CN108939808B - Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof - Google Patents

Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof Download PDF

Info

Publication number
CN108939808B
CN108939808B CN201810762472.9A CN201810762472A CN108939808B CN 108939808 B CN108939808 B CN 108939808B CN 201810762472 A CN201810762472 A CN 201810762472A CN 108939808 B CN108939808 B CN 108939808B
Authority
CN
China
Prior art keywords
flue gas
activated carbon
gas
adsorption tower
heat exchanger
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201810762472.9A
Other languages
Chinese (zh)
Other versions
CN108939808A (en
Inventor
李俊杰
魏进超
康建刚
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Zhongye Changtian International Engineering Co Ltd
Original Assignee
Zhongye Changtian International Engineering Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Zhongye Changtian International Engineering Co Ltd filed Critical Zhongye Changtian International Engineering Co Ltd
Priority to CN201810762472.9A priority Critical patent/CN108939808B/en
Publication of CN108939808A publication Critical patent/CN108939808A/en
Application granted granted Critical
Publication of CN108939808B publication Critical patent/CN108939808B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • 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

Abstract

The invention provides an activated carbon treatment system for improving the waste heat utilization rate and the denitration rate, wherein heat exchangers are respectively arranged before flue gas is input into a first-stage adsorption tower and a second-stage adsorption tower, so that the temperature of the flue gas entering the first-stage adsorption tower and the second-stage adsorption tower is controlled, and the temperature of desulfurization and denitration is ensured. The invention utilizes the high-temperature flue gas (about 150-2And NOx removal efficiency. The high-temperature flue gas utilization efficiency behind the main exhaust fan is improved, and the flue gas temperature entering the desulfurization tower and the denitration tower is controlled, so that the desulfurization and denitration efficiency is improved.

Description

Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof
Technical Field
The invention relates to an activated carbon treatment system, in particular to a flue gas treatment desulfurization and denitrification system capable of improving the waste heat utilization rate and the denitrification rate, and belongs to the field of flue gas purification.
Background
The discharge temperature of the sintering flue gas after passing through the main exhaust fan is between 110 ℃ and 170 ℃, and SO is contained in the sintering flue gas2、NOxDust, dioxin, heavy metal and other pollutants, and the activated carbon flue gas purification technology is just suitable for a sintering flue gas temperature emission interval, can realize the synergistic efficient purification of the multiple pollutants, can simultaneously remove the multiple pollutants on one set of equipment, and realizes the byproduct SO2The technology has the advantages of high pollutant removal efficiency, no water resource consumption basically, no secondary pollution and the like. The activated carbon flue gas purification device is provided with a plurality of subsystems such as an adsorption system, an analytic system and an acid making system, the flue gas is purified after passing through the activated carbon adsorption unit, and activated carbon particles circularly flow between the adsorption unit and the analytic unit to realize' adsorption of pollutants->Thermal desorption activation (to make pollutants escape)>Cooling->And (4) recycling adsorbed pollutants.
The active carbon adsorption is currently divided into two modes of single-stage adsorption and two-stage adsorption, wherein the single-stage adsorption is to simultaneously adsorb multiple pollutants in one adsorption tower, ammonia gas is added at the inlet of the adsorption tower, and the method can achieve SO2Efficiency of removal>98％，The denitration rate is about 50 percent, and the outlet concentration of dust is less than 20mg/Nm3. Along with the improvement of the environmental protection requirement, part of steel plants adopt double-stage adsorption, wherein a first-stage tower carries out desulfurization, dust removal and the like, and a second-stage tower carries out denitration, and the treatment effect of the method is as follows: SO (SO)2Efficiency of removal>98 percent, the denitration rate is more than 80 percent, and the dust outlet concentration is less than 10mg/Nm3。
As is well known, the flue gas desulfurization and denitration process by an activated carbon method has important influence on the pollutant removal effect, the low temperature is favorable for desulfurization reaction, and the high temperature is favorable for denitration reaction, so that in order to improve the multi-pollutant removal efficiency, the flue gas temperature at the inlet of a first-stage tower and the flue gas temperature at the inlet of a second-stage tower can be preferably controlled respectively in a second-stage treatment process, wherein the first-stage low temperature (120 ℃ and t >100 ℃) and the second-stage high temperature (155 ℃ and t >140 ℃) are met.
The process flow in the prior art is as follows: the flue gas temperature after passing through the main exhaust fan is too high (110-3Is added at the inlet of the denitration tower. The active carbon is delivered to the second-stage tower after being analyzed in the analyzing tower, the active carbon after denitration in the second-stage tower is delivered to the first-stage tower through the conveying system, the active carbon in the first-stage tower after adsorption, desulfurization and dust removal is delivered to the analyzing tower through the conveying system, and one-time complete material circulation is completed.
In the prior art, a process of adding cold air or cold water into original flue gas is adopted, so that the original flue gas is cooled and then is input into a desulfurization tower, the heat of high-temperature flue gas behind a main exhaust fan cannot be fully utilized, and in order to ensure the temperature of the flue gas entering the desulfurization tower, cold air needs to be additionally added, and the loss of the high-temperature flue gas is caused. However, low temperatures aid desulfurization, high temperatures aid denitrification; after cold air is added, the temperature requirement of the desulfurization tower is met, but after desulfurization, the flue gas temperature is low, and after entering the next denitration tower, the denitration effect is poor. The direct adoption of cooling air is difficult to aim at SO2、NOxThe adsorption property of the catalyst can not effectively improve the desulfurization and denitrification efficiency,cause heat and denitration reaction product NH3Is wasted.
In addition, the activated carbon analysis system indirectly heats the activated carbon in the analysis tower by burning fuels such as blast furnace gas, coke oven gas and the like through a hot blast stove, so that the activated carbon is analyzed and regenerated in the analysis tower; therefore, the high-temperature gas after combustion in the hot blast furnace contains about 100ppm of SO2Gas at a temperature of about 300 ℃. At present, most of the burnt high-temperature gas is used for hot air circulation and is used for reducing the application of blast furnace gas, coke oven gas or other fuels, meanwhile, in order to keep the pressure and the oxygen content in a hot air circulation system stable, a part of the high-temperature gas needs to be discharged into a flue all the time, the discharged gas amount of the part is about 10 percent of the circulation amount, and the temperature is about 300 ℃.
In the prior art, the discharged gas is directly discharged, and trace SO exists in the discharged heating gas2The heat is discharged outside, which affects the environment, and the discharged heat can not be fully utilized, which causes heat waste. Therefore, the heat of the part of the discharged air quantity discharged to the flue is not fully utilized, and energy waste is caused. Furthermore, the portion of the discharged gas contains SO2The gas is directly discharged to the outside to cause pollution to the surrounding environment.
The activated carbon having adsorbed the contaminants is desorbed by an desorption column. The desorption system aims at carrying out high-temperature desorption regeneration on the active carbon adsorbed with pollutants, and the production gas contains high-concentration SO2And a large amount of water and other various pollutants (SRG), and sending the SRG gas to an acid making system for making acid.
SO in the sintering flue gas due to the adsorption property of the activated carbon2And other harmful impurities are almost entirely enriched in the SRG gas. Therefore, almost undetectable harmful components in the sintering clean flue gas reach very high concentration in the SRG flue gas, and the SRG flue gas has the following characteristics: (1) small flow, high temperature, average temperature of flue gas about 400 deg.C, 600m2SRG flue gas flow (dry basis) of sintering machine is 2000m3About/h; (2) flue gas SO2High concentration of SO in SRG flue gas2The mass fraction can reach 25 percent (dry basis); (3) the water content in the smoke is high, and the highest water content can reach33%; (4) the CO content of the flue gas is high, and the mass fraction is about 0.5%; (5) the content of harmful components such as ammonia, fluorine, chlorine, mercury and the like in the smoke is high, and the average mass fraction is respectively 3.1%/0.1%/1.6%/51 mg/Nm3(ii) a (6) The smoke dust content is high, and the average dust content is 2g/m3Left and right; the main component of the smoke dust is active carbon which accounts for 65-85% of the total dust. It can be known that SRG gas has a large water content, a high temperature, and a high temperature and high corrosion property, so the acid making process is made of glass fiber reinforced plastic, which has a high requirement on temperature, and generally requires to operate at a temperature of 100 ℃, but SRG gas has a high water content, which causes the following adverse effects: (1) in order to treat pollutants in the SRG, a large amount of water is consumed, so that resource waste is caused; (2) because the specific heat capacity of water is large, in order to treat SRG gas in an acid making system made of glass fiber reinforced plastic materials, water must be added into the SRG gas to achieve the purpose of reducing the temperature, and because the moisture content is heavy, the temperature is relatively high after the temperature is reduced, so that the service life of the glass fiber reinforced plastic materials is influenced; (3) a large amount of process wastewater is produced.
Disclosure of Invention
Aiming at the problems of low heat utilization efficiency, poor denitration effect and the like when flue gas is treated by an activated carbon treatment system in the prior art, the invention provides the activated carbon treatment system for improving the waste heat utilization rate and the denitration rate.
The invention utilizes the high-temperature flue gas (about 150-2An apparatus and method for NOx removal efficiency. The method for improving the utilization efficiency of the high-temperature flue gas behind the main exhaust fan, controlling the temperature of the flue gas entering the desulfurization tower and the denitration tower and improving the desulfurization and denitration efficiency is realized.
A second object of the present invention is to: prevention of SO contained in heated air circulation gas for analysis2Direct discharge, in order to solve the problem, the inventionObviously provides a method capable of removing discharged SO2Flue gas purification device of concentration. The device introduces a part of externally-discharged hot air after heat exchange with the activated carbon to be analyzed into a flue gas inlet of a secondary adsorption tower, and on one hand, externally-discharged SO is removed2The concentration, the flue gas of heating second grade adsorption tower entrance simultaneously, the flue gas temperature obtains improving. Generally speaking, SO of flue gas at inlet of secondary adsorption tower2The lower the concentration, the higher the denitration rate, and the temperature is correspondingly increased. Therefore, the device removes the discharged SO2While the concentration, the denitration efficiency and the waste heat utilization rate are also improved.
A third object of the present invention is to: aiming at the problem that the moisture content in SRG gas is heavy and is not beneficial to subsequent treatment of the hyaluronic acid in the prior art, the invention develops a novel desorption tower structure, separates the moisture in the activated carbon in advance by a step-by-step heating method according to different decomposition temperatures of pollutants adsorbed by the activated carbon, reduces the moisture content in the SRG gas and creates good conditions for normal operation of downstream acid making and wastewater treatment processes.
According to the first embodiment provided by the invention, the activated carbon treatment system for improving the waste heat utilization rate and the denitration rate is provided.
