable for subsequent matter The problem of acid processing, the present invention develop a kind of new desorption tower structure, different according to the decomposition temperature of activated carbon adsorption pollutant, Shift to an earlier date the moisture in isolating active charcoal by the method for step heating, reduce moisture content in SRG gas, is downstream relieving haperacidity, useless Water process process normal operation creates good conditions.
The first embodiment provided according to the present invention provides a kind of active carbon for improving utilization rate of waste heat and denitrification rate Processing system.
A kind of active carbon processing system improving utilization rate of waste heat and denitrification rate, which includes active carbon Adsorption tower, active carbon Analytic Tower.The activated carbon adsorber is two-stage adsorption tower, including first order adsorption tower and second level absorption Tower.The active carbon processing system further includes former smoke conveying duct, the first flue gas heat-exchange unit, the second flue gas heat-exchange unit, preliminary place Manage smoke conveying duct, the first active carbon conveying device, the second active carbon conveying device, third active carbon conveying device.
Wherein: former smoke conveying duct is connected to the smoke inlet of first order adsorption tower.The flue gas of first order adsorption tower goes out Mouth is connected to the smoke inlet of second level adsorption tower by preliminary treatment smoke conveying duct.First flue gas heat-exchange unit is arranged in original On smoke conveying duct.Second flue gas heat-exchange unit is arranged on preliminary treatment smoke conveying duct.First active carbon conveying device Connect the active carbon entrance of the active carbon outlet and second level adsorption tower of active carbon Analytic Tower.The connection of second active carbon conveying device The active carbon entrance of the active carbon outlet and first order adsorption tower of second level adsorption tower.Third active carbon conveying device connection first The active carbon entrance of the active carbon outlet and active carbon Analytic Tower of grade adsorption tower.
Preferably, active carbon Analytic Tower is equipped with a heating section and a cooling section from top to bottom.The lower part of bringing-up section is equipped with heating The top of section gas access, bringing-up section is equipped with bringing-up section gas vent.The device further includes hot-blast stove.Hot-blast stove is equipped with hot wind Entrance and hot-blast outlet.The first pipe drawn from the hot-blast outlet of hot-blast stove is connected to the bringing-up section gas of active carbon Analytic Tower Entrance.The second pipe drawn from bringing-up section gas vent is connected to the hot-wind inlet of hot-blast stove.One is separated from second pipe Branch, that is, third pipeline, third pipeline are connected to the smoke inlet of preliminary treatment smoke conveying duct or second level adsorption tower.
Preferably, institute's active carbon Analytic Tower includes the preheating zone being arranged from top to bottom, vapor resolver, pollutant point Xie Qu, cooling zone, First Transition section and the second changeover portion.
Wherein: the lower part of preheating zone is equipped with preheating zone gas access and preheating zone gas vent.Under vapor resolver Portion is equipped with vapor resolver gas access and vapor resolver gas vent.The lower part of pollutant resolver is equipped with pollutant Resolver gas access and pollutant resolver gas vent.The lower part of cooling zone is equipped with cooling zone gas access and cooling zone gas Body outlet.It is First Transition section between vapor resolver and pollutant resolver.It is between pollutant resolver and cooling zone Second changeover portion.The side wall of First Transition section is equipped with steam outlet.The side wall of second changeover portion is equipped with SRG gas and goes out Mouthful.
Preferably, the device further includes hot-blast stove.Hot-blast stove is equipped with hot-wind inlet and hot-blast outlet.Cooling zone gas Entrance is connect with cooling gas conveyance conduit.The first pipe drawn from the hot-blast outlet of hot-blast stove is connected to pollutant resolver Gas access.Pollutant resolver gas vent is connected to vapor resolver gas access by the 4th pipeline.Vapor point Solution area's gas vent is connected to the hot-wind inlet of hot-blast stove by second pipe.
Preferably, separating a branch i.e. third pipeline from second pipe, third pipeline is connected to preliminary treatment flue gas The smoke inlet of conveyance conduit or second level adsorption tower.
Preferably, cooling zone gas vent is connected to preheating zone gas access by the 5th pipeline.
Preferably, the active carbon Analytic Tower further includes the nitrogen delivery pipe for being passed through nitrogen to active carbon Analytic Tower top Road.Nitrogen gas delivery-line is connected to Analytic Tower, and the link position of nitrogen gas delivery-line and active carbon Analytic Tower is located at preheating The top in area.
Preferably, nitrogen gas delivery-line is equipped with nitrogen heat exchanger.Preheating zone gas vent is connected by the 6th pipeline To the entrance of the heating medium passage of nitrogen heat exchanger.
Preferably, steam outlet passes through the 7th pipeline to former smoke conveying duct.
Preferably, SRG gas vent is delivered to acid making system by SRG gas transmission pipeline.
Preferably, cooling gas conveyance conduit is equipped with cooling wind blower.
Preferably, first pipe is equipped with air-heater.
Preferably, being additionally provided with wind-supplying mouth on hot-blast stove.
Preferably, the device further includes chimney.The exhanst gas outlet of second level adsorption tower is connected to cigarette via the 8th pipeline Chimney.
Preferably, the gas vent of the first flue gas heat-exchange unit is connected to second by First Heat Exchanger medium delivery pipe road The gas access of flue gas heat-exchange unit.The gas vent of second flue gas heat-exchange unit is connected to by the second heat exchanger media conveyance conduit The gas access of first flue gas heat-exchange unit.
Preferably, First Heat Exchanger medium delivery pipe road and/or the second heat exchanger media conveyance conduit are equipped with blower.
Preferably, First Heat Exchanger medium delivery pipe road is equipped with discharge outlet.
Preferably, the second heat exchanger media conveyance conduit is equipped with filler.
Preferably, former smoke conveying duct is equipped with the first temperature-detecting device, and the first temperature-detecting device is set It sets in the downstream of the first flue gas heat-exchange unit.
Preferably, preliminary treatment smoke conveying duct is equipped with second temperature detection device, and second temperature detects The downstream of the second flue gas heat-exchange unit is arranged in device.
In the present invention, first order adsorption tower is desulfurizing tower, and second level adsorption tower is denitrating tower.
Second of the embodiment provided according to the present invention provides a kind of active carbon for improving utilization rate of waste heat and denitrification rate Processing method.
A kind of active carbon processing method improving utilization rate of waste heat and denitrification rate or using described in the first embodiment A method of the active carbon processing system of utilization rate of waste heat and denitrification rate is improved, method includes the following steps:
1) fresh active carbon is obtained by the parsing of active carbon Analytic Tower be delivered to the by the first active carbon conveying device The active carbon entrance of secondary absorption tower；In the adsorption tower of the second level from top to bottom, from the second level, adsorption tower active carbon goes out active carbon Then the active carbon that second level adsorption tower is discharged is delivered to first order absorption by the second active carbon conveying device by mouth discharge Tower；Active carbon from top to bottom, is exported from the active carbon of first order adsorption tower and is discharged, then will be from the first order in first order adsorption tower The active carbon of adsorption tower discharge is delivered to active carbon Analytic Tower by third active carbon conveying device and carries out parsing regeneration；
2) former flue gas is delivered to first order adsorption tower by former smoke conveying duct, former flue gas in first order adsorption tower into Row desulfurization process is delivered to the second level by preliminary treatment smoke conveying duct by first order adsorption tower treated flue gas and inhales Attached tower, preliminary treatment flue gas carry out out of stock processing in the adsorption tower of the second level, by first order adsorption tower and second level adsorption tower Treated flue gas is from smoke stack emission；
Wherein: in the first flue gas heat-exchange unit on former smoke conveying duct, in former flue gas and the first flue gas heat-exchange unit Medium exchanges heat, and former flue gas discharges heat in the first flue gas heat-exchange unit, and medium absorbs heat in the first flue gas heat-exchange unit, Former flue gas after release heat cooling enters first order adsorption tower；Medium after absorbing heat is conveyed by First Heat Exchanger medium Pipeline is to the second flue gas heat-exchange unit；
In the second flue gas heat-exchange unit of preliminary treatment smoke conveying duct, by first order adsorption tower, that treated is preliminary Processing flue gas exchanges heat with the medium in the second flue gas heat-exchange unit, and the medium that heat is absorbed from the first flue gas heat-exchange unit exists Heat is discharged in second flue gas heat-exchange unit, preliminary treatment flue gas absorbs heat in the second flue gas heat-exchange unit, absorbs heat heating Preliminary treatment flue gas afterwards enters second level adsorption tower；Medium after release heat is followed by the second heat exchanger media conveyance conduit Ring is to the first flue gas heat-exchange unit.
Preferably, this method further include:
3) hot wind stove heating hot wind, hot wind enter work from the bringing-up section gas access of active carbon Analytic Tower by first pipe The bringing-up section of property charcoal Analytic Tower, hot wind exchanges heat in active carbon Analytic Tower with active carbon, in heating of Activated charcoal Analytic Tower Then active carbon enters by second pipe after the discharge of bringing-up section gas vent and continues heat cycles in hot-blast stove；Second pipe A branch is separated on road, is third pipeline, a part warp for the hot wind after heat exchange being discharged from bringing-up section gas vent Third pipeline is crossed to preliminary treatment smoke conveying duct or the smoke inlet of second level adsorption tower.
Preferably, the active carbon Analytic Tower includes the preheating zone being arranged from top to bottom, vapor resolver, pollutant Resolver, cooling zone, First Transition section and the second changeover portion；Wherein: the lower part of preheating zone is equipped with preheating zone gas access and in advance Hot-zone gas vent；The lower part of vapor resolver is equipped with vapor resolver gas access and vapor resolver gas goes out Mouthful；The lower part of pollutant resolver is equipped with pollutant resolver gas access and pollutant resolver gas vent；Cooling zone Lower part is equipped with cooling zone gas access and cooling zone gas vent；It is the first mistake between vapor resolver and pollutant resolver Cross section；It is the second changeover portion between pollutant resolver and cooling zone；The side wall of First Transition section is equipped with steam outlet；The The side wall of two changeover portions is equipped with SRG gas vent.
Preferably, this method further include: 4) first order adsorption tower discharge active carbon in active carbon Analytic Tower successively By preheating zone, vapor resolver, First Transition section, pollutant resolver, the second changeover portion and cooling zone；Contain pollutant Active carbon after entering active carbon Analytic Tower, first preheated in preheating zone, then carry out moisture in vapor resolver Removing, from the moisture being removed in active carbon from First Transition section side wall on steam outlet be expelled directly out；Then, it goes to remove water Point active carbon containing pollutant decompose and the removing of pollutant in pollutant resolver again, pollutant is from the second changeover portion side SRG gas vent discharge on wall；Then active carbon is cooled down by cooling zone, obtains fresh active carbon.
Preferably, this method further include:
5) cooling gas enters the cooling of active carbon Analytic Tower by cooling gas conveyance conduit from cooling zone gas access Area, the gas being discharged from cooling zone gas vent pass through the 5th pipeline to preheating zone；
Hot wind stove heating hot wind, hot wind by first pipe from the pollutant resolver gas access of active carbon Analytic Tower into Enter the pollutant resolver of active carbon Analytic Tower, hot wind exchanges heat in pollutant resolver with active carbon, heating of Activated charcoal Active carbon in Analytic Tower, the pollutant of removal activity charcoal；Then by the 4th after the discharge of pollutant resolver gas vent Pipeline is delivered to vapor resolver from vapor resolver gas access, which continues and activity in vapor resolver Charcoal exchanges heat, the moisture in removal activity charcoal；Then it is discharged from vapor resolver gas vent, by second pipe from heat The hot-wind inlet of wind furnace, which enters, continues heat cycles in hot-blast stove；
A branch is separated on second pipe, is third pipeline, and the process being discharged from vapor resolver gas vent is changed A part of hot wind after heat is by third pipeline to preliminary treatment smoke conveying duct or the flue gas of second level adsorption tower Entrance.
Preferably, the gas of preheating zone gas vent discharge is situated between by the heating of the 6th pipeline to nitrogen heat exchanger The entrance in matter channel, heated nitrogen.