The utility model provides an improve activated carbon processing system of waste heat utilization ratio and denitration rate, this activated carbon processing system includes activated carbon adsorption tower, active carbon analytic tower. The active carbon adsorption tower is a two-stage adsorption tower and comprises a first-stage adsorption tower and a second-stage adsorption tower. The active carbon treatment system also comprises a raw flue gas conveying pipeline, a first flue gas heat exchanger, a second flue gas heat exchanger, a primary treatment flue gas conveying pipeline, a first active carbon conveying device, a second active carbon conveying device and a third active carbon conveying device.
Wherein: the raw flue gas conveying pipeline is connected to a flue gas inlet of the first-stage adsorption tower. The flue gas outlet of the first-stage adsorption tower is connected to the flue gas inlet of the second-stage adsorption tower through a primary treatment flue gas conveying pipeline. The first flue gas heat exchanger is arranged on the original flue gas conveying pipeline. The second flue gas heat exchanger is arranged on the primary treatment flue gas conveying pipeline. The first active carbon conveying device is connected with an active carbon outlet of the active carbon desorption tower and an active carbon inlet of the second-stage adsorption tower. The second active carbon conveying device is connected with an active carbon outlet of the second-stage adsorption tower and an active carbon inlet of the first-stage adsorption tower. The third active carbon conveying device is connected with an active carbon outlet of the first-stage adsorption tower and an active carbon inlet of the active carbon desorption tower.
Preferably, the activated carbon desorption tower is provided with a heating section and a cooling section from top to bottom. The lower part of the heating section is provided with a heating section gas inlet, and the upper part of the heating section is provided with a heating section gas outlet. The device also comprises a hot blast stove. The hot blast stove is provided with a hot blast inlet and a hot blast outlet. A first pipeline led out from a hot air outlet of the hot blast stove is connected to a heating section gas inlet of the activated carbon desorption tower. A second duct leading from the gas outlet of the heating section is connected to the hot air inlet of the stove. And a branch, namely a third pipeline, is separated from the second pipeline, and the third pipeline is connected to a primary treatment flue gas conveying pipeline or a flue gas inlet of a second-stage adsorption tower.
Preferably, the activated carbon desorption tower comprises a preheating zone, a steam decomposition zone, a pollutant decomposition zone, a cooling zone, a first transition section and a second transition section which are arranged from top to bottom.
Wherein: the lower part of the preheating zone is provided with a preheating zone gas inlet and a preheating zone gas outlet. The lower part of the water vapor decomposition area is provided with a gas inlet of the water vapor decomposition area and a gas outlet of the water vapor decomposition area. The lower part of the pollutant decomposition area is provided with a pollutant decomposition area gas inlet and a pollutant decomposition area gas outlet. The lower part of the cooling area is provided with a cooling area gas inlet and a cooling area gas outlet. A first transition section is arranged between the water vapor decomposition area and the pollutant decomposition area. A second transition section is arranged between the pollutant decomposition area and the cooling area. The side wall of the first transition section is provided with a steam outlet. And the side wall of the second transition section is provided with an SRG gas outlet.
Preferably, the device further comprises a hot blast stove. The hot blast stove is provided with a hot blast inlet and a hot blast outlet. The cooling zone gas inlet is connected with a cooling gas delivery pipeline. A first pipeline led out from a hot air outlet of the hot blast stove is connected to a gas inlet of the pollutant decomposition area. The pollutant decomposition zone gas outlet is connected to the water vapor decomposition zone gas inlet through a fourth conduit. The gas outlet of the water vapor decomposition area is connected to the hot air inlet of the hot air furnace through a second pipeline.
Preferably, a branch, i.e. a third duct, branches off from the second duct, the third duct being connected to the primary treatment flue gas delivery duct or to the flue gas inlet of the second stage adsorption column.
Preferably, the cooling zone gas outlet is connected to the preheating zone gas inlet by a fifth conduit.
Preferably, the activated carbon desorption column further comprises a nitrogen gas transfer line for introducing nitrogen gas into an upper part of the activated carbon desorption column. The nitrogen conveying pipeline is connected to the desorption tower, and the connecting position of the nitrogen conveying pipeline and the activated carbon desorption tower is positioned above the preheating zone.
Preferably, the nitrogen conveying pipeline is provided with a nitrogen heat exchanger. The preheating zone gas outlet is connected to the inlet of the heating medium channel of the nitrogen heat exchanger through a sixth pipeline.
Preferably, the water vapour outlet is fed to the raw flue gas feed duct via a seventh duct.
Preferably, the SRG gas outlet is conveyed to the acid making system via an SRG gas conveying conduit.
Preferably, the cooling air delivery duct is provided with a cooling air blower.
Preferably, the first pipeline is provided with a hot air fan.
Preferably, the hot blast stove is also provided with an air supplementing opening.
Preferably, the apparatus further comprises a chimney. And the smoke outlet of the second-stage adsorption tower is connected to the chimney through an eighth pipeline.
Preferably, the gas outlet of the first flue gas heat exchanger is connected to the gas inlet of the second flue gas heat exchanger by a first heat exchanger medium delivery duct. And a gas outlet of the second flue gas heat exchanger is connected to a gas inlet of the first flue gas heat exchanger through a second heat exchanger medium conveying pipeline.
Preferably, a fan is arranged on the first heat exchanger medium conveying pipeline and/or the second heat exchanger medium conveying pipeline.
Preferably, the first heat exchanger medium conveying pipeline is provided with a water outlet.
Preferably, a water filling port is arranged on the second heat exchanger medium conveying pipeline.
Preferably, the raw flue gas conveying pipeline is provided with a first temperature detection device, and the first temperature detection device is arranged at the downstream of the first flue gas heat exchanger.
Preferably, the primary treatment flue gas conveying pipeline is provided with a second temperature detection device, and the second temperature detection device is arranged at the downstream of the second flue gas heat exchanger.
In the invention, the first-stage adsorption tower is a desulfurization tower, and the second-stage adsorption tower is a denitration tower.
According to a second embodiment provided by the invention, the activated carbon treatment method for improving the waste heat utilization rate and the denitration rate is provided.
An activated carbon treatment method for improving the residual heat utilization rate and the denitration rate or a method using the activated carbon treatment system for improving the residual heat utilization rate and the denitration rate in the first embodiment, the method comprising the steps of:
1) fresh activated carbon obtained by the analysis of the activated carbon analysis tower is conveyed to an activated carbon inlet of the second-stage adsorption tower through a first activated carbon conveying device; the activated carbon is discharged from an activated carbon outlet of the second-stage adsorption tower from top to bottom in the second-stage adsorption tower, and then the activated carbon discharged from the second-stage adsorption tower is conveyed to the first-stage adsorption tower through a second activated carbon conveying device; the activated carbon is discharged from an activated carbon outlet of the first-stage adsorption tower from top to bottom in the first-stage adsorption tower, and the activated carbon discharged from the first-stage adsorption tower is conveyed to an activated carbon desorption tower through a third activated carbon conveying device for desorption and regeneration;
2) the method comprises the following steps that raw flue gas is conveyed to a first-stage adsorption tower through a raw flue gas conveying pipeline, the raw flue gas is subjected to desulfurization treatment in the first-stage adsorption tower, the flue gas treated by the first-stage adsorption tower is conveyed to a second-stage adsorption tower through a primary treatment flue gas conveying pipeline, the primary treatment flue gas is subjected to denitration treatment in the second-stage adsorption tower, and the flue gas treated by the first-stage adsorption tower and the second-stage adsorption tower is discharged from a chimney;
wherein: in a first flue gas heat exchanger on a raw flue gas conveying pipeline, raw flue gas exchanges heat with a medium in the first flue gas heat exchanger, the raw flue gas releases heat in the first flue gas heat exchanger, the medium absorbs the heat in the first flue gas heat exchanger, and the raw flue gas after releasing the heat and cooling enters a first-stage adsorption tower; the medium after absorbing heat is conveyed to a second flue gas heat exchanger through a first heat exchanger medium conveying pipeline;
in a second flue gas heat exchanger of the primary treatment flue gas conveying pipeline, heat exchange is carried out between primary treatment flue gas treated by the primary treatment flue gas conveying pipeline and a medium in the second flue gas heat exchanger, the medium absorbing heat from the first flue gas heat exchanger releases heat in the second flue gas heat exchanger, the primary treatment flue gas absorbs heat in the second flue gas heat exchanger, and the primary treatment flue gas after absorbing heat and raising the temperature enters a second-stage adsorption tower; and the medium after releasing the heat is circulated to the first flue gas heat exchanger through a medium conveying pipeline of the second heat exchanger.
Preferably, the method further comprises:
3) the hot blast stove heats hot blast, the hot blast enters the heating section of the activated carbon analysis tower from a heating section gas inlet of the activated carbon analysis tower through a first pipeline, the hot blast exchanges heat with activated carbon in the activated carbon analysis tower to heat the activated carbon in the activated carbon analysis tower, and then the hot blast is discharged from a heating section gas outlet and enters the hot blast stove through a second pipeline to continue heating and circulating; and a branch is divided from the second pipeline and is a third pipeline, and a part of hot air which is discharged from the gas outlet of the heating section and subjected to heat exchange is conveyed to a primary treatment flue gas conveying pipeline or a flue gas inlet of a second-stage adsorption tower through the third pipeline.
Preferably, the activated carbon desorption tower comprises a preheating zone, a steam decomposition zone, a pollutant decomposition zone, a cooling zone, a first transition section and a second transition section which are arranged from top to bottom; wherein: the lower part of the preheating zone is provided with a preheating zone gas inlet and a preheating zone gas outlet; the lower part of the water vapor decomposition area is provided with a gas inlet of the water vapor decomposition area and a gas outlet of the water vapor decomposition area; the lower part of the pollutant decomposition area is provided with a pollutant decomposition area gas inlet and a pollutant decomposition area gas outlet; the lower part of the cooling area is provided with a cooling area gas inlet and a cooling area gas outlet; a first transition section is arranged between the water vapor decomposition area and the pollutant decomposition area; a second transition section is arranged between the pollutant decomposition area and the cooling area; a water vapor outlet is arranged on the side wall of the first transition section; and the side wall of the second transition section is provided with an SRG gas outlet.
Preferably, the method further comprises: 4) the active carbon discharged from the first-stage adsorption tower sequentially passes through a preheating zone, a steam decomposition zone, a first transition section, a pollutant decomposition zone, a second transition section and a cooling zone in an active carbon desorption tower; after entering an activated carbon desorption tower, preheating activated carbon containing pollutants in a preheating zone, then removing moisture in a steam decomposition zone, and directly discharging the moisture removed from the activated carbon from a steam outlet on the side wall of the first transition section; then, decomposing the water-removed pollutant-containing activated carbon in a pollutant decomposition area and removing pollutants, and discharging the pollutants from an SRG gas outlet on the side wall of the second transition section; the activated carbon is then cooled in a cooling zone to obtain fresh activated carbon.