Preferably, the gas being discharged from steam outlet passes through the 7th pipeline to former smoke conveying duct.
Preferably, being delivered to acid making system by SRG gas transmission pipeline from the SRG gas that SRG gas vent is discharged.
Preferably, the heat after heat exchange being discharged from bringing-up section gas vent or vapor resolver gas vent Wind, wherein volume fraction is that the hot wind of 0.5-30% (preferably 1-20%, more preferably 2-15%) passes through third pipeline To preliminary treatment smoke conveying duct or the smoke inlet of second level adsorption tower.
Preferably, the temperature of the first temperature-detecting device detection former flue gas in former smoke conveying duct pipeline after exchanging heat, 1. and/or 2. by following step, so that into the flue-gas temperature in first order adsorption tower be 100-120 DEG C；
1. adjusting the amount for the water being added from discharge outlet on First Heat Exchanger medium delivery pipe road；
2. adjusting the amount from discharge water in filler on the second heat exchanger media conveyance conduit.
Preferably, second temperature detection device detects the temperature of flue gas after preliminary treatment in the second flue gas heat-exchange unit, lead to 1. and/or 2. and/or 3. cross following step so that into the flue-gas temperature in the adsorption tower of the second level be 140-155 DEG C；
1. adjusting the amount for the water being added from discharge outlet on First Heat Exchanger medium delivery pipe road；
2. adjusting the amount from discharge water in filler on the second heat exchanger media conveyance conduit；
3. adjusting the hot wind after heat exchange being discharged from bringing-up section gas vent or vapor resolver gas vent, warp Cross the amount of third pipeline to preliminary treatment smoke conveying duct or the hot wind of the smoke inlet of second level adsorption tower.
In the present invention, it is changed by the way that the first flue gas is arranged on the former smoke conveying duct before entering first order adsorption tower Hot device absorbs the waste heat in former flue gas, adjusts the former flue-gas temperature for entering first order adsorption tower, controls between 100-120 DEG C, This temperature is to be most suitable for flue gas desulfurization temperature, to guarantee desulfurization effect.Change the technical solution for being blended into cold wind in the prior art, The increase for avoiding former amount of flue gas emission reduces the load of subsequent desulfurization and denitration.
In the present invention, by being arranged second on the preliminary treatment smoke conveying duct before entering second level adsorption tower Flue gas heat-exchange unit, the second heat exchanger discharge heat, improve the temperature for absorbing preliminary treatment flue gas, inhale to adjust into the first order The flue-gas temperature of attached tower controls between 140-155 DEG C, this temperature is to be most suitable for denitrating flue gas temperature, to guarantee that denitration is imitated Fruit.Change in the prior art, flue gas directly inputs the technical solution of denitrating tower after desulfurization, improves flue gas in denitrating tower Denitration temperature, substantially increase denitration efficiency, denitrification rate from the prior art 50% or so be increased to 80% or more.Together When, due to the enhancing of denitration effect, reduce the straying quatity of ammonia in denitrification process；In the prior art, since denitration temperature is low, In order to guarantee denitration effect, needs to spray into a large amount of ammonia, cause the waste of ammonia resource, meanwhile, ammonia is easily escaped, In the presence of very big security risk.In the activated carbon system of the application, due to the setting of the second heat exchanger, cigarette in denitrating tower ensure that The out of stock temperature of gas, the denitration efficiency greatly improved reduce the straying quatity of ammonia, economize on resources.
In the present invention, pass through First Heat Exchanger medium delivery pipe road and second between First Heat Exchanger and the second heat exchanger The connection of heat exchanger media conveyance conduit.First Heat Exchanger on former smoke conveying duct with the former flue gas in former smoke conveying duct It exchanges heat, the heat of the Absorption of Medium original flue gas in First Heat Exchanger, so that the temperature of former flue gas is reduced to suitable range It is interior.The medium for absorbing heat is transported to the second heat exchanger, and the certain media is defeated with preliminary treatment flue gas in the second heat exchanger The preliminary treatment flue gas in pipeline is sent to exchange heat, medium discharges heat, preliminary treatment flue gas is heated, so that the flue gas is transported to Temperature increases when in the adsorption tower of the second level, and second level adsorption tower is suitble to carry out denitration process to flue gas.That is, heat transferring medium It is recycled between First Heat Exchanger and the second heat exchanger, heat transferring medium absorbs heat in First Heat Exchanger, then changes second Heat is discharged in hot device, using the heat in former flue gas, the flue gas Jing Guo desulfurization process is heated by heat transferring medium, improves flue gas Temperature when into denitrating tower.
In the present invention, former flue gas is exchanged heat by First Heat Exchanger, and temperature drops to the temperature of suitable desulfurization, then into Enter and carries out desulfurization process in first order adsorption tower (desulfurizing tower).Flue gas (preliminary treatment flue gas) by desulfurization process is by with Two heat exchangers exchange heat, and increase the temperature to the temperature of suitable denitration, carry out subsequently into second level adsorption tower (denitrating tower) Denitration process.Using active carbon processing system of the invention, flue gas carries out desulfurization and denitration process is all in optimum temperature Lower progress, improves the efficiency of desulfurization and denitration.Waste heat in former flue gas is by First Heat Exchanger and the second heat exchanger for adding The flue gas of hot preliminary treatment, is fully used.It when carrying out fume treatment, does not need additionally to be blended into cold wind or cold air, protect The stabilization for having demonstrate,proved amount of flue gas emission also mitigates the load of desulfurizing tower and denitrating tower.In addition, denitrating tower carries out at a suitable temperature Denitration process, denitration efficiency is high, and ammonia straying quatity is small；The use for reducing ammonia, economizes on resources, and also avoids happy because ammonia is big Amount uses the security risk for leading to escape.
In the present invention, active carbon parses in active carbon Analytic Tower obtains fresh active carbon, then living by first Property charcoal conveying device is delivered to second level adsorption tower, and fresh active carbon carries out at absorption pollutant in the adsorption tower of the second level Reason；Then first order adsorption tower is delivered to by the second active carbon conveying device, the active carbon is in first order adsorption tower to dirt It contaminates object and carries out adsorption treatment.The active carbon being discharged from first order adsorption tower is delivered to active carbon by third active carbon conveying device Analytic Tower is parsed and is regenerated, and is then recycled.
In the present invention, the flue gas that each process generates is former flue gas, is first by the flue gas that first order adsorption tower is handled Step processing flue gas, is discharge flue gas (or neat stress or discharge gas) by the flue gas that second level adsorption tower is handled.
In the present invention, First Heat Exchanger gas transmission pipeline and/or the second heat exchanger gas transmission pipeline are equipped with wind Machine.Blower is for medium (or heat transferring medium) in First Heat Exchanger gas transmission pipeline and the second heat exchanger gas transmission pipeline Circulation and circulation.
In the present invention, the second heat exchanger gas transmission pipeline is equipped with filler, First Heat Exchanger gas transmission pipeline It is equipped with discharge outlet.Carry out the temperature of desulfurization according to the temperature of former flue gas, desulfurizing tower, denitrating tower carries out the temperature of denitration, can be with The water being added from filler is adjusted, or adjusts the water being discharged from discharge outlet, to control and guarantee that flue gas enters Temperature when desulfurizing tower and denitrating tower.
In the present invention, by heat exchange, (first exchanges heat flue gas in the former smoke conveying duct of the first temperature-detecting device detection Device heat exchange) after temperature, that is, detection enter first order adsorption tower (desulfurizing tower) flue gas temperature.Second temperature detection dress It sets for detecting flue gas in preliminary treatment smoke conveying duct by the temperature after (heat exchange of the second heat exchanger) that exchanges heat, that is, examines Survey the temperature for entering the flue gas of second level adsorption tower (denitrating tower).
In the present invention, the end of preliminary treatment smoke conveying duct refers to preliminary treatment smoke conveying duct close to second One end of grade adsorption tower, that is to say, that downstream of the air-flow in preliminary treatment smoke conveying duct.First temperature-detecting device is set Set and refer in the downstream of the first flue gas heat-exchange unit: it is defeated that the first temperature-detecting device and the first flue gas heat-exchange unit are all disposed within former flue gas It send on pipeline, along the flow direction of gas in former smoke conveying duct, the setting of the first temperature-detecting device is changed in the first flue gas After hot device；That is, the original between the first flue gas heat-exchange unit and first order adsorption tower is arranged in the first temperature-detecting device On smoke conveying duct.The downstream that the second flue gas heat-exchange unit is arranged in second temperature detection device refers to: second temperature detection dress It sets and is all disposed on preliminary treatment smoke conveying duct with the second flue gas heat-exchange unit, along gas in preliminary treatment smoke conveying duct The flow direction of body, second temperature detection device are arranged after the second flue gas heat-exchange unit；That is, second temperature detection dress It installs on the preliminary treatment smoke conveying duct between the second flue gas heat-exchange unit and second level adsorption tower.
As shown in Figure 7, it can be seen that influence of the flue-gas temperature to denitration effect.Technical solution of the present invention is as shown in Fig. 5, Process flow is as follows: the temperature of the flue gas (former flue gas) after main exhaust fan is T1 (about 110-170 DEG C), by First Heat Exchanger Former flue-gas temperature is down to temperature T2 (about 110-120 DEG C) afterwards, the former flue gas in T2 temperature range enter desulfurizing tower carry out desulfurization, Dedusting, due to containing 10% or so moisture, 16% or so O in former flue gas2, therefore SO in desulfurizing tower2Sulphur will be converted mainly into Acid, SO2Being oxidized to sulfuric acid is a strong exothermic reaction, therefore active carbon temperature can be than entering the temperature of tower in desulfurizing tower The flue-gas temperature of T2 is 7-10 DEG C high, consider heat loss, and pass through desulfurizing tower after flue-gas temperature still and enter desulfurizing tower Temperature it is almost the same, the flue gas after desulfurization is again introduced into the second heat exchanger by about T2, which is heated to temperature It spends T3 (about 140-155 DEG C), NH then is added under T3 state of temperature3, denitration process is carried out in denitrating tower, improves active carbon Adsorption efficiency.
Active carbon loop direction: active carbon is sent to denitrating tower by transportation system and enters denitration after regenerator regeneration, passes through The active carbon for crossing denitration process is sent to desulfurizing tower and carries out desulfurization, and the active carbon after desulfurization is circulated again by transportation system Regenerator completes an active carbon circulation.Active carbon can be generated largely after desorption rich in sulfur dioxide gas, this portion Gas is divided to be sent to the resource that other process such as relieving haperacidity, reduction elemental sulfur, preparation high concentration liquid SO2, sulphite etc. realize sulphur Change and utilizes.
In the present invention, it is recycled in the first flue gas heat-exchange unit and the second flue gas heat-exchange unit using heat transferring medium.Heat transferring medium (or medium) generally high, incorrosive substance using water, air or other calorific values；Medium is most commonly with for water.It, can by taking water as an example It (is controlled by filler and discharge outlet) according to water, the adjustings such as heat exchanger area enter desulfurizing tower, denitrating tower inlet flue gas temperature Degree.
Using active carbon processing system of the invention, the utilization rate of high-temperature flue gas after main exhaust fan is improved；It is warmed by height Flue gas heat adjusts desulfurizing tower, denitrating tower entrance flue gas temperature by heat exchange, and it is slightly lower to reach desulfurizing tower temperature, denitrating tower temperature It is slightly higher, improve denitrification efficiency.
Using active carbon processing system of the invention, it is more that manageable flue gas can be sintering, coking, waste incineration etc. The flue gas that kind of technique generates, that is to say, that active carbon processing system of the invention can handle sintering flue gas, coking flue gas or It is the flue gas that waste incineration generates.
In the present invention, adsorption tower includes first order adsorption tower and second level adsorption tower, adsorbs tower structure for two-stage.Its In, first order adsorption tower and second level adsorption tower can control arrangement, i.e. first order adsorption tower is arranged in second level adsorption tower Side (left side or right side).First order adsorption tower and second level adsorption tower can also arrange that i.e. second level adsorption tower is set up and down It sets on the top of primary adsorption tower.During gas cleaning, (sintering) containing multiple pollutant former flue gas is adsorbed by the first order Tower carries out desulfurization and dedusting, carries out denitration, NH subsequently into second level adsorption tower3It is added in the smoke inlet of secondary absorption tower.
The main purpose of Analytic Tower is to carry out heating regeneration to the active carbon for having adsorbed pollutant.Analytic Tower divides from top to bottom For a heating section and a cooling section, described a heating section and a cooling section have shell pipe type or pipe type heat exchanger structure.Active carbon passes through respectively By the tube side of a heating section and a cooling section, and heat gas in bringing-up section via shell side, cooling wind is in cooling section via shell side. Buffer area or middle area with a receiving active carbon between a heating section and a cooling section.It lives again in Analytic Tower for heating Property charcoal the combustion heat of the heat from blast furnace gas or coke-stove gas or other materials, such as hot-blast stove exhaust or hot wind or heat it is empty The bringing-up section gas access of gas, hot wind analytically tower enters Analytic Tower, carries out indirect heat exchange with active carbon to be resolved.Heat exchange heat The temperature that wind enters Analytic Tower is 400-500 DEG C, and preferably 410-470 DEG C, more preferably 430-450 DEG C heat after heat exchange The delivery temperature of section gas vent is 300-380 DEG C, preferably 320-375 DEG C, more preferably 340-370 DEG C.In general, hot wind into Enter Analytic Tower and active carbon indirect heat exchange, the hot wind after heat exchange is heated further through hot-blast stove and is recycled, in order to keep The stabilization of pressure and oxygen content in hot air circulating system, the present invention analytically tower bringing-up section gas vent draw second pipe (or branch of the 4th pipeline) is connected to the smoke inlet of second level adsorption tower, the part hot wind after exchanging with active carbon (0.5-30% (preferably 1-20%, more preferably 2-15%)) introduces second level adsorption tower, on the one hand can remove cycling hot SO in wind2, this partial heat on the other hand can be efficiently used, the flue-gas temperature at the adsorption column inlet of the second level is improved, from And denitration efficiency is improved, while the dosage of ammonia can be reduced.
Active carbon parsing technique, the technique the following steps are included:
1) active carbon for having adsorbed pollutant enters active carbon Analytic Tower from the entrance of active carbon Analytic Tower, has adsorbed pollution The active carbon of object under the effect of gravity, moves from up to down, successively decomposes by the preheating zone of active carbon Analytic Tower, vapor Area, First Transition section, pollutant resolver, the second changeover portion, cooling zone；
2) active carbon for having adsorbed pollutant is adsorbed by preheating subsequently into vapor resolver in preheating zone Moisture in the active carbon of pollutant is decomposed and is detached from vapor resolver, then enters First Transition section together, from The moisture for decomposing and detaching in the active carbon of pollutant has been adsorbed to be discharged from steam outlet；
3) active carbon for having adsorbed pollutant after having separated moisture enters pollutant resolver, has adsorbed the work of pollutant Pollutant in property charcoal is decomposed and is parsed in pollutant resolver, subsequently into the second changeover portion, is decomposed and is parsed Pollutant is discharged from SRG gas vent, and the active carbon after having parsed is discharged from the outlet of active carbon Analytic Tower.
In the present invention, cooling wind enters cooling zone from cooling zone gas access, and after heat exchange, from cooling zone, gas vent is defeated It send to vapor resolver and/or preheating zone.
In the present invention, parsing hot wind enters pollutant resolver from pollutant resolver gas access, from dirt after heat exchange Dye object resolver gas vent is delivered to vapor resolver and/or preheating zone.
In the present invention, the gas in vapor resolver after heat exchange is delivered to from vapor resolver gas vent Preheating zone and/or cooling zone.
It is well known that using the device of activated carbon method flue gas desulfurization and denitrification, flue-gas temperature has pollutant removal Great influence, favors low temperature facilitate denitration reaction in desulphurization reaction, high temperature.
The bringing-up section of Analytic Tower is used for the hot wind of heating of Activated charcoal, from the hot wind that bringing-up section gas vent is discharged, part Outer capacity (amount for being delivered to the gas of secondary absorption tower) is about internal circulating load (total amount of the hot wind for heating of Activated charcoal) 10% or so, SO2Content about 100ppm, but the amount of the gas due to being delivered to second level adsorption tower is far smaller than cigarette to be processed Tolerance, after the processing of second level adsorption tower, the SO that is delivered in the gas of second level adsorption tower2It can be good at by the second level Activated carbon adsorption in adsorption tower, will not be to SO in discharge gas at smoke stack emission2Concentration causes big influence.Mesh of the invention Be prevent SO contained in the hot air circulation gas for parsing2Direct outlet.
In the device of the invention, it will be used to heat the hot wind of active carbon in Analytic Tower, analytically tower bringing-up section or vapor Resolver discharge in the hot wind after active carbon heat exchange a part (such as 0.5-30%, preferably 1-20%, more preferably 2-15%) by third pipeline to the smoke inlet of second level adsorption tower；It changes part heat in the prior art The technical solution of wind direct emission.By the way that part hot wind of the Analytic Tower heat exchanging segment after heat exchange is delivered to second level adsorption tower It is handled, avoids the direct outlet of part hot wind, prevented pollution of the pollutant to environment in the hot wind.Simultaneously as The temperature of the part hot wind is higher, is delivered to the air inlet of second level adsorption tower, with the original flue gas for entering second level adsorption tower Mixing improves the entire flue-gas temperature for entering second level adsorption tower, improves secondary absorption tower to the out of stock efficiency of flue gas.
In addition, in the prior art, due to discharging SO to control using by the direct outlet of part circulating air2Amount, only Few a part of hot wind can be subjected to outlet, constrain the heat exchange efficiency of circulating air and active carbon；Since internal circulating load is less, mend The air quantity being charged into hot-blast stove is also smaller, and therefore, in the program, hot-blast stove is constantly in hypoxia burning, causes fuel not Energy full combustion, causes the waste of resource.Using the design of the application, inhaled since part circulating air is delivered to the second level Attached tower, second level adsorption tower can be handled the part hot wind, after treatment from smoke stack emission, therefore, Ke Yigen According to needs, therefore the hot blast rate that increase is delivered to second level adsorption tower can fill into a greater amount of skies from the gas supplementing opening of hot-blast stove Gas increases the oxygen content in hot-blast stove, improves the combustion rate of fuel, makes its full combustion, saves fuel source；Together When, since fuel combustion is abundant, calorific value is higher, also improve from hot-blast stove convey hot wind enter Analytic Tower after, hot wind and activity The heat exchange efficiency of charcoal.
Using the device of the application, can also by detecting the temperature of the flue gas after the processing of first order adsorption tower, according to Active carbon carries out the best theoretical temperatures of denitration process to flue gas, controls from third pipeline to the hot wind of second level adsorption tower Amount, when so that the part hot wind being delivered to second level adsorption tower, and treated after flue gas mix by first order adsorption tower, mixed The temperature for closing gas is the temperature for being most suitable for active carbon and carrying out denitration process, improves second level adsorption tower and imitates to the denitration of flue gas Rate.If the temperature of flue gas is higher after the processing of first order adsorption tower, reduce from third pipeline to second level adsorption tower Hot blast rate；If the temperature of flue gas is lower after the processing of first order adsorption tower, increase from third pipeline to the second level The hot blast rate of adsorption tower.
Therefore, using the device of the invention, wind Analytic Tower being used in the circulating air of heating of Activated charcoal is conveyed To second level adsorption tower: first, it avoids by the direct outlet of part hot wind, due to SO in hot wind2Presence bring pollution ring The problem of border；Second, due to the part, hot wind is delivered to second level adsorption tower, can increase and branch to second from circulating air The hot blast rate of grade adsorption tower, improves the efficiency of combustion of fuel in hot-blast stove, economizes on resources；Third, the part hot wind are delivered to Secondary absorption tower, and treated after flue gas mixes by first order adsorption tower, improves to be processed in the adsorption tower of the second level The temperature of flue gas, improves denitration efficiency.
Preferably, using special parsing tower structure, by active carbon Analytic Tower (or being Analytic Tower) and under It is set as preheating zone, vapor resolver, pollutant resolver, cooling zone, First Transition section and the second changeover portion；And The side wall of one changeover portion is equipped with steam outlet.So that the active carbon containing pollutant after entering Analytic Tower, first carries out pre- Then heat carries out the removing of moisture, from the moisture being removed in active carbon from First Transition section side wall in vapor resolver Steam outlet be expelled directly out, directly eliminate the moisture in active carbon containing pollutant.Then, that removes moisture removal contains pollutant Active carbon decompose and the removing of pollutant in pollutant resolver again, is substantially carried out the decomposition of sulphur-containing substance, pollutant from SRG gas vent discharge on second changeover portion side wall；Moisture content is few the SRG gas being discharged herein in, convenient for subsequent Relieving haperacidity process.Active carbon containing pollutant removes moisture in vapor resolver, removes other pollutants in pollutant resolver Afterwards, it is activated and is regenerated, then passed it through cooling zone again and cooled down, obtain fresh active carbon, be recycled to absorption Tower carry out using.
In the present invention, retaining I area is preheating zone, and old-fashioned desorber bringing-up section is divided into two sections, i.e. Section II area For vapor resolver；Temperature controls in 100-300 DEG C of section, and the moisture adsorbed in active carbon (Free water or the crystallization water) is gone It removes；Section III area is the pollutant resolver of ammonium sulfate or other pollutants, is substantially carried out SO2Decomposition, outlet temperature 400- 550 DEG C, and stop certain time, it is ensured that active carbon desorbs completely.Section IV area active carbon cooling zone.
In the present invention, according to the decomposition temperature of moisture in absorption pollutant active carbon, the temperature of vapor resolver is controlled Degree so that the moisture in absorption pollutant active carbon is decomposed in vapor resolver, and pollutant again in this section not It changes and (does not decompose and remove), moisture is removed from absorption pollutant active carbon in vapor resolver, then from the Steam outlet discharge on one changeover portion side wall.The temperature of vapor resolver is generally 100-200 DEG C, preferably 105- 190 DEG C, more preferably 110-180 DEG C.
In the present invention, according to the decomposition temperature of pollutant (sulphur-containing substance or other pollutants) in absorption pollutant active carbon Degree controls the temperature of pollutant resolver, so that the pollutant in absorption pollutant active carbon carries out in pollutant resolver It decomposes, pollutant removes completely from active carbon, then from the SRG gas vent discharge on the second changeover portion side wall.Pollutant The temperature of resolver is generally 400-550 DEG C, preferably 410-500 DEG C, more preferably 420-480 DEG C.
In the present invention, desorber hot wind process: hot wind movement flow direction is by the way of bottom in and top out, first from active carbon Bringing-up section outlet enters, and is entered by the entrance that pollutant decomposes section, then is discharged from the outlet that pollutant decomposes section, then The entrance entrance that vapor decomposes section is entered back into, is then discharged again from the outlet that vapor decomposes section.
The centre of vapor resolver and pollutant resolver is the first transition, is active carbon layer, is substantially carried out water steaming The outlet of gas；It is internal also to contain volatile NH3.It is the second changeover portion between pollutant resolver and cooling zone, is active carbon Layer of charcoal is substantially carried out rich in SO2The outlet of gas.The water vapour content about 500Nm of first transition discharge3/ h or so is (containing micro Ammonia), it can be discharged into the former flue gas of sintering.For the moisture discharge into former sintering flue gas, first will not influence sintering flue gas It forms (since former sintering flue gas amount is huge, the vapor of the ratio will not influence the composition of former sintering flue gas completely), second can With the ammonia for utilizing the inside to contain again, reach the effective use of resource.