Preferably, the method further comprises:
5) cooling gas enters a cooling area of the activated carbon desorption tower from a gas inlet of the cooling area through a cooling gas conveying pipeline, and gas discharged from a gas outlet of the cooling area is conveyed to a preheating area through a fifth pipeline;
the hot blast stove heats hot blast, the hot blast enters the pollutant decomposition area of the activated carbon desorption tower from a gas inlet of the pollutant decomposition area of the activated carbon desorption tower through a first pipeline, the hot blast exchanges heat with the activated carbon in the pollutant decomposition area, heats the activated carbon in the activated carbon desorption tower, and removes pollutants of the activated carbon; then the hot air is discharged from a gas outlet of the pollutant decomposition area and is conveyed to the steam decomposition area from a gas inlet of the steam decomposition area through a fourth pipeline, and the hot air continuously exchanges heat with the activated carbon in the steam decomposition area to remove the moisture in the activated carbon; then the gas is discharged from a gas outlet of the water vapor decomposition area and enters the hot blast stove from a hot blast inlet of the hot blast stove through a second pipeline to continue heating and circulating;
and a branch is divided from the second pipeline and is a third pipeline, and a part of hot air which is discharged from a gas outlet of the water vapor decomposition area and subjected to heat exchange is conveyed to a primary treatment flue gas conveying pipeline or a flue gas inlet of a second-stage adsorption tower through the third pipeline.
Preferably, the gas discharged from the gas outlet of the preheating zone is supplied to the inlet of the heating medium passage of the nitrogen heat exchanger through a sixth pipe to heat the nitrogen gas.
Preferably, the gas discharged from the water vapour outlet is conveyed to the raw flue gas conveying duct by a seventh duct.
Preferably, the SRG gas exiting the SRG gas outlet is transported to the acid making system via an SRG gas transport conduit.
Preferably, the hot air discharged from the gas outlet of the heating section or the gas outlet of the steam decomposition zone after heat exchange is conveyed, wherein the volume fraction of the hot air is 0.5-30% (preferably 1-20%, more preferably 2-15%) to the primary treatment flue gas conveying pipeline or the flue gas inlet of the second-stage adsorption tower through the third pipeline.
Preferably, the first temperature detection device detects the temperature of the raw flue gas in the raw flue gas conveying pipeline after heat exchange, and the temperature of the flue gas entering the first-stage adsorption tower is 100-120 ℃ through the following steps (i) and/or (ii);
adjusting the amount of water added from a water outlet on a first heat exchanger medium conveying pipeline;
adjusting the amount of water discharged from a water filling port on the second heat exchanger medium conveying pipeline.
Preferably, the second temperature detection device detects the temperature of the flue gas after primary treatment in the second flue gas heat exchanger, and the temperature of the flue gas entering the second-stage adsorption tower is 140-155 ℃ through the following steps of (i), (ii) and (iii);
adjusting the amount of water added from a water outlet on a first heat exchanger medium conveying pipeline;
adjusting the amount of water discharged from a water filling port on a medium conveying pipeline of the second heat exchanger;
regulating the amount of hot air which is discharged from a gas outlet of the heating section or a gas outlet of the steam decomposition area and subjected to heat exchange, and conveying the hot air to a primary treatment flue gas conveying pipeline or a flue gas inlet of a second-stage adsorption tower through a third pipeline.
In the invention, the first flue gas heat exchanger is arranged on the original flue gas conveying pipeline before entering the first-stage adsorption tower, so that the waste heat in the original flue gas is absorbed, the temperature of the original flue gas entering the first-stage adsorption tower is regulated and controlled to be between 100 ℃ and 120 ℃, and the temperature is the most suitable flue gas desulfurization temperature, thereby ensuring the desulfurization effect. The technical scheme of adding cold air in the prior art is changed, the increase of the total amount of the original flue gas is avoided, and the loads of subsequent desulfurization and denitration are reduced.
In the invention, the second flue gas heat exchanger is arranged on the primary treatment flue gas conveying pipeline before entering the second-stage adsorption tower, the second heat exchanger releases heat, and the temperature of the primary treatment flue gas is increased, so that the temperature of the flue gas entering the first-stage adsorption tower is regulated and controlled to be between 140 ℃ and 155 ℃, and the temperature is the most suitable flue gas denitration temperature, thereby ensuring the denitration effect. The technical scheme that in the prior art, flue gas is directly input into the denitration tower after being desulfurized is changed, the denitration temperature of the flue gas in the denitration tower is improved, the denitration efficiency is greatly improved, and the denitration rate is improved to more than 80% from about 50% in the prior art. Meanwhile, the spraying amount of ammonia gas in the denitration process is reduced due to the enhancement of the denitration effect; in the prior art, because the denitration temperature is low, in order to guarantee the denitration effect, need spout into a large amount of ammonia, cause the waste of ammonia resource, simultaneously, the ammonia is very easily taken place to escape, has very big potential safety hazard. In the activated carbon system of this application, because the setting of second heat exchanger, guaranteed the denitration temperature of flue gas in the denitration tower, the great denitration efficiency of improvement has reduced the injected volume of ammonia, resources are saved.
In the invention, the first heat exchanger and the second heat exchanger are connected through a first heat exchanger medium conveying pipeline and a second heat exchanger medium conveying pipeline. The first heat exchanger exchanges heat with the raw flue gas in the raw flue gas conveying pipeline on the raw flue gas conveying pipeline, and the medium in the first heat exchanger absorbs the heat of the raw flue gas, so that the temperature of the raw flue gas is reduced to a proper range. Absorbed thermal medium and carried the second heat exchanger, this part medium carries out the heat transfer with the preliminary treatment flue gas in the preliminary treatment flue gas pipeline in the second heat exchanger, and medium release heat adds the preliminary treatment flue gas for temperature risees when this flue gas is carried in the second grade adsorption tower, is fit for the second grade adsorption tower and carries out denitration treatment to the flue gas. That is to say, heat transfer medium circulates between first heat exchanger and second heat exchanger, and heat transfer medium absorbs the heat in first heat exchanger, then releases the heat in the second heat exchanger, utilizes the heat in the former flue gas, through heat transfer medium heating flue gas through desulfurization treatment, temperature when the improvement flue gas gets into the denitration tower.
In the invention, the raw flue gas exchanges heat through the first heat exchanger, the temperature is reduced to the temperature suitable for desulfurization, and then the raw flue gas enters the first-stage adsorption tower (desulfurizing tower) for desulfurization treatment. The flue gas (primary treated flue gas) after desulfurization is subjected to heat exchange with the second heat exchanger, the temperature is raised to a temperature suitable for denitration, and then the flue gas enters a second-stage adsorption tower (denitration tower) for denitration treatment. By using the active carbon treatment system, the flue gas is subjected to desulfurization and denitration treatment at the optimum temperature, so that the desulfurization and denitration efficiency is improved. The waste heat in the original flue gas is used for heating the flue gas subjected to primary treatment through the first heat exchanger and the second heat exchanger, so that the flue gas is fully utilized. When the flue gas is treated, cold air or cold air does not need to be added additionally, so that the stability of the total amount of the flue gas is ensured, and the loads of the desulfurization tower and the denitration tower are also reduced. In addition, the denitration tower carries out denitration treatment at a proper temperature, so that the denitration efficiency is high, and the ammonia gas injection amount is small; the use of ammonia gas is reduced, resources are saved, and the potential safety hazard that ammonia gas is used in a large amount to cause escape is avoided.
In the invention, the activated carbon is analyzed in the activated carbon analysis tower to obtain fresh activated carbon, and then the fresh activated carbon is conveyed to the second-stage adsorption tower through the first activated carbon conveying device, and the fresh activated carbon is used for adsorbing pollutants in the second-stage adsorption tower; then the sewage is conveyed to the first-stage adsorption tower through a second activated carbon conveying device, and the activated carbon adsorbs pollutants in the first-stage adsorption tower. And conveying the activated carbon discharged from the first-stage adsorption tower to an activated carbon desorption tower through a third activated carbon conveying device for desorption and regeneration, and then recycling.
In the invention, the flue gas generated in each process is raw flue gas, the flue gas treated by the first-stage adsorption tower is primary treated flue gas, and the flue gas treated by the second-stage adsorption tower is discharged flue gas (or clean flue gas or discharged gas).
In the invention, the first heat exchanger gas conveying pipeline and/or the second heat exchanger gas conveying pipeline are/is provided with a fan. The fan is used for circulating and circulating media (or heat exchange media) in the first heat exchanger gas conveying pipeline and the second heat exchanger gas conveying pipeline.
In the invention, a water filling port is arranged on the second heat exchanger gas conveying pipeline, and a water drainage port is arranged on the first heat exchanger gas conveying pipeline. According to the temperature of the original flue gas, the temperature of desulfurization in the desulfurization tower and the temperature of denitration in the denitration tower, the water amount added from the water adding port or the water amount discharged from the water discharging port can be adjusted, so that the temperature of the flue gas entering the desulfurization tower and the denitration tower can be controlled and guaranteed.
In the invention, the first temperature detection device detects the temperature of the flue gas in the original flue gas conveying pipeline after heat exchange (heat exchange of the first heat exchanger), namely detects the temperature of the flue gas entering the first-stage adsorption tower (desulfurizing tower). The second temperature detection device is used for detecting the temperature of the flue gas in the primary treatment flue gas conveying pipeline after heat exchange (heat exchange of the second heat exchanger), namely the temperature of the flue gas entering the second-stage adsorption tower (denitration tower).
In the present invention, the end of the primary treatment flue gas conveying pipe refers to the end of the primary treatment flue gas conveying pipe close to the second-stage adsorption tower, that is, the gas flow is downstream in the primary treatment flue gas conveying pipe. The first temperature detection device arranged at the downstream of the first flue gas heat exchanger means that: the first temperature detection device and the first flue gas heat exchanger are both arranged on the original flue gas conveying pipeline, and the first temperature detection device is arranged behind the first flue gas heat exchanger along the flowing direction of gas in the original flue gas conveying pipeline; that is to say, the first temperature detection device is arranged on the raw flue gas conveying pipeline between the first flue gas heat exchanger and the first-stage adsorption tower. The second temperature detection device is arranged at the downstream of the second flue gas heat exchanger, and the second temperature detection device is characterized in that: the second temperature detection device and the second flue gas heat exchanger are both arranged on the primary treatment flue gas conveying pipeline, and the second temperature detection device is arranged behind the second flue gas heat exchanger along the flowing direction of gas in the primary treatment flue gas conveying pipeline; that is to say, the second temperature detection device is arranged on the primary treatment flue gas conveying pipeline between the second flue gas heat exchanger and the second-stage adsorption tower.
As shown in fig. 7, the influence of the flue gas temperature on the denitration effect can be seen. The technical scheme of the invention is shown as attached figure 5, and the process flow is as follows: the temperature of the flue gas (raw flue gas) after the main exhaust fan is T1 (about 110-2Therefore SO in the desulfurizing tower2Will be converted mainly into sulfuric acid, SO2The oxidation to sulfuric acid is a strong exothermic reaction, so the temperature of the activated carbon in the desulfurization tower is 7-10 ℃ higher than the temperature of the flue gas entering the tower at the temperature of T2, the temperature of the flue gas passing through the desulfurization tower is still basically consistent with the temperature of the flue gas entering the desulfurization tower, about T2 in consideration of heat loss, the flue gas after desulfurization enters a second heat exchanger again, the temperature of the flue gas is heated to the temperature of T3 (about 140-3Denitration treatment is carried out in the denitration tower, and the adsorption efficiency of the activated carbon is improved.
Activated carbon circulation direction: activated carbon is sent to the denitration tower through conveying system and gets into the denitration from the regenerator column after regeneration, and the activated carbon through denitration treatment sends to the desulfurizing tower and carries out the desulfurization, and the activated carbon after the desulfurization passes through conveying system and recycles to the regenerator column once more, accomplishes an activated carbon circulation. The active carbon can generate a large amount of gas rich in sulfur dioxide after desorption, and the gas is sent to other processes such as acid preparation, elemental sulfur reduction, preparation of high-concentration liquid SO2, sulfite and the like to realize resource utilization of sulfur.
In the invention, the first flue gas heat exchanger and the second flue gas heat exchanger are circulated by adopting heat exchange media. The heat exchange medium (or media) is generally water, air or other substances with high heat value and no corrosion; the medium is most commonly water. Taking water as an example, the temperature of flue gas entering the inlet of the desulfurization tower and the inlet of the denitrification tower can be adjusted according to the water quantity (controlled by a water filling port and a water outlet), the area of a heat exchanger and the like.
By adopting the active carbon treatment system, the utilization rate of high-temperature flue gas behind the main exhaust fan is improved; rely on the hot flue gas heat of high temperature, through the heat transfer, adjust desulfurizing tower, denitration tower entry flue gas temperature, reach the desulfurizing tower temperature slightly low, the denitration tower temperature is slightly higher, improves SOx/NOx control efficiency.
The flue gas which can be treated by adopting the active carbon treatment system can be flue gas generated by various processes such as sintering, coking, waste incineration and the like, namely the active carbon treatment system can treat sintering flue gas, coking flue gas or flue gas generated by waste incineration.
In the invention, the adsorption tower comprises a first-stage adsorption tower and a second-stage adsorption tower and is of a two-stage adsorption tower structure. Wherein, first order adsorption tower and second level adsorption tower can be arranged about, and second level adsorption tower sets up one side (left side or right side) at first order adsorption tower promptly. The first-stage adsorption tower and the second-stage adsorption tower can also be arranged up and down, namely the second-stage adsorption tower is arranged at the upper part of the first-stage adsorption tower. In the process of flue gas purification, the (sintered) raw flue gas containing various pollutants is desulfurized and dedusted by the first-stage adsorption tower and then enters the second-stage adsorption tower for denitration, NH3Is added into a flue gas inlet of the second-stage adsorption tower.
The main purpose of the desorption tower is to heat and regenerate the active carbon adsorbing the pollutants. The analysis tower is divided into a heating section and a cooling section from top to bottom, and the heating section and the cooling section are provided with a shell-and-tube or shell-and-tube heat exchanger structure. The activated carbon passes through the tube passes of the heating section and the cooling section respectively, while the heating gas passes through the shell pass in the heating section, and the cooling air passes through the shell pass in the cooling section. Between the heating section and the cooling section there is a buffer zone or intermediate zone containing activated carbon. The heat for heating the regenerated active carbon in the desorption tower comes from blast furnace gas or coke oven gas orThe combustion heat of other substances, such as hot blast furnace exhaust gas or hot blast or hot air, enters the desorption tower from a gas inlet of a heating section of the desorption tower and indirectly exchanges heat with the activated carbon to be desorbed. The temperature of the heat exchange hot air entering the desorption tower is 400-500 ℃, preferably 410-470 ℃, more preferably 430-450 ℃, and the exhaust temperature of the gas outlet of the heating section after heat exchange is 300-380 ℃, preferably 320-375 ℃, more preferably 340-370 ℃. In order to keep the pressure and oxygen content in the hot air circulation system stable, the invention leads a second pipeline (or a branch of a fourth pipeline) from a gas outlet of a heating section of the desorption tower to be connected to a flue gas inlet of a second-stage adsorption tower, and leads partial hot air (0.5-30 percent (preferably 1-20 percent, more preferably 2-15 percent)) after being exchanged with the activated carbon into the second-stage adsorption tower, SO that on one hand, SO in the circulating hot air can be removed2On the other hand, the heat can be effectively utilized, and the flue gas temperature at the inlet of the second-stage adsorption tower is improved, so that the denitration efficiency is improved, and the using amount of ammonia can be reduced.
An activated carbon desorption process, comprising the steps of:
1) the active carbon adsorbed with the pollutants enters the active carbon desorption tower from an inlet of the active carbon desorption tower, moves from top to bottom under the action of gravity and sequentially passes through a preheating zone, a water vapor decomposition zone, a first transition section, a pollutant decomposition zone, a second transition section and a cooling zone of the active carbon desorption tower;
2) the active carbon adsorbed with the pollutants is preheated in the preheating zone and then enters the steam decomposition zone, the moisture in the active carbon adsorbed with the pollutants is decomposed and separated in the steam decomposition zone and then enters the first transition section together, and the moisture decomposed and separated from the active carbon adsorbed with the pollutants is discharged from the steam outlet;
3) the active carbon that has adsorbed the pollutant after having separated moisture gets into the pollutant decomposition district, and the pollutant in the active carbon that has adsorbed the pollutant is decomposed and is analyzed in the pollutant decomposition district, then gets into the second changeover portion, and the pollutant that decomposes and resolve out is discharged from the SRG gas outlet, and the active carbon after the analysis is accomplished is discharged from the export of active carbon analytic tower.
In the invention, cooling air enters the cooling zone from a gas inlet of the cooling zone, and is conveyed to the water vapor decomposition zone and/or the preheating zone from a gas outlet of the cooling zone after heat exchange.
In the invention, the desorption hot air enters the pollutant decomposition area from the gas inlet of the pollutant decomposition area, and is conveyed to the water vapor decomposition area and/or the preheating area from the gas outlet of the pollutant decomposition area after heat exchange.
In the invention, the gas subjected to heat exchange in the steam decomposition zone is conveyed to the preheating zone and/or the cooling zone from a gas outlet of the steam decomposition zone.
As is well known, the flue gas desulfurization and denitration device adopting the activated carbon method has important influence on the pollutant removal effect, low temperature is favorable for desulfurization reaction, and high temperature is favorable for denitration reaction.
The heating section of the desorption tower is used for heating hot air of the activated carbon, part of the discharged air amount (the amount of the gas conveyed to the secondary adsorption tower) in the hot air discharged from the gas outlet of the heating section is about 10 percent of the circulating amount (the total amount of the hot air used for heating the activated carbon), and SO2The content is about 100ppm, but because the amount of the gas conveyed to the second-stage adsorption tower is far less than the amount of the flue gas to be treated, the SO in the gas conveyed to the second-stage adsorption tower after being treated by the second-stage adsorption tower2Can be well adsorbed by the active carbon in the second-stage adsorption tower, and can not discharge SO in the gas at the discharge position of the chimney2The concentration causes a large influence. The purpose of the present invention is to prevent SO contained in a hot-air circulating gas for analysis2Directly discharged outside.
In the device, hot air for heating the activated carbon in the desorption tower is conveyed to a flue gas inlet of the second-stage adsorption tower through a third pipeline, wherein a part (for example, 0.5-30%, preferably 1-20%, and more preferably 2-15%) of the hot air discharged from the heating section or the steam decomposition zone of the desorption tower and subjected to heat exchange with the activated carbon is conveyed to the flue gas inlet of the second-stage adsorption tower; the technical scheme that the part of hot air is directly discharged in the prior art is changed. Partial hot air after heat exchange of the heat exchange section of the desorption tower is conveyed to the second-stage adsorption tower for treatment, so that direct outward discharge of the partial hot air is avoided, and pollution of pollutants in the hot air to the environment is avoided. Meanwhile, the temperature of the hot air is higher, and the hot air is conveyed to the air inlet of the second-stage adsorption tower and is mixed with the original flue gas entering the second-stage adsorption tower, so that the temperature of the whole flue gas entering the second-stage adsorption tower is improved, and the denitration efficiency of the second-stage adsorption tower on the flue gas is improved.
In addition, in the prior art, part of circulating hot air is directly discharged outside in order to control SO discharge2The amount of the heat exchange agent is that only a small part of hot air can be discharged outside, so that the heat exchange efficiency of circulating hot air and activated carbon is restricted; because the circulation volume is less and the air volume which is supplemented to enter the hot blast stove is also less, in the scheme, the hot blast stove is always in a low-oxygen state for combustion, so that fuel can not be fully combusted, and the waste of resources is caused. By adopting the design of the application, as part of the circulating hot air is conveyed to the second-stage adsorption tower, the second-stage adsorption tower can process the part of the hot air and discharge the processed hot air from the chimney, the hot air quantity conveyed to the second-stage adsorption tower can be increased according to the requirement, and therefore, a larger amount of air can be supplied from the air supplementing port of the hot blast stove, the oxygen content in the hot blast stove is increased, the combustion rate of fuel is improved, the fuel can be fully combusted, and the fuel resource is saved; meanwhile, due to the fact that fuel is fully combusted and the calorific value is high, the heat exchange efficiency of hot air and active carbon after the hot air conveyed by the hot air furnace enters the desorption tower is improved.
Adopt the device of this application, also can be through detecting the temperature of handling the back flue gas through first order adsorption tower, carry out denitration treatment's best theoretical temperature to the flue gas according to the active carbon, control is from the hot air volume of third pipe-line transportation to second level adsorption tower for when this part hot-blast carries to second level adsorption tower, after mixing with the flue gas after handling through first order adsorption tower, the temperature of mist carries out denitration treatment for the most suitable active carbon, improve the denitration efficiency of second level adsorption tower to the flue gas. If the temperature of the flue gas treated by the first-stage adsorption tower is higher, the amount of hot air conveyed to the second-stage adsorption tower from the third pipeline is reduced; if the temperature of the flue gas treated by the first-stage adsorption tower is lower, the amount of hot air conveyed to the second-stage adsorption tower from the third pipeline is increased.