In the present invention, it solves to contain 30% in SRG gas in Analytic Tower (desorber of prototype structure) in the prior art The moisture content of left and right, the problem of not utilizing subsequent technique to run；By adsorbing pollutant decomposition temperature different principle, will desorb Tower bringing-up section is divided into vapor resolver and pollutant resolver, and wherein vapor resolver carries out the moisture of activated carbon adsorption The decomposition of (Free water and combine water), it is also possible to contain micro ammonia；Pollutant resolver is sulfate or other materials Watershed area, main decomposition go out a large amount of SO2Gas or other materials, moisture content substantially reduce.It then is below active carbon Cooling zone, the active carbon of heating is cooling.The steam vapour amount that active carbon decomposes is few, can be sent to former flue, micro using the inside Ammonia；Moisture content greatly reduces in SRG gas, SO2Volume fraction greatly increases, and facilitates subsequent handling.
In the present invention, can make full use of in active carbon each section in Analytic Tower (preheating zone, vapor resolver, Pollutant resolver, cooling zone) heat that exchanges heat；According to active carbon or each section of active carbon of pollutant is adsorbed In, respective technique, in other words each section of Analytic Tower to active carbon or adsorbed pollutant progress effect or technique, control The temperature of each section (preheating zone, vapor resolver, pollutant resolver, cooling zone) air inlet (or air inlet) is made, To control the temperature of active carbon in each section of Analytic Tower, its each respective function of section is realized.It is each into Analytic Tower After the cold wind or hot wind (or gas) of section with the active carbon in the section by being exchanged heat, go out from the gas of respective segments Mouth discharge is input to other sections according to the temperature conditions adaptability of the discharge gas then according to the temperature of discharge gas The gas access of (section for needing the temperature gas), is recycled or is recycled；Make full use of the heat of recuperated gas Amount, economizes on resources.
In the present invention, cooling wind is input to cooling zone from cooling zone gas access by cooling gas conveyance conduit.Heat Wind is transported to pollutant resolver from pollutant resolver gas access by hot blast conveying pipe road.
In the present invention, according to the temperature from pollutant resolver gas vent discharge gas, pollutant resolver gas Export the gas property of can choose of discharge is delivered to vapor decomposition from vapor resolver gas access by conveyance conduit Area, or preheating zone is delivered to from preheating zone gas access by conveyance conduit.In actual process, according to pollutant resolver gas The temperature of body outlet discharge gas, vapor resolver and preheating zone need the temperature of hot wind (or hot gas) medium, selection Property slave pollutant resolver gas vent discharge gas be delivered to the wherein gas access of vapor resolver and/or preheating The gas access in area, for exchanging heat in vapor resolver or preheating zone with active carbon.
In the present invention, according to the temperature from cooling zone gas vent discharge gas, the gas of cooling zone gas vent discharge The body property of can choose is delivered to preheating zone from preheating zone gas access by the 5th pipeline, or is steamed by the 5th pipeline from water Gas resolver gas access is delivered to vapor resolver.In actual process, the temperature of gas is discharged according to cooling zone gas vent Degree, vapor resolver and preheating zone need the temperature of hot wind (or hot gas) medium, selective to go out from cooling zone gas The gas of mouth discharge is delivered to the wherein gas access of the gas access of vapor resolver and/or preheating zone.
In the present invention, according to the temperature from vapor resolver gas vent discharge gas, vapor resolver gas Export the hot-wind inlet that hot-blast stove is connected to by second pipe of the gas property of can choose of discharge；Or pass through the second conveying Pipeline is delivered to preheating zone from preheating zone gas access, or is delivered to from cooling zone gas access by the second conveyance conduit cold But area.In actual process, the temperature of gas is discharged according to vapor resolver gas vent, preheating zone and cooling zone need hot wind The temperature of (or hot gas) medium, the selective gas being discharged from vapor resolver gas vent, which is delivered to, wherein to be preheated The gas access in area and/or the gas access of cooling zone.
In the present invention, which further includes the nitrogen delivery pipe that nitrogen is passed through to active carbon Analytic Tower top Road.It is protected in resolving using nitrogen, the SO that nitrogen is used as carrier that will parse simultaneously2Equal pernicious gases are taken out of. Nitrogen gas delivery-line is equipped with nitrogen heat exchanger.4th pipeline and/or the gas of the 6th pipeline can connect to nitrogen and changes The entrance of the heating medium passage of hot device；4th pipeline and/or the gas of the 6th pipeline with nitrogen for exchanging heat.
In the present invention, according to the temperature from preheating zone gas vent discharge gas, the gas of preheating zone gas vent discharge The body property of can choose is delivered to nitrogen heat exchanger from the entrance of the heating medium passage of nitrogen heat exchanger by the 6th pipeline, or Person is delivered to cooling zone from cooling zone gas access by the 6th conveyance conduit.In actual process, according to preheating zone gas vent The temperature of gas is discharged, nitrogen heat exchanger and cooling zone need the temperature of gas (or wind) medium, selective from preheating zone The gas of gas vent discharge is delivered to the gas of the wherein gas access and/or cooling zone of the heating medium passage of nitrogen heat exchanger Body entrance.
In the present invention, when handling in adsorption tower former flue gas due to active carbon, ammonia has been sprayed into adsorption tower, Active carbon has also adsorbed part ammonia in adsorption tower, living when having adsorbed the active carbon of pollutant and being parsed in Analytic Tower again Property charcoal in adsorb ammonia removed in this section of vapor resolver, vapor resolver removing vapor and ammonia Gas, the gas being discharged from First Transition section can be delivered to former smoke conveying duct by the 5th conveyance conduit, by ammonia recycle It utilizes, economizes on resources.
In the present invention, the cooling wind blower on cooling gas conveyance conduit is used to convey cooling gas to cooling zone.Heat Air-heater on wind conveyance conduit is used for pollutant resolver heat air delivery.
In general, there is shell pipe type or pipe type to change for the preheating zone, vapor resolver, pollutant resolver, cooling zone Hot device structure.Active carbon is respectively via the tube side of preheating zone, vapor resolver, pollutant resolver, cooling zone, and pre- hot gas Body is via shell side in preheating zone, and via shell side in vapor resolver and pollutant resolver, cooling wind exists heat gas Via shell side in cooling zone.Between vapor resolver and pollutant resolver with one receiving active carbon buffer area or Middle area is First Transition section；Between pollutant resolver and cooling zone with one receiving active carbon buffer area or in Between area, be the second changeover portion.
Novel absorbent charcoal Analytic Tower provided by the invention, it is different according to the pollutant decomposition temperature adsorbed in active carbon, it will Vapor is separated in advance in desorption gas progress, provides help for the stable operation of subsequent technique.Pollutant is adsorbed For active carbon in Analytic Tower, the moisture adsorbed in active carbon carries out decomposition disengaging in vapor resolver first, vapor from The steam outlet of Analytic Tower is discharged, and the active carbon continuation for having adsorbed other pollutants for being stripped of vapor solves in Analytic Tower The removing of analysis and pollutant, sulphur-containing substance and other pollutants are decomposed and are removed in the pollutant resolver of Analytic Tower, analytically The SRG gas vent of tower is discharged.Since vapor is most removed and is discharged first, referring now to the prior art, mentioned using the application The novel absorbent charcoal Analytic Tower of confession, moisture content greatly reduces from the SRG gas that SRG gas vent is discharged, due to SRG gas Temperature is higher, and must cool down processing when into acid making system, since moisture content is few in SRG gas, the difficulty of cooling is big It is big to reduce.The process cooling generally adopt be water-cooled or water heat exchange, since moisture content itself is few in SRG gas, cooling be added Cooling water greatly reduce, and cooling efficiency greatly increase (since moisture content itself is few in SRG gas, the specific heat of water Hold big).Therefore, using active carbon Analytic Tower provided by the present application, cooling procedure letter of the SRG gas of acquisition for acid-making process Cooling water single, being added is few, cooling efficiency is high.
The wastewater treatment of acid-making process is the great difficult problem of the technology, and since wastewater flow rate is big, in waste water, acidity is big, pollutant Broad categories contain the features such as organic matter, and waste water treatment process is the key link of acid-making process.Using the active carbon of the application Analytic Tower greatly reduces the moisture content in SRG gas from source, and the cooling water being added in cooling procedure is further reduced, So that the wastewater flow rate that acid making system generates greatly reduces, after the device of the application, the waste water that acid-making process generates is about For the 30-60% for generating wastewater flow rate in the prior art, wastewater treatment workload and wastewater treatment difficulty are reduced.The waste water of generation Amount is reduced, and the total amount of pollutant is constant, so that the pollutant concentration liter after using the active carbon Analytic Tower of the application, in waste water Height, processing (separation or enrichment) significant effect increase.
In addition, moisture content is few in the SRG gas of parsing after using the active carbon Analytic Tower of the application, into relieving haperacidity system Cooling technique before system more efficiently and is stablized, and since the content of the big moisture of specific heat capacity greatly reduces, mainly carries out to gas Cooling, control is simpler, and cooling technique is more stable, and cooling effect is more guaranteed；It more can accurately grasp and entering glass When the relieving haperacidity process of glass steel material, the temperature of SRG gas, to ensure that the safety of the acid making system of glass steel material, simultaneously It prolongs its service life.
Tower structure is parsed using the active carbon of the application, water in desorber SRG gas in the prior art can be solved perfectly The problem for dividing content excessive creates conditions for subsequent relieving haperacidity stable operation, and can be reduced Wastewater from Acid Preparation treating capacity.
In the present invention, Analytic Tower and active carbon Analytic Tower are general, and adsorption tower and activated carbon adsorber are general.
In the present invention, the downstream that first order adsorption tower is arranged in second level adsorption tower refers to: according to walking for flow of flue gas To flue gas first passes through first order adsorption tower, using second level adsorption tower；Second level adsorption tower is located at first order absorption tower flue gas The downstream of flow direction.
In the present invention, the first active carbon conveying device, the second active carbon conveying device, third active carbon conveying device are equal It, can be using any conveying device in the prior art for conveying active carbon.
In the present invention, preheating zone, vapor resolver, pollutant resolver and cooling zone are shell structure.
Preferably, heat exchanger is electric heater.
The work of pollutant will have been adsorbed in active carbon Analytic Tower using the active carbon parsing tower structure of the application first Moisture in property charcoal is decomposed and is detached from vapor resolver；Since the temperature that the decomposition of vapor needs is lower, generally It is 100-150 DEG C, therefore, the temperature in vapor resolver is 100-150 DEG C.Active carbon behind vapor resolver into Enter pollutant resolver, in the section, need active carbon being heated to 410-460 DEG C, is generally heated using hot-blast stove Processing.In the prior art, the pollutant (including moisture) for needing to adsorb in active carbon and active carbon is heated to pollutant Decomposition temperature (410-460 DEG C), the active carbon Analytic Tower of the application since the moisture in active carbon being separated in advance, The moisture separated does not enter pollutant resolver, also just reduce pollutant resolver give separate moisture heat Heat；Therefore, using the active carbon Analytic Tower of the application, in pollutant resolver, the heat of consumption is considerably less than in the prior art The heat of active carbon Analytic Tower bringing-up section consumption.
Tower structure is parsed using the active carbon of the application, moisture is separated in advance in vapor resolver, is avoided The part water enters pollutant resolver, also avoids the heat consumption heated in pollutant resolver to the part water, reduces Heat consumption in active carbon resolving, has saved the energy, while reducing the discharge of energy burning pollutant.
After vapor is decomposed and is detached from vapor resolver, it is discharged from steam outlet, does not enter pollutant resolver；From And moisture content greatly reduces from the SRG gas that SRG gas vent is discharged.SRG gas is delivered to the progress of relieving haperacidity purification device When processing, need to cool down to SRG gas, since the moisture content in SRG gas is few, cool down to the portion gas Workload it is small, cool down it is high-efficient.General use is blended into cold water cooling, since the moisture contained in itself in SRG gas is reduced, is The cool water quantity that cooling is blended into is reduced, to reduce the wastewater flow rate of relieving haperacidity cleaning procedure generation.Further, since in SRG gas The moisture itself contained is few, and the cold water being blended into is further reduced, to improve the volumetric concentration of sulfur dioxide.
Wherein: the height of Analytic Tower is 8-30 meters, preferably 10-25 meters, more preferably 12-20 meters；Such as 15m or so. The diameter of second pipe be 0.1-1.2 meters, preferably 0.2-1.0 meters, further preferably 0.3-0.8 meters, more preferably 0.4- 0.6 meter.
In the present invention: the height of active carbon Analytic Tower is 8-30 meters, preferably 10-25 meters, more preferably 12-20 meters； Such as 15m or so.18-35 meters of the height of activated carbon adsorber, preferably 20-30 meters, more preferably 24-28m.
Compared with prior art, the present invention has following advantageous effects:
1, it by the way that heat exchanger is respectively set before flue gas inputs first order adsorption tower and second level adsorption tower, can control Flue gas enters temperature when first order adsorption tower and second level adsorption tower, to ensure that the temperature of desulfurization and denitration, improves de- The efficiency of sulphur denitration；
2, the first flue gas heat-exchange unit and the second flue gas heat-exchange unit are recycled by heat transferring medium, make full use of heat, save money Discharge is reduced in source；Reduce the straying quatity of ammonia while improving denitrification efficiency by the setting of heat exchanger；In addition, It avoids and converts cold wind, reduce the amount of flue gas emission of active carbon processing system processing.
3, apparatus of the present invention analytically draw second pipe and be connected to the cigarette of secondary absorption tower by the bringing-up section gas vent of tower Gas entrance, by the prior art analytically the direct outlet of bringing-up section gas vent of tower hot wind introduce secondary absorption tower, effectively Prevent SO contained in this part hot wind2Direct outlet, reduces environmental pollution；
4, the present invention will introduce secondary absorption tower with the part hot wind after active carbon heat exchange, efficiently use this part heat Amount improves the flue-gas temperature of secondary absorption tower inlet, to improve denitration efficiency；
5, the application develops a kind of new desorption tower structure, different according to the pollutant decomposition temperature adsorbed in active carbon, By desorption gas carry out in vapor separated in advance, provide help for the stable operation of subsequent technique；Using the application's Active carbon Analytic Tower, it is few to parse moisture content in the SRG gas of acquisition, in the cooling procedure before relieving haperacidity process, consumption Cooling water is few；After relieving haperacidity process, the wastewater flow rate of generation is few；
6, using the active carbon Analytic Tower of the application, it is few to parse moisture content in the SRG gas of acquisition, to SRG gas Cooling technique is simple, and cooling efficiency greatly improves, and ensure that the gas temperature into the relieving haperacidity process of glass steel material, to protect The safety for having demonstrate,proved glass-reinforced plastic material device extends its service life.
7, the device of the invention can be used for being sintered, coking, the various actives charcoal smoke gas treatment field such as waste incineration, it is especially suitable For the operating condition of low exhaust gas volumn, heating effect and the better effect for improving denitrification rate.
Detailed description of the invention
Fig. 1 is a kind of structural schematic diagram for the active carbon processing system for improving utilization rate of waste heat and denitrification rate of the present invention；
Fig. 2 is a kind of knot of another design of active carbon processing system for improving utilization rate of waste heat and denitrification rate of the present invention Structure schematic diagram；
Fig. 3 is that not grace recycles Analytic Tower in a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate of the present invention Hot wind is delivered to the structural schematic diagram of first smoke conveying duct；
Fig. 4 is active carbon Thermal desorption tower in a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate of the present invention Structural schematic diagram；
Fig. 5 is active carbon Thermal desorption tower in a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate of the present invention Attachment structure schematic diagram；
Fig. 6 is active carbon Thermal desorption tower in a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate of the present invention Structural schematic diagram equipped with nitrogen heat exchanger；
Fig. 7 is the graph of relation of flue-gas temperature and denitrification rate.
Appended drawing reference:
1: activated carbon adsorber；101: first order adsorption tower；102: second level adsorption tower；2: active carbon Analytic Tower；3: the One flue gas heat-exchange unit；4: the second flue gas heat-exchange units；5: bringing-up section；501: bringing-up section gas access；502: bringing-up section gas vent； 6: cooling section；7: hot-blast stove；701: hot-wind inlet；702: hot-blast outlet；703: wind-supplying mouth；8: chimney；9: blower；10: draining Mouthful；11: filler；L1: former smoke conveying duct；L2: preliminary treatment smoke conveying duct；L3: first pipe；L4: the second pipe Road；L5: third pipeline；L6: cooling gas conveyance conduit；L7: the four pipeline；L8: the five pipeline；L9: nitrogen gas delivery-line； L10: the six pipeline；L11: the seven pipeline；L12:SRG gas transmission pipeline；L13: the eight pipeline；L14: First Heat Exchanger medium Conveyance conduit；L15: the second heat exchanger media conveyance conduit；D1: the first active carbon conveying device；D2: the second active carbon conveying dress It sets；D3: third active carbon conveying device；A1: preheating zone；A101: preheating zone gas access；A102: preheating zone gas vent； A2: vapor resolver；A201: vapor resolver gas access；A202: vapor resolver gas vent；A3: pollutant Resolver；A301: pollutant resolver gas access；A302: pollutant resolver gas vent；A4: cooling zone；A401: cold But area gas access；A402: cooling zone gas vent；A5: First Transition section；A6: the second changeover portion；A7: steam outlet； A8:SRG gas vent；A9: nitrogen heat exchanger；A10: cooling wind blower；A11: air-heater；P1: the first temperature-detecting device； P2: second temperature detection device.
Specific embodiment
The first embodiment provided according to the present invention provides a kind of active carbon for improving utilization rate of waste heat and denitrification rate Processing system.
A kind of active carbon processing system improving utilization rate of waste heat and denitrification rate, which includes active carbon Adsorption tower 1, active carbon Analytic Tower 2.The activated carbon adsorber 1 is two-stage adsorption tower, including first order adsorption tower 101 and second Grade adsorption tower 102.The active carbon processing system further includes that former smoke conveying duct L1, the first flue gas heat-exchange unit 3, the second flue gas change Hot device 4, preliminary treatment smoke conveying duct L2, the first active carbon conveying device D1, the second active carbon conveying device D2, third are living Property charcoal conveying device D3.
Wherein: former smoke conveying duct L1 is connected to the smoke inlet of first order adsorption tower 101.First order adsorption tower 101 Exhanst gas outlet the smoke inlet of second level adsorption tower 102 is connected to by preliminary treatment smoke conveying duct L2.First flue gas Heat exchanger 3 is arranged on former smoke conveying duct L1.Second flue gas heat-exchange unit 4 is arranged in preliminary treatment smoke conveying duct L2 On.The active carbon of the active carbon outlet and second level adsorption tower 102 of first active carbon conveying device D1 connection active carbon Analytic Tower 2 Entrance.The work of the active carbon outlet and first order adsorption tower 101 of second active carbon conveying device D2 connection second level adsorption tower 102 Property charcoal entrance.Active carbon outlet and the active carbon Analytic Tower 2 of third active carbon conveying device D3 connection first order adsorption tower 101 Active carbon entrance.
Preferably, active carbon Analytic Tower 2 is equipped with bringing-up section 5 and cooling section 6 from top to bottom.The lower part of bringing-up section 5 is equipped with The top of bringing-up section gas access 501, bringing-up section 5 is equipped with bringing-up section gas vent 502.The device further includes hot-blast stove 7.Hot wind Furnace 7 is equipped with hot-wind inlet 701 and hot-blast outlet 702.The first pipe L3 connection drawn from the hot-blast outlet 702 of hot-blast stove 7 To the bringing-up section gas access 501 of active carbon Analytic Tower 2.The second pipe L4 drawn from bringing-up section gas vent 502 is connected to The hot-wind inlet 701 of hot-blast stove 7.A branch i.e. third pipeline L5 is separated from second pipe L4, third pipeline L5 is connected to just The smoke inlet of step processing smoke conveying duct L2 or second level adsorption tower 102.
Preferably, institute's active carbon Analytic Tower 2 includes preheating zone A1, the vapor resolver A2, dirt being arranged from top to bottom Contaminate object resolver A3, cooling zone A4, First Transition section A5 and the second changeover portion A6.
Wherein: the lower part of preheating zone A1 is equipped with preheating zone gas access A101 and preheating zone gas vent A102.Vapor The lower part of resolver A2 is equipped with vapor resolver gas access A201 and vapor resolver gas vent A202.Pollutant point The lower part for solving area A3 is equipped with pollutant resolver gas access A301 and pollutant resolver gas vent A302.Cooling zone A4's Lower part is equipped with cooling zone gas access A401 and cooling zone gas vent A402.Vapor resolver A2 and pollutant resolver A3 Between be First Transition section A5.It is the second changeover portion A6 between pollutant resolver A3 and cooling zone A4.First Transition section A5's Side wall is equipped with steam outlet A7.The side wall of second changeover portion A6 is equipped with SRG gas vent A8.
Preferably, the device further includes hot-blast stove 7.Hot-blast stove 7 is equipped with hot-wind inlet 701 and hot-blast outlet 702.It is cold But area gas access A401 is connect with cooling gas conveyance conduit L6.The first pipe drawn from the hot-blast outlet 702 of hot-blast stove 7 L3 is connected to pollutant resolver gas access A301.Pollutant resolver gas vent A302 is connected to by the 4th pipeline L7 Vapor resolver gas access A201.Vapor resolver gas vent A202 is connected to hot-blast stove 7 by second pipe L4 Hot-wind inlet 701.
Preferably, separating a branch i.e. third pipeline L5 from second pipe L4, third pipeline L5 is connected to preliminary place Manage the smoke inlet of smoke conveying duct L2 or second level adsorption tower 102.
Preferably, cooling zone gas vent A402 is connected to preheating zone gas access A101 by the 5th pipeline L8.
Preferably, the active carbon Analytic Tower 2 further includes the nitrogen delivery pipe for being passed through nitrogen to 2 top of active carbon Analytic Tower Road L9.Nitrogen gas delivery-line L9 is connected to Analytic Tower 2, and the link position of nitrogen gas delivery-line L9 and active carbon Analytic Tower 2 Positioned at the top of preheating zone A1.
Preferably, nitrogen gas delivery-line L9 is equipped with nitrogen heat exchanger A9.Preheating zone gas vent A102 passes through the 6th Pipeline L10 is connected to the entrance of the heating medium passage of nitrogen heat exchanger A9.
Preferably, steam outlet A7 is delivered to former smoke conveying duct L1 by the 7th pipeline L11.
Preferably, SRG gas vent A8 is delivered to acid making system by SRG gas transmission pipeline L12.
Preferably, cooling gas conveyance conduit L6 is equipped with cooling wind blower A10.
Preferably, first pipe L3 is equipped with air-heater A11.
Preferably, being additionally provided with wind-supplying mouth 703 on hot-blast stove 7.
Preferably, the device further includes chimney 8.The exhanst gas outlet of second level adsorption tower 102 connects via the 8th pipeline L13 It is connected to chimney 8.
Preferably, the gas vent of the first flue gas heat-exchange unit 3 is connected to by First Heat Exchanger medium delivery pipe road L14 The gas access of second flue gas heat-exchange unit 4.The gas vent of second flue gas heat-exchange unit 4 passes through the second heat exchanger media conveyance conduit L15 is connected to the gas access of the first flue gas heat-exchange unit 3.
Preferably, being set on First Heat Exchanger medium delivery pipe road L14 and/or the second heat exchanger media conveyance conduit L15 There is blower 9.
Preferably, First Heat Exchanger medium delivery pipe road L14 is equipped with discharge outlet 10.
Preferably, the second heat exchanger media conveyance conduit L15 is equipped with filler 11.
Preferably, original smoke conveying duct L1 is equipped with the first temperature-detecting device P1, and the first temperature detection fills Set the downstream that the first flue gas heat-exchange unit 3 is arranged in P1.
Preferably, preliminary treatment smoke conveying duct L2 is equipped with second temperature detection device P2, and second temperature The downstream of the second flue gas heat-exchange unit 4 is arranged in detection device P2.