Therefore, with the apparatus of the present invention, a part of the circulating hot air used by the desorption tower to heat the activated carbon is sent to the second-stage adsorption tower: firstly, the direct discharge of the part of hot air is avoided, because SO in the hot air2The existence of (2) brings the problem of environmental pollution; secondly, as the part of hot air is conveyed to the second-stage adsorption tower, the amount of the hot air which is distributed from the circulating hot air to the second-stage adsorption tower can be increased, the combustion efficiency of fuel in the hot air furnace is improved, and resources are saved; thirdly, the part of hot air is conveyed to the second-stage adsorption tower and is mixed with the flue gas treated by the first-stage adsorption tower, so that the temperature of the flue gas to be treated in the second-stage adsorption tower is increased, and the denitration efficiency is improved.
As a preferred scheme, a special desorption tower structure is adopted, and an activated carbon desorption tower (or called as a desorption tower) is arranged in a preheating zone, a steam decomposition zone, a pollutant decomposition zone, a cooling zone, a first transition section and a second transition section from top to bottom; and a water vapor outlet is arranged on the side wall of the first transition section. After the active carbon containing the pollutants enters the desorption tower, preheating is firstly carried out, then moisture is removed in the steam decomposition area, the moisture removed from the active carbon is directly discharged from a steam outlet on the side wall of the first transition section, and the moisture in the active carbon containing the pollutants is directly removed. Then, decomposing the water-removed pollutant-containing activated carbon in a pollutant decomposition area and removing pollutants, mainly decomposing sulfur-containing substances, and discharging the pollutants from an SRG gas outlet on the side wall of the second transition section; the moisture content in the SRG gas discharged from the device is very low, so that the subsequent acid making process is facilitated. The active carbon containing the pollutants is dehydrated in the water vapor decomposition area, is activated and regenerated after other pollutants are removed in the pollutant decomposition area, and is cooled in the cooling area to obtain fresh active carbon which is recycled to the adsorption tower for use.
In the invention, the first zone is reserved as a preheating zone, and the heating section of the old desorption tower is divided into two zones, namely the second zone is steamA gas decomposition zone; controlling the temperature within the range of 100-300 ℃, and removing the water (free water or crystal water) adsorbed in the activated carbon; zone III is a pollutant decomposition zone for ammonium sulfate or other pollutants, primarily SO2The final temperature is 400-550 ℃, and the mixture stays for a certain time to ensure the complete desorption of the active carbon. And a zone IV active carbon cooling zone.
In the invention, the temperature of the steam decomposition zone is controlled according to the decomposition temperature of the water in the pollutant-adsorbing activated carbon, so that the water in the pollutant-adsorbing activated carbon is decomposed in the steam decomposition zone, the pollutant is not changed (not decomposed and removed) in the zone, the water is removed from the pollutant-adsorbing activated carbon in the steam decomposition zone, and then the pollutant-adsorbing activated carbon is discharged from a steam outlet on the side wall of the first transition section. The temperature of the water vapor decomposition zone is typically 100-200 deg.C, preferably 105-190 deg.C, more preferably 110-180 deg.C.
In the invention, the temperature of the pollutant decomposition area is controlled according to the decomposition temperature of the pollutant (sulfur-containing substance or other pollutants) in the pollutant-adsorbing activated carbon, so that the pollutant in the pollutant-adsorbing activated carbon is decomposed in the pollutant decomposition area, the pollutant is completely removed from the activated carbon, and then the pollutant is discharged from the SRG gas outlet on the side wall of the second transition section. The temperature of the pollutant decomposition zone is typically 400-550 ℃, preferably 410-500 ℃, more preferably 420-480 ℃.
In the invention, the hot air flow of the desorption tower comprises the following steps: the hot air enters from the outlet of the activated carbon heating section, enters through the inlet of the pollutant decomposition section, is discharged from the outlet of the pollutant decomposition section, enters through the inlet of the steam decomposition section, and is discharged from the outlet of the steam decomposition section.
The middle of the steam decomposition area and the pollutant decomposition area is a first transition section which is an activated carbon layer and mainly used for discharging steam; the interior also contains volatile NH 3. A second transition section is arranged between the pollutant decomposition area and the cooling area and is an activated carbon layer which is mainly rich in SO2And (4) discharging the gas. The water vapor content discharged from the first transition stage is about 500Nm3About/h(containing trace ammonia gas) can be discharged into the sintering raw flue gas. The water vapor is discharged into the original sintering flue gas, the composition of the sintering flue gas cannot be influenced firstly (the composition of the original sintering flue gas cannot be influenced completely by the water vapor with the proportion because the volume of the original sintering flue gas is huge), and the ammonia gas contained in the water vapor can be reused secondly, so that the effective utilization of resources is achieved.
In the invention, the problem that the SRG gas in the desorption tower (desorption tower with original structure) in the prior art contains about 30 percent of moisture content and does not use the subsequent process operation is solved; the heating section of the desorption tower is divided into a water vapor decomposition area and a pollutant decomposition area by the principle that the decomposition temperature of adsorbed pollutants is different, wherein the water vapor decomposition area decomposes water (free water and combined water) adsorbed by activated carbon and can also contain trace ammonia gas; the pollutant decomposing region is a boundary region of sulfate or other substances, and mainly decomposes a large amount of SO2Gas or other substances, the moisture content is greatly reduced. The heated activated carbon is then cooled down in a cooling zone of activated carbon. The water vapor amount decomposed by the active carbon is small, and the active carbon can be sent to the original flue and utilizes trace ammonia gas in the flue; the moisture content in the SRG gas is greatly reduced, SO2The volume fraction is greatly increased, which is beneficial to subsequent procedures.
In the invention, the heat of heat exchange in each section (a preheating zone, a steam decomposition zone, a pollutant decomposition zone and a cooling zone) in the desorption tower in the activated carbon can be fully utilized; according to the respective processes in each section of the activated carbon or the activated carbon adsorbing pollutants, or the action or the processes of each section of the desorption tower on the activated carbon or the adsorbed pollutants, the temperature of an air inlet (or an air inlet) of each section (a preheating zone, a water vapor decomposition zone, a pollutant decomposition zone and a cooling zone) is controlled, so that the temperature of the activated carbon in each section of the desorption tower is controlled, and the respective functions of each section are realized. Cold air or hot air (or gas) entering each section of the desorption tower exchanges heat with the activated carbon in the section, is discharged from a gas outlet of the corresponding section, is adaptively input into a gas inlet of other sections (sections requiring the temperature gas) according to the temperature of the discharged gas and the temperature condition of the discharged gas, and is recycled or recycled; the heat of the heat exchange gas is fully utilized, and resources are saved.
In the present invention, cooling air is input from the cooling zone gas inlet to the cooling zone through the cooling gas delivery duct. The hot air is conveyed from the gas inlet of the pollutant decomposition area to the pollutant decomposition area through a hot air conveying pipeline.
In the present invention, depending on the temperature of the gas exiting the gas outlet of the pollutant decomposition zone, the gas exiting the gas outlet of the pollutant decomposition zone may be selectively transported from the gas inlet of the water vapour decomposition zone to the water vapour decomposition zone via a transport conduit or from the gas inlet of the pre-heating zone to the pre-heating zone via a transport conduit. In the actual process, according to the temperature of the gas discharged from the gas outlet of the pollutant decomposition zone and the temperature of the hot air (or hot gas) medium required by the water vapor decomposition zone and the preheating zone, the gas selectively discharged from the gas outlet of the pollutant decomposition zone is conveyed to the gas inlet of the water vapor decomposition zone and/or the gas inlet of the preheating zone for heat exchange with the activated carbon in the water vapor decomposition zone or the preheating zone.
In the present invention, depending on the temperature of the gas exiting the cooling zone gas outlet, the gas exiting the cooling zone gas outlet may be selectively conveyed from the preheating zone gas inlet to the preheating zone via a fifth conduit or from the water vapour decomposition zone gas inlet to the water vapour decomposition zone via a fifth conduit. In practice, the gas selectively discharged from the gas outlet of the cooling zone is supplied to the gas inlet of the water vapor decomposition zone and/or the gas inlet of the preheating zone, depending on the temperature of the gas discharged from the gas outlet of the cooling zone, the temperature of the hot air (or hot gas) medium required for the water vapor decomposition zone and the preheating zone.
In the invention, the gas discharged from the gas outlet of the water vapor decomposition zone can be selectively connected to the hot air inlet of the hot blast stove through a second pipeline according to the temperature of the gas discharged from the gas outlet of the water vapor decomposition zone; either from the preheating zone gas inlet to the preheating zone via a second transfer duct or from the cooling zone gas inlet to the cooling zone via a second transfer duct. In practice, the gas optionally discharged from the gas outlet of the water vapour decomposition zone is supplied to the gas inlet of the preheating zone and/or to the gas inlet of the cooling zone, depending on the temperature of the gas discharged from the gas outlet of the water vapour decomposition zone, the temperature of the hot (or hot) gas medium required for the preheating zone and the cooling zone.
In the invention, the activated carbon desorption tower also comprises a nitrogen conveying pipeline for introducing nitrogen to the upper part of the activated carbon desorption tower. The nitrogen is adopted for protection in the analysis process, and the nitrogen is simultaneously used as a carrier to analyze the SO2And the harmful gases are brought out. And a nitrogen heat exchanger is arranged on the nitrogen conveying pipeline. The gas conveyed by the fourth pipeline and/or the sixth pipeline can be connected to the inlet of the heating medium channel of the nitrogen heat exchanger; the gas conveyed by the fourth pipeline and/or the sixth pipeline is used for exchanging heat with nitrogen.
In the present invention, depending on the temperature of the gas discharged from the gas outlet of the preheating zone, the gas discharged from the gas outlet of the preheating zone may be selectively supplied from the inlet of the heating medium passage of the nitrogen heat exchanger to the nitrogen heat exchanger through the sixth piping or supplied from the gas inlet of the cooling zone to the cooling zone through the sixth supply piping. In practice, the temperature of the gas (or wind) medium required for the nitrogen heat exchanger and the cooling zone depends on the temperature of the gas discharged from the gas outlet of the preheating zone, and the gas selectively discharged from the gas outlet of the preheating zone is supplied to the gas inlet of the heating medium passage of the nitrogen heat exchanger and/or the gas inlet of the cooling zone.