In the present invention, first order adsorption tower 101 is desulfurizing tower, and second level adsorption tower 102 is denitrating tower.
Embodiment 1
As shown in Figure 1, a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate, the active carbon processing system Including activated carbon adsorber 1, active carbon Analytic Tower 2.The activated carbon adsorber 1 is two-stage adsorption tower, including the first order is adsorbed Tower 101 and second level adsorption tower 102.The active carbon processing system further includes former smoke conveying duct L1, the first flue gas heat-exchange unit 3, the second flue gas heat-exchange unit 4, preliminary treatment smoke conveying duct L2, the first active carbon conveying device D1, the conveying of the second active carbon Device D2, third active carbon conveying device D3.
Wherein: former smoke conveying duct L1 is connected to the smoke inlet of first order adsorption tower 101.First order adsorption tower 101 Exhanst gas outlet the smoke inlet of second level adsorption tower 102 is connected to by preliminary treatment smoke conveying duct L2.First flue gas Heat exchanger 3 is arranged on former smoke conveying duct L1.Second flue gas heat-exchange unit 4 is arranged in preliminary treatment smoke conveying duct L2 On.The active carbon of the active carbon outlet and second level adsorption tower 102 of first active carbon conveying device D1 connection active carbon Analytic Tower 2 Entrance.The work of the active carbon outlet and first order adsorption tower 101 of second active carbon conveying device D2 connection second level adsorption tower 102 Property charcoal entrance.Active carbon outlet and the active carbon Analytic Tower 2 of third active carbon conveying device D3 connection first order adsorption tower 101 Active carbon entrance.The device further includes chimney 8.The exhanst gas outlet of second level adsorption tower 102 is connected to cigarette via the 8th pipeline L13 Chimney 8.
Embodiment 2
As shown in Fig. 2, repeating embodiment 1, only the gas vent of the first flue gas heat-exchange unit 3 passes through First Heat Exchanger medium Conveyance conduit L14 is connected to the gas access of the second flue gas heat-exchange unit 4.The gas vent of second flue gas heat-exchange unit 4 passes through second Heat exchanger media conveyance conduit L15 is connected to the gas access of the first flue gas heat-exchange unit 3.First Heat Exchanger medium delivery pipe road L3 It is equipped with blower 5.First Heat Exchanger medium delivery pipe road L3 and/or the second heat exchanger media conveyance conduit L4 is equipped with blower 9.
Embodiment 3
Embodiment 2 is repeated, only the second heat exchanger media conveyance conduit L15 is equipped with filler 11.First Heat Exchanger is situated between Matter conveyance conduit L14 is equipped with discharge outlet 10.The active carbon processing system further includes chimney 8.The gas of second level adsorption tower 102 Outlet is connect by flue gas exhausting pipe line L13 with chimney 8.
Embodiment 4
Embodiment 3 is repeated, only original smoke conveying duct L1 is equipped with the first temperature-detecting device P1, and the first temperature The downstream of the first flue gas heat-exchange unit 3 is arranged in detection device P1.Preliminary treatment smoke conveying duct L2 is examined equipped with second temperature Device P2 is surveyed, and the downstream of the second flue gas heat-exchange unit 4 is arranged in second temperature detection device P2.
Embodiment 5
As shown in figure 3, repeating embodiment 3, only active carbon Analytic Tower 2 is equipped with bringing-up section 5 and cooling section 6 from top to bottom. The lower part of bringing-up section 5 is equipped with bringing-up section gas access 501, and the top of bringing-up section 5 is equipped with bringing-up section gas vent 502.The device It further include hot-blast stove 7.Hot-blast stove 7 is equipped with hot-wind inlet 701 and hot-blast outlet 702.Draw from the hot-blast outlet 702 of hot-blast stove 7 First pipe L3 out is connected to the bringing-up section gas access 501 of active carbon Analytic Tower 2.It is drawn from bringing-up section gas vent 502 Second pipe L4 be connected to the hot-wind inlet 701 of hot-blast stove 7.A branch i.e. third pipeline L5 is separated from second pipe L4, Third pipeline L5 is connected to the smoke inlet of preliminary treatment smoke conveying duct L2 or second level adsorption tower 102.First pipe L3 It is equipped with air-heater A11.Wind-supplying mouth 703 is additionally provided on hot-blast stove 7.
Embodiment 6
As shown in figure 4, repeat embodiment 3, only institute's active carbon Analytic Tower 2 include be arranged from top to bottom preheating zone A1, Vapor resolver A2, pollutant resolver A3, cooling zone A4, First Transition section A5 and the second changeover portion A6.
Wherein: the lower part of preheating zone A1 is equipped with preheating zone gas access A101 and preheating zone gas vent A102.Vapor The lower part of resolver A2 is equipped with vapor resolver gas access A201 and vapor resolver gas vent A202.Pollutant point The lower part for solving area A3 is equipped with pollutant resolver gas access A301 and pollutant resolver gas vent A302.Cooling zone A4's Lower part is equipped with cooling zone gas access A401 and cooling zone gas vent A402.Vapor resolver A2 and pollutant resolver A3 Between be First Transition section A5.It is the second changeover portion A6 between pollutant resolver A3 and cooling zone A4.First Transition section A5's Side wall is equipped with steam outlet A7.The side wall of second changeover portion A6 is equipped with SRG gas vent A8.
The device further includes hot-blast stove 7.Hot-blast stove 7 is equipped with hot-wind inlet 701 and hot-blast outlet 702.Cooling zone gas Entrance A401 is connect with cooling gas conveyance conduit L6.The first pipe L3 drawn from the hot-blast outlet 702 of hot-blast stove 7 is connected to Pollutant resolver gas access A301.Pollutant resolver gas vent A302 is connected to vapor point by the 4th pipeline L7 The gas access Xie Qu A201.Vapor resolver gas vent A202 is entered by the hot wind that second pipe L4 is connected to hot-blast stove 7 Mouth 701.
A branch i.e. third pipeline L5 is separated from second pipe L4, third pipeline L5 is connected to the conveying of preliminary treatment flue gas Pipeline L2.Cooling zone gas vent A402 is connected to preheating zone gas access A101 by the 5th pipeline L8.
Cooling gas conveyance conduit L6 is equipped with cooling wind blower A10.
Embodiment 7
As shown in fig. 6, repeating embodiment 5, only the active carbon Analytic Tower 2 further includes logical to 2 top of active carbon Analytic Tower Enter the nitrogen gas delivery-line L9 of nitrogen.Nitrogen gas delivery-line L9 is connected to Analytic Tower 2, and nitrogen gas delivery-line L9 and active carbon The link position of Analytic Tower 2 is located at the top of preheating zone A1.Nitrogen gas delivery-line L9 is equipped with nitrogen heat exchanger A9.Preheating zone gas Body outlet A102 is connected to the entrance of the heating medium passage of nitrogen heat exchanger A9 by the 6th pipeline L10.
Steam outlet A7 is delivered to former smoke conveying duct L1 by the 7th pipeline L11.SRG gas vent A8 passes through SRG gas transmission pipeline L12 is delivered to acid making system.
Use embodiment 1
It is used for the processing of sintering flue gas using active carbon processing system described in embodiment 4, passes through the first temperature detection The monitoring of device P1, controls the water of filler 10 and discharge outlet 11, and temperature when former flue gas enters first order adsorption tower 101 is 110℃；By the monitoring of second temperature detection device P2, the flue gas of preliminary treatment enters the temperature when adsorption tower 102 of the second level It is 145 DEG C；The flue gas is handled using the system of the application, the dirt of discharge gas is detected at flue gas exhausting pipe line L13 (or chimney 8) Contaminate the removal effect of object are as follows: SO2Removal efficiency is 98.6%, denitrification rate 84%, and dust outlet concentration is 8.9mg/Nm3。
Use embodiment 2
Using active carbon processing system described in embodiment 5, it to be used for 600000Nm3/ h, the work that flue-gas temperature is 140 DEG C Under the conditions of condition, second level adsorption tower is introduced by 1% of thermal wind exhausting outside Analytic Tower bringing-up section, wherein the hot blast rate introduced is 6000Nm3/h(SO2Concentration is in 100ppm), the hot blast rate for introducing second level adsorption tower is only the 1/100 of raw flue gas amount, mixed Close SO in flue gas2Concentration is also extremely low, will not impact to denitration.
Calculate flue gas heating value after mixing:
1. secondary absorption tower inlet original obvious heat of smoke:
Q1=600000Nm3/h*140℃*0.32Kcal/Nm3DEG C=2.688*107kcal/h；
2. analytically introducing the hot wind sensible heat of secondary absorption tower in the bringing-up section discharge hot wind of tower:
Q2=6000Nm3/h*30℃*0.337Kcal/Nm3DEG C=0.606*106kcal/h；
3. flue gas and the introducing mixed temperature of hot wind:
T=(2.688*107+0.606*106)/(600000*0.32+6000*0.337)=141.67；
After thermal wind exhausting outside Analytic Tower is introduced second level adsorption tower, flue-gas temperature rising value are as follows:
T=141.67 DEG C -140 DEG C=1.67 DEG C of Δ.
Attached drawing 7 show influence of the flue-gas temperature to denitrification rate, from attached drawing 5 it is found that flue-gas temperature improve, denitrification rate by It gradually improves, especially in 140-160 DEG C of temperature range, as temperature improves, the denitrification rate rate of climb is faster.It can from above-mentioned calculating Know, the outer thermal wind exhausting of Analytic Tower bringing-up section is introduced into secondary absorption tower entrance, and flue-gas temperature improves 1-2 DEG C, and denitrification rate can mention It is high by 1%.In addition, can improve introduce two as far as possible under the premise of guaranteeing active carbon resolution factor to pursue higher denitration efficiency The hot blast rate of grade adsorption tower.
Use embodiment 3
A kind of active carbon parsing technique, the technique the following steps are included:
1) active carbon for having adsorbed pollutant enters active carbon Analytic Tower A from the entrance of active carbon Analytic Tower A, has adsorbed dirt The active carbon for contaminating object under the effect of gravity, moves from up to down, successively passes through preheating zone A1, the vapor of active carbon Analytic Tower A Resolver A2, First Transition section A5, pollutant resolver A3, the second changeover portion A6, cooling zone A4；
2) active carbon for having adsorbed pollutant is inhaled by preheating subsequently into vapor resolver A2 in the A1 of preheating zone Moisture in the attached active carbon of pollutant is decomposed and is detached from vapor resolver A2, then enters First Transition together Section A5, the moisture for decomposing and detaching out of active carbon that adsorbed pollutant are discharged from steam outlet A7；
3) active carbon for having adsorbed pollutant after having separated moisture enters pollutant resolver A3, has adsorbed pollutant Pollutant in active carbon is decomposed and is parsed in pollutant resolver A3, subsequently into the second changeover portion A6, decomposes reconciliation The pollutant of precipitation is discharged from SRG gas vent A8, and the active carbon after having parsed is discharged from the outlet of active carbon Analytic Tower A.
Use embodiment 4
Embodiment 3 is reused, only cooling wind enters cooling zone A4 from cooling zone gas access A401, after heat exchange, from Cooling zone gas vent A402 is delivered to preheating zone A1 by the second conveyance conduit L4；Hot wind is parsed from pollutant resolver gas Entrance A301 enters pollutant resolver A3, passes through the first conveyance conduit L3 from pollutant resolver gas vent A302 after heat exchange It is delivered to vapor resolver；Gas in the A2 of vapor resolver after heat exchange is from vapor resolver gas vent A202 Cooling zone A4 is delivered to by third conveyance conduit L5.
Parsing activation (or regeneration) processing, processing are carried out to the active carbon containing pollutant using system described in embodiment 6 600m2The flue gas that sintering machine generates is by activated carbon adsorber treated the active carbon containing pollutant, analytically tower SRG gas In the SRG gas of exit discharge, moisture content 100-200m3(moisture content is about 600-750m to/h in the prior art3/ H), account for the 5-10% of SRG gas volume (it is about 25-40% that moisture content, which accounts for SRG gas volume, in the prior art).The SRG gas Body is the 30-60% for generating wastewater flow rate in the prior art by entering towerman's sequence, the wastewater flow rate that relieving haperacidity process generates after cooling.