According to the invention, when the activated carbon is used for treating the raw flue gas in the adsorption tower, ammonia gas is sprayed into the adsorption tower, the activated carbon also adsorbs part of the ammonia gas in the adsorption tower, when the activated carbon adsorbing pollutants is desorbed in the desorption tower, the ammonia gas adsorbed in the activated carbon is removed in the section of the steam decomposition area, the steam and the ammonia gas removed in the steam decomposition area can be conveyed to the raw flue gas conveying pipeline through the fifth conveying pipeline, the ammonia gas can be recycled, and resources are saved.
In the invention, the cooling air blower on the cooling air conveying pipeline is used for conveying cooling air to the cooling area. And the hot air fan on the hot air conveying pipeline is used for conveying hot air to the pollutant decomposition area.
Typically, the preheating zone, the water vapor decomposition zone, the contaminant decomposition zone, and the cooling zone have a shell-and-tube or tube-and-tube heat exchanger configuration. The active carbon passes through tube passes of a preheating zone, a steam decomposition zone, a pollutant decomposition zone and a cooling zone respectively, the preheating gas passes through a shell pass in the preheating zone, the heating gas passes through a shell pass in the steam decomposition zone and the pollutant decomposition zone, and the cooling air passes through the shell pass in the cooling zone. A buffer zone or an intermediate zone for containing activated carbon is arranged between the water vapor decomposition zone and the pollutant decomposition zone and is a first transition section; a buffer zone or intermediate zone containing activated carbon is provided between the pollutant decomposition zone and the cooling zone as a second transition zone.
According to the novel active carbon desorption tower provided by the invention, water vapor in desorption gas is separated in advance according to different decomposition temperatures of pollutants adsorbed in active carbon, so that the stable operation of a subsequent process is facilitated. The active carbon adsorbed with the pollutant is in the desorption tower, the moisture adsorbed in the active carbon is firstly decomposed and separated in the water vapor decomposition area, the water vapor is discharged from the water vapor outlet of the desorption tower, the active carbon adsorbed with other pollutants and without the water vapor is continuously analyzed in the desorption tower and the pollutants are removed, the sulfur-containing substances and other pollutants are decomposed and removed in the pollutant decomposition area of the desorption tower and are discharged from the SRG gas outlet of the desorption tower. Because vapor is at first got rid of and is discharged, now to prior art, adopt the novel active carbon analytical tower that this application provided, moisture content greatly reduced in the gaseous SRG who follows the gaseous export exhaust of SRG, because SRG gas temperature is higher, must cool down when getting into the system acid system and handle, because moisture content is few in the SRG gas, consequently, the degree of difficulty greatly reduced of cooling. This process cooling generally adopts water cooling or water heat transfer, because moisture content is few itself in the SRG is gaseous, the cooling water that the cooling was added significantly reduces, the great increase of cooling efficiency moreover (because moisture content is few itself in the SRG is gaseous, the specific heat capacity of water is big). Therefore, by adopting the activated carbon desorption tower provided by the application, the cooling process of the obtained SRG gas for the acid making process is simple, the added cooling water is less, and the cooling efficiency is high.
The waste water treatment of the acid making process is a great problem of the technology, and the waste water treatment process is a key link of the acid making process due to the characteristics of large waste water amount, large acidity in the waste water, various pollutants, organic matters and the like. Adopt the active carbon analytic tower of this application, follow the moisture content in the source greatly reduced SRG gas, the cooling water that adds in the cooling process further reduces to make the waste water volume that the system acid system produced significantly reduce, adopt the device of this application after, the waste water that the system acid technology produced is about 30-60% of the waste water volume that produces among the prior art, reduced waste water treatment work load and the waste water treatment degree of difficulty. The amount of the generated wastewater is reduced, and the total amount of pollutants is unchanged, so that the concentration of the pollutants in the wastewater is increased after the activated carbon desorption tower is adopted, and the treatment (separation or enrichment) effect is obviously improved.
In addition, after the activated carbon desorption tower is adopted, the moisture content in the desorbed SRG gas is low, the cooling process before entering the acid making system is more efficient and stable, the gas is mainly cooled due to the fact that the moisture content with high specific heat capacity is greatly reduced, the control is simpler, the cooling process is more stable, and the cooling effect is more guaranteed; the temperature of SRG gas can be accurately controlled when the acid making process of the glass fiber reinforced plastic material is carried out, so that the safety of the acid making system of the glass fiber reinforced plastic material is ensured, and the service life of the acid making system is prolonged.
By adopting the structure of the activated carbon desorption tower, the problem of excessive moisture content in SRG gas of the desorption tower in the prior art can be perfectly solved, conditions are created for stable operation of subsequent acid making, and the treatment capacity of acid making wastewater can be reduced.
In the invention, the desorption tower and the activated carbon desorption tower are commonly used, and the adsorption tower and the activated carbon adsorption tower are commonly used.
In the present invention, the arrangement of the second-stage adsorption tower downstream of the first-stage adsorption tower means that: according to the flowing trend of the flue gas, the flue gas firstly passes through a first-stage adsorption tower and then passes through a second-stage adsorption tower; the second-stage adsorption tower is positioned at the downstream of the flue gas flowing direction of the first-stage adsorption tower.
In the invention, the first activated carbon conveying device, the second activated carbon conveying device and the third activated carbon conveying device are all used for conveying activated carbon, and any conveying device in the prior art can be adopted.
In the present invention, the preheating zone, the water vapor decomposition zone, the pollutant decomposition zone and the cooling zone are all of a tube-in-tube structure.
Preferably, the heat exchangers are all electric heaters.
By adopting the structure of the activated carbon desorption tower, in the activated carbon desorption tower, firstly, the moisture in the activated carbon adsorbed with pollutants is decomposed and separated in a water vapor decomposition area; since the temperature required for the decomposition of the water vapor is lower, generally 100-150 ℃, the temperature in the water vapor decomposition zone is 100-150 ℃. The activated carbon after passing through the steam decomposition zone enters a pollutant decomposition zone, and in the zone, the activated carbon needs to be heated to the temperature of 410-460 ℃, and a hot blast stove is generally adopted for heating treatment. In the prior art, the activated carbon and pollutants (including moisture) adsorbed in the activated carbon need to be heated to the pollutant decomposition temperature (410-; therefore, by adopting the activated carbon desorption tower, the heat consumed in the pollutant decomposition area is greatly less than that consumed in the heating section of the activated carbon desorption tower in the prior art.
Adopt the active carbon analytic tower structure of this application, separate out moisture in advance at the vapor decomposition district, avoided this part of water to get into the pollutant decomposition district, also avoided giving the heat consumption of this part of water heating at the pollutant decomposition district, reduced the heat consumption of the analytic in-process of active carbon, practiced thrift the energy, reduced the emission of energy burning pollutant simultaneously.
The water vapor is discharged from a water vapor outlet after being decomposed and separated in the water vapor decomposition area and does not enter the pollutant decomposition area; thus, the moisture content of the SRG gas discharged from the SRG gas outlet is greatly reduced. When the SRG gas is conveyed to the acid making purification device for treatment, the SRG gas needs to be cooled, and the moisture content in the SRG gas is low, so that the workload of cooling the part of gas is low, and the cooling efficiency is high. Generally, cold water is added for cooling, and the amount of cold water added for cooling is reduced because the moisture contained in the SRG gas is reduced, so that the amount of wastewater generated in the acid making and purifying process is reduced. In addition, because the SRG gas contains less moisture, the amount of added cold water is further reduced, and the volume concentration of the sulfur dioxide is increased.
Wherein: the height of the resolving tower is 8-30 m, preferably 10-25 m, more preferably 12-20 m; for example around 15 m. The diameter of the second pipe is 0.1 to 1.2 m, preferably 0.2 to 1.0 m, more preferably 0.3 to 0.8 m, and still more preferably 0.4 to 0.6 m.
In the present invention: the height of the activated carbon desorption tower is 8-30 meters, preferably 10-25 meters, and more preferably 12-20 meters; for example around 15 m. The height of the activated carbon adsorption tower is 18-35 m, preferably 20-30 m, and more preferably 24-28 m.
Compared with the prior art, the invention has the following beneficial technical effects:
1. the heat exchangers are respectively arranged before the flue gas is input into the first-stage adsorption tower and the second-stage adsorption tower, so that the temperature of the flue gas entering the first-stage adsorption tower and the second-stage adsorption tower can be controlled, the temperature of desulfurization and denitrification is ensured, and the desulfurization and denitrification efficiency is improved;
2. the first flue gas heat exchanger and the second flue gas heat exchanger circulate through heat exchange media, so that heat is fully utilized, resources are saved, and emission is reduced; due to the arrangement of the heat exchanger, the spraying amount of ammonia gas is reduced while the desulfurization and denitrification efficiency is improved; in addition, cold air blending is avoided, and the total amount of flue gas treated by the active carbon treatment system is reduced.
3. The device leads out a second pipeline from the gas outlet of the heating section of the desorption tower to be connected to the flue gas inlet of the secondary adsorption tower, leads the hot air directly discharged from the gas outlet of the heating section of the desorption tower in the prior art to the secondary adsorption tower, and effectively prevents SO contained in the hot air2The waste water is directly discharged outside, so that the environmental pollution is reduced;
4. according to the invention, part of hot air after heat exchange with the activated carbon is introduced into the secondary adsorption tower, so that the heat is effectively utilized, the flue gas temperature at the inlet of the secondary adsorption tower is increased, and the denitration efficiency is improved;
5. the application develops a new desorption tower structure, and water vapor in desorption gas is separated in advance according to different decomposition temperatures of pollutants adsorbed in active carbon, so that the stable operation of a subsequent process is facilitated; by adopting the activated carbon desorption tower, the moisture content in SRG gas obtained by desorption is low, and the consumed cooling water is low in the cooling process before the acid making process; after the acid making process, the amount of generated waste water is small;
6. adopt the analytic tower of active carbon of this application, moisture content is few in the SRG gas of analytic acquisition, and to the gaseous cooling process of SRG simple, cooling efficiency improves greatly, has guaranteed the gas temperature who gets into the system acid process of glass steel material to guarantee the safety of glass steel material device, prolonged its life.
7. The device can be used in the fields of various activated carbon flue gas treatment such as sintering, coking, waste incineration and the like, is particularly suitable for the working condition of low smoke, and has better heating effect and denitration rate improving effect.