Heat Calculation, it is assumed that SRG gas flow is Q (wet basis state), and in the prior art, vapor percentage composition is 30%, Vapor specific heat capacity Cp is 33.94J (mol/K), and vapor decomposition temperature is 150 DEG C, and Analytic Tower bringing-up section target temperature is 430 DEG C, moisture discharge amount is the 60% of total amount.The hot wind efficiency of furnace is 80%.
It is handled using the parsing tower structure of the application, is first detached from vapor in the vapor resolver of Analytic Tower, It is discharged from steam outlet, to reduce the moisture content in SRG gas.Meanwhile dirt will have been adsorbed in vapor bringing-up section The moisture contaminated in the active carbon of object detaches, and in the heating process of pollutant resolver, just reduces the demand of heat, separates Vapor out not be heated to 430 DEG C；That is, in advance separating moisture, reduce the supply of heat, saves The energy.
Heat=Q*30%/the 18*60%*Cp* (430-130) for the vapor reduction discharged in advance；
With 600m2For sintering machine, Q=4000m3/ h, by calculate it is found that using the application Analytic Tower, active carbon solution It reduces heat and is supplied as 40733kJ/h in analysis tower pollutant resolver.
Known blast furnace gas calorific value is 3500kJ/Nm3。
Give active carbon Analytic Tower pollutant resolver heat supply by hot-blast stove, then after the parsing tower apparatus for using the application, It is=40733/3500/80%=14.5Nm that blast furnace coal tolerance, which can be reduced,3/h.The use of fuel is greatly reduced, energy is saved While source, reduce the discharge of pollutant.

Claims (18)

1. a kind of active carbon processing system for improving utilization rate of waste heat and denitrification rate, which includes that active carbon is inhaled Attached tower (1), active carbon Analytic Tower (2)；It is characterized by: the activated carbon adsorber (1) is two-stage adsorption tower, including the first order Adsorption tower (101) and second level adsorption tower (102)；The active carbon processing system further includes former smoke conveying duct (L1), first Flue gas heat-exchange unit (3), the second flue gas heat-exchange unit (4), preliminary treatment smoke conveying duct (L2), the first active carbon conveying device (D1), the second active carbon conveying device (D2), third active carbon conveying device (D3)；Wherein: former smoke conveying duct (L1) is even It is connected to the smoke inlet of first order adsorption tower (101)；The exhanst gas outlet of first order adsorption tower (101) is defeated by preliminary treatment flue gas The smoke inlet for sending pipeline (L2) to be connected to second level adsorption tower (102)；First flue gas heat-exchange unit (3) setting is conveyed in former flue gas On pipeline (L1)；Second flue gas heat-exchange unit (4) is arranged on preliminary treatment smoke conveying duct (L2)；First active carbon conveying dress Set the active carbon entrance of the active carbon outlet and second level adsorption tower (102) of (D1) connection active carbon Analytic Tower (2)；Second activity The active carbon outlet of charcoal conveying device (D2) connection second level adsorption tower (102) and the active carbon of first order adsorption tower (101) enter Mouthful；Third active carbon conveying device (D3) connects the active carbon outlet and active carbon Analytic Tower (2) of first order adsorption tower (101) Active carbon entrance.
2. active carbon processing system according to claim 1, it is characterised in that: active carbon Analytic Tower (2) is set from top to bottom There are bringing-up section (5) and cooling section (6)；The lower part of bringing-up section (5) is equipped with bringing-up section gas access (501), the top of bringing-up section (5) Equipped with bringing-up section gas vent (502)；The device further includes hot-blast stove (7)；Hot-blast stove (7) be equipped with hot-wind inlet (701) and Hot-blast outlet (702)；The first pipe (L3) drawn from the hot-blast outlet (702) of hot-blast stove (7) is connected to active carbon Analytic Tower (2) bringing-up section gas access (501), the second pipe (L4) drawn from bringing-up section gas vent (502) are connected to hot-blast stove (7) hot-wind inlet (701)；A branch i.e. third pipeline (L5), third pipeline (L5) connection are separated from second pipe (L4) To preliminary treatment smoke conveying duct (L2) or the smoke inlet of second level adsorption tower (102).
3. active carbon processing system according to claim 1, it is characterised in that: institute's active carbon Analytic Tower (2) includes from upper And the preheating zone (A1) of lower setting, vapor resolver (A2), pollutant resolver (A3), cooling zone (A4), First Transition section (A5) and the second changeover portion (A6)；Wherein: the lower part of preheating zone (A1) is equipped with preheating zone gas access (A101) and preheating zone gas Body exports (A102)；The lower part of vapor resolver (A2) is equipped with vapor resolver gas access (A201) and vapor decomposes Area's gas vent (A202)；The lower part of pollutant resolver (A3) is equipped with pollutant resolver gas access (A301) and pollutant Resolver gas vent (A302)；The lower part of cooling zone (A4) is equipped with cooling zone gas access (A401) and cooling zone gas vent (A402)；It is between vapor resolver (A2) and pollutant resolver (A3) First Transition section (A5)；Pollutant resolver (A3) it is between cooling zone (A4) the second changeover portion (A6)；The side wall of First Transition section (A5) is equipped with steam outlet (A7)；The side wall of second changeover portion (A6) is equipped with SRG gas vent (A8).
4. active carbon processing system according to claim 3, it is characterised in that: the device further includes hot-blast stove (7)；Hot wind Furnace (7) is equipped with hot-wind inlet (701) and hot-blast outlet (702)；Cooling zone gas access (A401) and cooling gas delivery pipe Road (L6) connection；The first pipe (L3) drawn from the hot-blast outlet (702) of hot-blast stove (7) is connected to pollutant resolver gas Entrance (A301)；Pollutant resolver gas vent (A302) is connected to vapor resolver gas by the 4th pipeline (L7) and enters Mouth (A201)；Vapor resolver gas vent (A202) is connected to the hot-wind inlet of hot-blast stove (7) by second pipe (L4) (701)。
5. flue gas purification device according to claim 4, it is characterised in that: separate a branch i.e. from second pipe (L4) Third pipeline (L5), third pipeline (L5) are connected to preliminary treatment smoke conveying duct (L2) or second level adsorption tower (102) Smoke inlet；And/or
Cooling zone gas vent (A402) is connected to preheating zone gas access (A101) by the 5th pipeline (L8).
6. flue gas purification device according to claim 5, it is characterised in that: the active carbon Analytic Tower (2) further includes to work Property charcoal Analytic Tower (2) top is passed through the nitrogen gas delivery-line (L9) of nitrogen, and nitrogen gas delivery-line (L9) is connected to Analytic Tower (2), And the link position of nitrogen gas delivery-line (L9) and active carbon Analytic Tower (2) is located at the top of preheating zone (A1).
7. flue gas purification device according to claim 6, it is characterised in that: nitrogen gas delivery-line (L9) is changed equipped with nitrogen Hot device (A9), preheating zone gas vent (A102) are connected to the heat medium of nitrogen heat exchanger (A9) by the 6th pipeline (L10) The entrance in channel；And/or
Steam outlet (A7) is delivered to former smoke conveying duct (L1) by the 7th pipeline (L11)；SRG gas vent (A8) is logical It crosses SRG gas transmission pipeline (L12) and is delivered to acid making system.
8. flue gas purification device according to claim 7, it is characterised in that: cooling gas conveyance conduit (L6) is equipped with cold But wind blower (A10)；First pipe (L3) is equipped with air-heater (A11)；Wind-supplying mouth (703) are additionally provided on hot-blast stove (7)； And/or
The device further includes chimney (8)；The exhanst gas outlet of second level adsorption tower (102) is connected to cigarette via the 8th pipeline (L13) Chimney (8).
9. flue gas purification device according to claim 1 to 8, it is characterised in that: the first flue gas heat-exchange unit (3) Gas vent the gas accesses of the second flue gas heat-exchange unit (4) is connected to by First Heat Exchanger medium delivery pipe road (L14), the The gas vent of two flue gas heat-exchange units (4) is connected to the first flue gas heat-exchange unit by the second heat exchanger media conveyance conduit (L15) (3) gas access.
10. active carbon processing system according to claim 9, it is characterised in that: First Heat Exchanger medium delivery pipe road (L14) and/or the second heat exchanger media conveyance conduit (L15) is equipped with blower (9)；And/or
First Heat Exchanger medium delivery pipe road (L14) is equipped with discharge outlet (10)；On second heat exchanger media conveyance conduit (L15) Equipped with filler (11).
11. active carbon processing system according to claim 1 to 10, it is characterised in that: former smoke conveying duct (L1) it is equipped with the first temperature-detecting device (P1), and the first temperature-detecting device (P1) is arranged in the first flue gas heat-exchange unit (3) downstream；Preliminary treatment smoke conveying duct (L2) is equipped with second temperature detection device (P2), and second temperature detects Device (P2) is arranged in the downstream of the second flue gas heat-exchange unit (4)；And/or
First order adsorption tower (101) is desulfurizing tower, and second level adsorption tower (102) is denitrating tower.
12. a kind of active carbon processing method for improving utilization rate of waste heat and denitrification rate uses any one of claim 1-11 institute A kind of method for stating active carbon processing system for improving utilization rate of waste heat and denitrification rate, method includes the following steps:
1) fresh active carbon is obtained by active carbon Analytic Tower (2) parsing to be delivered to by the first active carbon conveying device (D1) The active carbon entrance of second level adsorption tower (102)；Active carbon from top to bottom, is inhaled in second level adsorption tower (102) from the second level Attached tower (102) active carbon outlet discharge, then the active carbon by second level adsorption tower (102) discharge is conveyed by the second active carbon Device (D2) is delivered to first order adsorption tower (101)；Active carbon is interior from top to bottom in first order adsorption tower (101), from the first order The active carbon of adsorption tower (101) exports discharge, then the active carbon being discharged from first order adsorption tower (101) is passed through third active carbon Conveying device (D3) is delivered to active carbon Analytic Tower (2) and carries out parsing regeneration；
2) former flue gas is delivered to first order adsorption tower (101) by former smoke conveying duct (L1), and former flue gas is adsorbed in the first order Desulfurization process is carried out in tower (101), treated that flue gas passes through preliminary treatment flue gas delivery pipe by first order adsorption tower (101) Road (L2) is delivered to second level adsorption tower (102), and preliminary treatment flue gas carries out out of stock processing in second level adsorption tower (102), It is discharged by first order adsorption tower (101) and second level adsorption tower (102) treated flue gas from chimney (8)；
Wherein: in the first flue gas heat-exchange unit (3) on former smoke conveying duct (L1), former flue gas and the first flue gas heat-exchange unit (3) medium in exchanges heat, and former flue gas discharges heat in the first flue gas heat-exchange unit (3), and medium is in the first flue gas heat-exchange unit (3) heat is absorbed in, the former flue gas after release heat cooling enters first order adsorption tower (101)；Medium after absorbing heat is logical It crosses First Heat Exchanger medium delivery pipe road (L14) and is delivered to the second flue gas heat-exchange unit (4)；
In the second flue gas heat-exchange unit (4) of preliminary treatment smoke conveying duct (L2), handled by first order adsorption tower (101) Preliminary treatment flue gas afterwards exchanges heat with the medium in the second flue gas heat-exchange unit (4), absorbs at the first flue gas heat-exchange unit (3) The medium of heat discharges heat in the second flue gas heat-exchange unit (4), and preliminary treatment flue gas is in the second flue gas heat-exchange unit (4) interior suction Heat is received, the preliminary treatment flue gas after absorbing heat heating enters second level adsorption tower (102)；Medium after release heat passes through Second heat exchanger media conveyance conduit (L15) is recycled to the first flue gas heat-exchange unit (3).