Drawings
FIG. 1 is a schematic structural diagram of an activated carbon treatment system for improving the waste heat utilization rate and the denitration rate according to the present invention;
FIG. 2 is a schematic structural diagram of another design of an activated carbon treatment system for increasing waste heat utilization and denitration rate in accordance with the present invention;
fig. 3 is a schematic structural diagram of a pipeline for conveying desorption tower-fran circulating hot air to flue gas in the activated carbon treatment system for improving the waste heat utilization rate and the denitration rate of the invention;
FIG. 4 is a schematic structural diagram of an activated carbon thermal desorption tower in an activated carbon treatment system for improving the waste heat utilization rate and the denitration rate according to the present invention;
FIG. 5 is a schematic diagram of a connection structure of an activated carbon thermal desorption tower in the activated carbon treatment system for improving the waste heat utilization rate and the denitration rate according to the present invention;
FIG. 6 is a schematic structural diagram of a nitrogen heat exchanger arranged in an activated carbon thermal desorption tower in the activated carbon treatment system for improving the waste heat utilization rate and the denitration rate of the invention;
FIG. 7 is a graph showing the relationship between flue gas temperature and denitration rate.
Reference numerals:
1: an activated carbon adsorption tower; 101: a first stage adsorption tower; 102: a second stage adsorption tower; 2: an activated carbon desorption tower; 3: a first flue gas heat exchanger; 4: a second flue gas heat exchanger; 5: a heating section; 501: a heating section gas inlet; 502: a heating section gas outlet; 6: a cooling section; 7: a hot blast stove; 701: a hot air inlet; 702: a hot air outlet; 703: an air supply opening; 8: a chimney; 9: a fan; 10: a water outlet; 11: a water filling port; l1: an original flue gas conveying pipeline; l2: preliminarily treating the flue gas conveying pipeline; l3: a first conduit; l4: a second conduit; l5: a third pipeline; l6: a cooling gas delivery conduit; l7: a fourth conduit; l8: a fifth pipeline; l9: a nitrogen gas delivery pipe; l10: a sixth pipeline; l11: a seventh pipe; l12: an SRG gas delivery line; l13: an eighth conduit; l14: a first heat exchanger media transport conduit; l15: a second heat exchanger media transport conduit; d1: a first activated carbon delivery device; d2: a second activated carbon delivery device; d3: a third activated carbon delivery device; a1: a preheating zone; a101: a preheating zone gas inlet; a102: a preheating zone gas outlet; a2: a water vapor decomposition zone; a201: a water vapor decomposition zone gas inlet; a202: a vapor decomposition zone gas outlet; a3: a pollutant decomposition zone; a301: a pollutant decomposition zone gas inlet; a302: a pollutant decomposition zone gas outlet; a4: a cooling zone; a401: a cooling zone gas inlet; a402: a cooling zone gas outlet; a5: a first transition section; a6: a second transition section; a7: a water vapor outlet; a8: an SRG gas outlet; a9: a nitrogen heat exchanger; a10: a cooling air blower; a11: a hot air blower; p1: a first temperature detection device; p2: and a second temperature detection device.
Detailed Description
According to the first embodiment provided by the invention, the activated carbon treatment system for improving the waste heat utilization rate and the denitration rate is provided.
The utility model provides an improve activated carbon processing system of waste heat utilization rate and denitration rate, this activated carbon processing system includes activated carbon adsorption tower 1, active carbon analytic tower 2. The activated carbon adsorption tower 1 is a two-stage adsorption tower, and comprises a first-stage adsorption tower 101 and a second-stage adsorption tower 102. The active carbon treatment system further comprises a raw flue gas conveying pipeline L1, a first flue gas heat exchanger 3, a second flue gas heat exchanger 4, a primary treatment flue gas conveying pipeline L2, a first active carbon conveying device D1, a second active carbon conveying device D2 and a third active carbon conveying device D3.
Wherein: the raw flue gas conveying pipeline L1 is connected to the flue gas inlet of the first stage adsorption tower 101. The flue gas outlet of the first stage adsorption tower 101 is connected to the flue gas inlet of the second stage adsorption tower 102 through a primary treatment flue gas conveying pipe L2. The first flue gas heat exchanger 3 is arranged on the raw flue gas supply line L1. The second flue gas heat exchanger 4 is arranged on the primary treatment flue gas conveying pipeline L2. The first activated carbon delivery device D1 connects the activated carbon outlet of the activated carbon desorption tower 2 and the activated carbon inlet of the second-stage adsorption tower 102. The second activated carbon delivery device D2 is connected with the activated carbon outlet of the second-stage adsorption tower 102 and the activated carbon inlet of the first-stage adsorption tower 101. The third activated carbon delivery device D3 is connected to the activated carbon outlet of the first-stage adsorption tower 101 and the activated carbon inlet of the activated carbon desorption tower 2.
Preferably, the activated carbon desorption tower 2 is provided with a heating section 5 and a cooling section 6 from top to bottom. The lower part of the heating section 5 is provided with a heating section gas inlet 501, and the upper part of the heating section 5 is provided with a heating section gas outlet 502. The device also comprises a hot blast stove 7. The hot blast stove 7 is provided with a hot blast inlet 701 and a hot blast outlet 702. A first pipe L3 leading from the hot air outlet 702 of the hot blast stove 7 is connected to the heating section gas inlet 501 of the activated carbon desorption tower 2. A second conduit L4 leading from the heating section gas outlet 502 is connected to the hot blast inlet 701 of the stove 7. A branch, i.e. a third duct L5, branches off from the second duct L4, and the third duct L5 is connected to the primary treatment flue gas conveying duct L2 or to the flue gas inlet of the second stage adsorption tower 102.
Preferably, the activated carbon desorption tower 2 comprises a preheating zone A1, a water vapor decomposition zone A2, a pollutant decomposition zone A3, a cooling zone A4, a first transition section A5 and a second transition section A6 which are arranged from top to bottom.
Wherein: the lower part of the preheating zone A1 is provided with a preheating zone gas inlet a101 and a preheating zone gas outlet a 102. The lower portion of the water vapor decomposition zone A2 is provided with a water vapor decomposition zone gas inlet a201 and a water vapor decomposition zone gas outlet a 202. The lower portion of pollutant decomposition zone A3 is provided with a pollutant decomposition zone gas inlet a301 and a pollutant decomposition zone gas outlet a 302. The lower portion of cooling zone A4 is provided with a cooling zone gas inlet a401 and a cooling zone gas outlet a 402. Between the water vapor decomposition zone a2 and the pollutant decomposition zone A3 is a first transition section a 5. Between the pollutant decomposition zone A3 and the cooling zone a4 is a second transition a 6. The side wall of the first transition section A5 is provided with a water vapor outlet A7. The side wall of the second transition section A6 is provided with an SRG gas outlet A8.
Preferably, the device further comprises a hot blast stove 7. The hot blast stove 7 is provided with a hot blast inlet 701 and a hot blast outlet 702. The cooling zone gas inlet a401 is connected to a cooling gas delivery line L6. A first conduit L3 leading from the hot air outlet 702 of the hot blast stove 7 is connected to the pollutant decomposing region gas inlet a 301. Pollutant decomposition zone gas outlet a302 is connected to water vapor decomposition zone gas inlet a201 by fourth conduit L7. The water vapour decomposition zone gas outlet a202 is connected to the hot air inlet 701 of the stove 7 by a second conduit L4.
Preferably, a branch, i.e. a third duct L5, branches off from the second duct L4, and the third duct L5 is connected to the flue gas inlet of the preliminary treatment flue gas conveying duct L2 or the second-stage adsorption tower 102.
Preferably, the cooling zone gas outlet a402 is connected to the preheating zone gas inlet a101 via a fifth conduit L8.
Preferably, the activated carbon desorption column 2 further includes a nitrogen gas transfer line L9 for introducing nitrogen gas into the upper part of the activated carbon desorption column 2. A nitrogen transfer line L9 was connected to the desorption column 2, and a connection position of the nitrogen transfer line L9 to the activated carbon desorption column 2 was located above the preheating zone a 1.
Preferably, the nitrogen transfer line L9 is provided with a nitrogen heat exchanger a 9. The preheating-zone gas outlet a102 is connected to the inlet of the heating medium passage of the nitrogen heat exchanger a9 through a sixth conduit L10.
Preferably, the water vapour outlet a7 feeds through a seventh conduit L11 to the raw flue gas feed conduit L1.
Preferably, SRG gas outlet A8 is delivered to the acid making system via SRG gas delivery line L12.
Preferably, the cooling air blower a10 is provided in the cooling air duct L6.
Preferably, the first duct L3 is provided with a hot air blower a 11.
Preferably, the hot blast stove 7 is further provided with an air supply port 703.
Preferably, the device further comprises a chimney 8. The flue gas outlet of the second stage adsorption tower 102 is connected to the stack 8 via an eighth duct L13.
Preferably, the gas outlet of the first flue gas heat exchanger 3 is connected to the gas inlet of the second flue gas heat exchanger 4 by a first heat exchanger medium conveying conduit L14. The gas outlet of the second flue gas heat exchanger 4 is connected to the gas inlet of the first flue gas heat exchanger 3 by a second heat exchanger medium conveying pipe L15.
Preferably, the fan 9 is provided on the first heat exchanger medium delivery pipe L14 and/or the second heat exchanger medium delivery pipe L15.
Preferably, the first heat exchanger medium transport pipe L14 is provided with a drain opening 10.
Preferably, the second heat exchanger medium delivery pipe L15 is provided with a filler 11.
Preferably, the raw flue gas conveying pipe L1 is provided with a first temperature detecting device P1, and the first temperature detecting device P1 is disposed downstream of the first flue gas heat exchanger 3.
Preferably, the primary treatment flue gas conveying pipeline L2 is provided with a second temperature detection device P2, and the second temperature detection device P2 is arranged downstream of the second flue gas heat exchanger 4.
In the present invention, the first-stage adsorption tower 101 is a desulfurization tower, and the second-stage adsorption tower 102 is a denitration tower.
Example 1
As shown in fig. 1, an activated carbon treatment system for improving waste heat utilization rate and denitration rate comprises an activated carbon adsorption tower 1 and an activated carbon desorption tower 2. The activated carbon adsorption tower 1 is a two-stage adsorption tower, and comprises a first-stage adsorption tower 101 and a second-stage adsorption tower 102. The active carbon treatment system further comprises a raw flue gas conveying pipeline L1, a first flue gas heat exchanger 3, a second flue gas heat exchanger 4, a primary treatment flue gas conveying pipeline L2, a first active carbon conveying device D1, a second active carbon conveying device D2 and a third active carbon conveying device D3.