13. according to the method for claim 12, it is characterised in that: this method further include:
3) hot-blast stove (7) heats hot wind, and hot wind passes through first pipe (L3) from the bringing-up section gas access of active carbon Analytic Tower (2) (501) entering the bringing-up section (5) of active carbon Analytic Tower (2), hot wind exchanges heat in active carbon Analytic Tower (2) with active carbon, Active carbon in heating of Activated charcoal Analytic Tower (2), then by second pipe (L4) after bringing-up section gas vent (502) discharge Continue heat cycles in into hot-blast stove (7)；A branch is separated on second pipe (L4), is third pipeline (L5), from heating The a part for the hot wind after heat exchange that section gas vent (502) is discharged is delivered to preliminary treatment cigarette by third pipeline (L5) The smoke inlet in letter shoot road (L2) or second level adsorption tower (102).
14. according to the method for claim 12, it is characterised in that: the active carbon Analytic Tower (2) includes setting from top to bottom The preheating zone (A1) set, vapor resolver (A2), pollutant resolver (A3), cooling zone (A4), First Transition section (A5) and Second changeover portion (A6)；Wherein: the lower part of preheating zone (A1) is equipped with preheating zone gas access (A101) and preheating zone gas vent (A102)；The lower part of vapor resolver (A2) is equipped with vapor resolver gas access (A201) and vapor resolver gas It exports (A202)；The lower part of pollutant resolver (A3) is equipped with pollutant resolver gas access (A301) and pollutant resolver Gas vent (A302)；The lower part of cooling zone (A4) is equipped with cooling zone gas access (A401) and cooling zone gas vent (A402)；It is between vapor resolver (A2) and pollutant resolver (A3) First Transition section (A5)；Pollutant resolver (A3) it is between cooling zone (A4) the second changeover portion (A6)；The side wall of First Transition section (A5) is equipped with steam outlet (A7)；The side wall of second changeover portion (A6) is equipped with SRG gas vent (A8)；
This method further include: the 4) active carbon of first order adsorption tower (101) discharge is in active carbon Analytic Tower (2) successively by pre- Hot-zone (A1), vapor resolver (A2), First Transition section (A5), pollutant resolver (A3), the second changeover portion (A6) and cold But area (A4)；Active carbon containing pollutant is first preheated at preheating zone (A1), so after entering active carbon Analytic Tower (2) The removing of moisture is carried out at vapor resolver (A2) afterwards, the moisture being removed from active carbon is from First Transition section (A5) side wall On steam outlet (A7) be expelled directly out；Then, go the active carbon containing pollutant of moisture removal again at pollutant resolver (A3) Decompose and the removing of pollutant, pollutant are discharged from the SRG gas vent (A8) on the second changeover portion (A6) side wall；Then Active carbon is cooled down by cooling zone (A4), obtains fresh active carbon.
15. according to the method for claim 14, it is characterised in that: this method further include:
5) cooling gas enters active carbon Analytic Tower from cooling zone gas access (A401) by cooling gas conveyance conduit (L6) (2) cooling zone (A4), the gas being discharged from cooling zone gas vent (A402) are delivered to preheating zone by the 5th pipeline (L8) (A1)；
Hot-blast stove (7) heats hot wind, and hot wind passes through the pollutant resolver gas of first pipe (L3) from active carbon Analytic Tower (2) Entrance (A301) enters the pollutant resolver (A3) of active carbon Analytic Tower (2), and hot wind is in pollutant resolver (A3) and living Property charcoal exchanges heat, the active carbon in heating of Activated charcoal Analytic Tower (2), the pollutant of removal activity charcoal；Then from pollutant point Water is delivered to from vapor resolver gas access (A201) by the 4th pipeline (L7) after solution area's gas vent (A302) discharge Steam resolver (A2), which continues to exchange heat with active carbon in vapor resolver (A2), in removal activity charcoal Moisture；Then it is discharged from vapor resolver gas vent (A202), is entered by second pipe (L4) from the hot wind of hot-blast stove (7) Mouth (701), which enters, continues heat cycles in hot-blast stove (7)；
A branch is separated on second pipe (L4), is third pipeline (L5), is arranged from vapor resolver gas vent (A202) Out by heat exchange after hot wind a part by third pipeline (L5) be delivered to preliminary treatment smoke conveying duct (L2) or The smoke inlet of second level adsorption tower (102).
16. according to the method for claim 15, it is characterised in that: the gas of preheating zone gas vent (A102) discharge passes through 6th pipeline (L10) is delivered to the entrance of the heating medium passage of nitrogen heat exchanger (A9), heated nitrogen；And/or
The gas being discharged from steam outlet (A7) is delivered to former smoke conveying duct (L1) by the 7th pipeline (L11)；From SRG The SRG gas of gas vent (A8) discharge is delivered to acid making system by SRG gas transmission pipeline (L12).
17. according to claim 13, method described in any one of 15-16, it is characterised in that: from bringing-up section gas vent (502) or vapor resolver gas vent (A202) discharge by heat exchange after hot wind；Wherein volume fraction is 0.5- The hot wind of 30% (preferably 1-20%, more preferably 2-15%) is delivered to the conveying of preliminary treatment flue gas by third pipeline (L5) The smoke inlet of pipeline (L2) or second level adsorption tower (102).
18. method described in any one of 2-17 according to claim 1, it is characterised in that: the first temperature-detecting device (P1) inspection The temperature for surveying former flue gas in former smoke conveying duct (L1) pipeline after heat exchange, 1. and/or 2. by following step, so that into the Flue-gas temperature in primary adsorption tower (101) is 100-120 DEG C；
1. adjusting the amount for the water being added from discharge outlet (10) on First Heat Exchanger medium delivery pipe road (L3)；
2. adjusting the amount from discharge water in filler (11) on the second heat exchanger media conveyance conduit (L4)；
And/or
Second temperature detection device (P2) detects the temperature of flue gas after the second flue gas heat-exchange unit (4) interior preliminary treatment, by following Step 1. and/or 2. and/or 3. so that into the flue-gas temperature in second level adsorption tower (102) be 140-155 DEG C；
1. adjusting the amount for the water being added from discharge outlet (10) on First Heat Exchanger medium delivery pipe road (L3)；
2. adjusting the amount from discharge water in filler (11) on the second heat exchanger media conveyance conduit (L4)；
3. adjust be discharged from bringing-up section gas vent (402) or vapor resolver gas vent (A202) after heat exchange Hot wind is delivered to the flue gas of preliminary treatment smoke conveying duct (L2) or second level adsorption tower (102) by third pipeline (L5) The amount of the hot wind of entrance.
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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109794137A (en) * 2019-01-15 2019-05-24 北京科技大学 A kind of method and system of adsorption cleaning and enriching and recovering flue gas nitrogen oxide
CN109794135A (en) * 2019-01-15 2019-05-24 北京科技大学 Flue gas multiple pollutant adsorbing and removing and method of resource based on UTILIZATION OF VESIDUAL HEAT IN
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CN110787612A (en) * 2019-10-25 2020-02-14 光大生物热电(六安)有限公司 Biomass power generation recycling device and method
CN112146453A (en) * 2019-06-27 2020-12-29 湖南中冶长天节能环保技术有限公司 Combined flue gas purification process
CN112403179A (en) * 2019-11-05 2021-02-26 中冶长天国际工程有限责任公司 Shunting type flue gas desulfurization and denitrification treatment system and method
CN112403180A (en) * 2019-11-05 2021-02-26 中冶长天国际工程有限责任公司 Centralized heating flue gas desulfurization and denitrification treatment system and method
CN113120871A (en) * 2020-01-16 2021-07-16 吉林紫金铜业有限公司 Method for heating desulfurization nitrogen in acid preparation by smelting flue gas
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CN114712982A (en) * 2021-01-05 2022-07-08 中冶长天国际工程有限责任公司 Method and system for judging temperature rise of activated carbon in desulfurization process
CN116351207A (en) * 2023-06-01 2023-06-30 中国华能集团清洁能源技术研究院有限公司 Low-temperature flue gas adsorption tower with flue gas cooling function and adsorption method

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100025303A1 (en) * 2006-12-19 2010-02-04 Instituto Mexicano Del Petroleo Application of microporous carbon adsorbent for reducing the benzene content in hydrocarbon streams
CN105688622A (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 adopting two adsorption columns in series connection and a device therefor
CN205461790U (en) * 2016-02-17 2016-08-17 中国科学院过程工程研究所 A SOx/NOx control device for coke oven gas cleaning
CN206103709U (en) * 2016-08-30 2017-04-19 重庆泰克环保科技股份有限公司 Glass high -temperature furnace flue gas energy saving and emission reduction clean system
CN107537591A (en) * 2017-10-20 2018-01-05 国电科学技术研究院 Three-stage carbon base catalyst regenerates Tower System

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100025303A1 (en) * 2006-12-19 2010-02-04 Instituto Mexicano Del Petroleo Application of microporous carbon adsorbent for reducing the benzene content in hydrocarbon streams
CN105688622A (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 adopting two adsorption columns in series connection and a device therefor
CN205461790U (en) * 2016-02-17 2016-08-17 中国科学院过程工程研究所 A SOx/NOx control device for coke oven gas cleaning
CN206103709U (en) * 2016-08-30 2017-04-19 重庆泰克环保科技股份有限公司 Glass high -temperature furnace flue gas energy saving and emission reduction clean system
CN107537591A (en) * 2017-10-20 2018-01-05 国电科学技术研究院 Three-stage carbon base catalyst regenerates Tower System

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109794135A (en) * 2019-01-15 2019-05-24 北京科技大学 Flue gas multiple pollutant adsorbing and removing and method of resource based on UTILIZATION OF VESIDUAL HEAT IN
CN109794137B (en) * 2019-01-15 2021-04-16 北京科技大学 Method and system for adsorbing, purifying, enriching and recovering nitrogen oxides in flue gas
CN109794137A (en) * 2019-01-15 2019-05-24 北京科技大学 A kind of method and system of adsorption cleaning and enriching and recovering flue gas nitrogen oxide
CN109925843A (en) * 2019-04-12 2019-06-25 清华大学 A kind of method of the adsorptive gaseous component of gas-solid multi-stage countercurrent
CN112146453A (en) * 2019-06-27 2020-12-29 湖南中冶长天节能环保技术有限公司 Combined flue gas purification process
CN112146453B (en) * 2019-06-27 2022-08-16 湖南中冶长天节能环保技术有限公司 Combined flue gas purification process
CN110787612A (en) * 2019-10-25 2020-02-14 光大生物热电(六安)有限公司 Biomass power generation recycling device and method
CN112403180B (en) * 2019-11-05 2022-06-03 中冶长天国际工程有限责任公司 Centralized heating flue gas desulfurization and denitrification treatment system and method
CN112403179A (en) * 2019-11-05 2021-02-26 中冶长天国际工程有限责任公司 Shunting type flue gas desulfurization and denitrification treatment system and method
CN112403180A (en) * 2019-11-05 2021-02-26 中冶长天国际工程有限责任公司 Centralized heating flue gas desulfurization and denitrification treatment system and method
CN112403179B (en) * 2019-11-05 2022-05-03 中冶长天国际工程有限责任公司 Shunting type flue gas desulfurization and denitrification treatment system and method
CN113120871A (en) * 2020-01-16 2021-07-16 吉林紫金铜业有限公司 Method for heating desulfurization nitrogen in acid preparation by smelting flue gas
CN113946173A (en) * 2020-07-15 2022-01-18 中冶长天国际工程有限责任公司 Temperature control system, method and device for analytical tower
CN113946173B (en) * 2020-07-15 2022-12-06 中冶长天国际工程有限责任公司 Temperature control system, method and device for analytical tower
CN114712982A (en) * 2021-01-05 2022-07-08 中冶长天国际工程有限责任公司 Method and system for judging temperature rise of activated carbon in desulfurization process
CN114712982B (en) * 2021-01-05 2023-09-01 中冶长天国际工程有限责任公司 Method and system for judging temperature rise of active carbon in desulfurization process
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