Wherein: the raw flue gas conveying pipeline L1 is connected to the flue gas inlet of the first stage adsorption tower 101. The flue gas outlet of the first stage adsorption tower 101 is connected to the flue gas inlet of the second stage adsorption tower 102 through a primary treatment flue gas conveying pipe L2. The first flue gas heat exchanger 3 is arranged on the raw flue gas supply line L1. The second flue gas heat exchanger 4 is arranged on the primary treatment flue gas conveying pipeline L2. The first activated carbon delivery device D1 connects the activated carbon outlet of the activated carbon desorption tower 2 and the activated carbon inlet of the second-stage adsorption tower 102. The second activated carbon delivery device D2 is connected with the activated carbon outlet of the second-stage adsorption tower 102 and the activated carbon inlet of the first-stage adsorption tower 101. The third activated carbon delivery device D3 is connected to the activated carbon outlet of the first-stage adsorption tower 101 and the activated carbon inlet of the activated carbon desorption tower 2. The device also comprises a chimney 8. The flue gas outlet of the second stage adsorption tower 102 is connected to the stack 8 via an eighth duct L13.
Example 2
As shown in fig. 2, example 1 is repeated, except that the gas outlet of the first flue gas heat exchanger 3 is connected to the gas inlet of the second flue gas heat exchanger 4 via a first heat exchanger medium conveying conduit L14. The gas outlet of the second flue gas heat exchanger 4 is connected to the gas inlet of the first flue gas heat exchanger 3 by a second heat exchanger medium conveying pipe L15. The first heat exchanger medium conveying pipeline L3 is provided with a fan 5. The fan 9 is arranged on the first heat exchanger medium conveying pipeline L3 and/or the second heat exchanger medium conveying pipeline L4.
Example 3
Example 2 is repeated, except that the second heat exchanger medium conveying pipeline L15 is provided with a water filling port 11. The first heat exchanger medium conveyance pipe L14 is provided with a drain opening 10. The activated carbon treatment system further comprises a chimney 8. The gas outlet of the second-stage adsorption tower 102 is connected with a chimney 8 through a flue gas discharge pipe L13.
Example 4
Example 3 is repeated except that the raw flue gas conveying pipe L1 is provided with a first temperature detecting device P1 and a first temperature detecting device P1 is provided downstream of the first flue gas heat exchanger 3. The preliminary treatment flue gas conveying pipeline L2 is provided with a second temperature detection device P2, and a second temperature detection device P2 is arranged downstream of the second flue gas heat exchanger 4.
Example 5
As shown in fig. 3, example 3 was repeated except that the activated carbon desorption tower 2 was provided with a heating section 5 and a cooling section 6 from the top. The lower part of the heating section 5 is provided with a heating section gas inlet 501, and the upper part of the heating section 5 is provided with a heating section gas outlet 502. The device also comprises a hot blast stove 7. The hot blast stove 7 is provided with a hot blast inlet 701 and a hot blast outlet 702. A first pipe L3 leading from the hot air outlet 702 of the hot blast stove 7 is connected to the heating section gas inlet 501 of the activated carbon desorption tower 2. A second conduit L4 leading from the heating section gas outlet 502 is connected to the hot blast inlet 701 of the stove 7. A branch, i.e. a third duct L5, branches off from the second duct L4, and the third duct L5 is connected to the primary treatment flue gas conveying duct L2 or to the flue gas inlet of the second stage adsorption tower 102. The first duct L3 is provided with a hot air blower a 11. An air supply port 703 is also arranged on the hot blast stove 7.
Example 6
As shown in fig. 4, example 3 was repeated except that the activated carbon desorption column 2 included, from top to bottom, a preheating zone a1, a water vapor decomposition zone a2, a pollutant decomposition zone A3, a cooling zone a4, a first transition section a5 and a second transition section a 6.
Wherein: the lower part of the preheating zone A1 is provided with a preheating zone gas inlet a101 and a preheating zone gas outlet a 102. The lower portion of the water vapor decomposition zone A2 is provided with a water vapor decomposition zone gas inlet a201 and a water vapor decomposition zone gas outlet a 202. The lower portion of pollutant decomposition zone A3 is provided with a pollutant decomposition zone gas inlet a301 and a pollutant decomposition zone gas outlet a 302. The lower portion of cooling zone A4 is provided with a cooling zone gas inlet a401 and a cooling zone gas outlet a 402. Between the water vapor decomposition zone a2 and the pollutant decomposition zone A3 is a first transition section a 5. Between the pollutant decomposition zone A3 and the cooling zone a4 is a second transition a 6. The side wall of the first transition section A5 is provided with a water vapor outlet A7. The side wall of the second transition section A6 is provided with an SRG gas outlet A8.
The device also comprises a hot blast stove 7. The hot blast stove 7 is provided with a hot blast inlet 701 and a hot blast outlet 702. The cooling zone gas inlet a401 is connected to a cooling gas delivery line L6. A first conduit L3 leading from the hot air outlet 702 of the hot blast stove 7 is connected to the pollutant decomposing region gas inlet a 301. Pollutant decomposition zone gas outlet a302 is connected to water vapor decomposition zone gas inlet a201 by fourth conduit L7. The water vapour decomposition zone gas outlet a202 is connected to the hot air inlet 701 of the stove 7 by a second conduit L4.
A branch, a third duct L5, branches off from the second duct L4, and the third duct L5 is connected to the preliminary treatment fume conveying duct L2. The cooling zone gas outlet a402 is connected to the preheating zone gas inlet a101 by a fifth conduit L8.
A cooling air blower A10 is arranged on the cooling gas conveying pipeline L6.
Example 7
As shown in FIG. 6, example 5 was repeated except that the activated carbon desorption column 2 further included a nitrogen gas feed line L9 for introducing nitrogen gas into the upper part of the activated carbon desorption column 2. A nitrogen transfer line L9 was connected to the desorption column 2, and a connection position of the nitrogen transfer line L9 to the activated carbon desorption column 2 was located above the preheating zone a 1. The nitrogen conveying pipeline L9 is provided with a nitrogen heat exchanger A9. The preheating-zone gas outlet a102 is connected to the inlet of the heating medium passage of the nitrogen heat exchanger a9 through a sixth conduit L10.
The water vapour outlet a7 feeds through a seventh conduit L11 to the raw flue gas feed conduit L1. SRG gas outlet A8 is fed to the acid making system via SRG gas feed line L12.
Use example 1
The activated carbon treatment system described in embodiment 4 is used for treating sintering flue gas, the water quantities of the water filling port 10 and the water discharging port 11 are controlled by monitoring of the first temperature detection device P1, and the temperature of raw flue gas entering the first-stage adsorption tower 101 is 110 ℃; the temperature of the primarily treated flue gas entering the second-stage adsorption tower 102 is 145 ℃ as monitored by a second temperature detection device P2; the flue gas is treated using the system of the present application, flue gas discharge line L13 (or flue gas)The removal effect of pollutants in the exhaust gas detected at the chimney 8) is as follows: SO (SO)2The removal efficiency is 98.6 percent, the denitration rate is 84 percent, and the outlet concentration of dust is 8.9mg/Nm3。
Use example 2
Using the activated carbon treatment System described in example 5 for 600000Nm3Introducing 1% of hot air discharged from the heating section of the desorption tower into the second-stage adsorption tower under the working condition that the flue gas temperature is 140 ℃, wherein the introduced hot air amount is 6000Nm3/h(SO2Concentration is 100ppm), the amount of the hot air introduced into the second stage adsorption tower is only 1/100 of the amount of the original flue gas, and SO is contained in the mixed flue gas2The concentration is also extremely low, and the denitration cannot be influenced.
Calculating the temperature rise value of the mixed flue gas:
sensible heat of raw flue gas at an inlet of a secondary adsorption tower:
Q1＝600000Nm3/h*140℃*0.32Kcal/Nm3.℃＝2.688*107kcal/h；
secondly, introducing sensible heat of hot air in the secondary adsorption tower from hot air discharged from a heating section of the desorption tower:
Q2＝6000Nm3/h*30℃*0.337Kcal/Nm3.℃＝0.606*106kcal/h；
mixing the flue gas with the introduced hot air to obtain the temperature:
T＝(2.688*107+0.606*106)/(600000*0.32+6000*0.337)＝141.67；
after the exhaust hot air outside the desorption tower is introduced into the second-stage adsorption tower, the rise value of the flue gas temperature is as follows:
ΔT＝141.67℃-140℃＝1.67℃。
FIG. 7 shows the influence of the flue gas temperature on the denitration rate, and it can be seen from FIG. 5 that the denitration rate gradually increases as the flue gas temperature increases, and particularly in the temperature range of 140 ℃ and 160 ℃, the denitration rate increases faster as the temperature increases. From the above calculation, it can be known that the discharged hot air in the heating section of the desorption tower is introduced into the inlet of the secondary adsorption tower, the flue gas temperature is increased by 1-2 ℃, and the denitration rate can be increased by 1%. In addition, in order to pursue higher denitration efficiency, the hot air quantity introduced into the secondary adsorption tower can be increased as much as possible on the premise of ensuring the resolution ratio of the activated carbon.
Use example 3
An activated carbon desorption process, comprising the steps of:
1) the active carbon adsorbed with the pollutants enters an active carbon desorption tower A from an inlet of the active carbon desorption tower A, moves from top to bottom under the action of gravity, and sequentially passes through a preheating zone A1, a water vapor decomposition zone A2, a first transition section A5, a pollutant decomposition zone A3, a second transition section A6 and a cooling zone A4 of the active carbon desorption tower A;
2) the active carbon adsorbed with the pollutants is preheated in a preheating zone A1 and then enters a steam decomposition zone A2, the moisture in the active carbon adsorbed with the pollutants is decomposed and separated in the steam decomposition zone A2 and then enters a first transition section A5 together, and the moisture decomposed and separated from the active carbon adsorbed with the pollutants is discharged from a steam outlet A7;
3) the active carbon which is separated from the water and adsorbs the pollutants enters a pollutant decomposition area A3, the pollutants in the active carbon which adsorbs the pollutants are decomposed and analyzed in a pollutant decomposition area A3 and then enter a second transition section A6, the decomposed and analyzed pollutants are discharged from an SRG gas outlet A8, and the analyzed active carbon is discharged from an outlet of an active carbon analysis tower A.
Use example 4
Example 3 is reused, except that cooling air enters the cooling zone A4 from the cooling zone gas inlet A401, and after heat exchange, the cooling air is conveyed to the preheating zone A1 from the cooling zone gas outlet A402 through the second conveying pipeline L4; the analysis hot air enters a pollutant decomposition area A3 from a pollutant decomposition area gas inlet A301, and is conveyed to the water vapor decomposition area from a pollutant decomposition area gas outlet A302 through a first conveying pipeline L3 after heat exchange; the gas after heat exchange in the water vapor decomposition zone A2 is delivered from the gas outlet a202 of the water vapor decomposition zone to the cooling zone a4 through the third delivery pipe L5.
The activated carbon containing the pollutants is subjected to desorption activation (or regeneration) treatment by using the system described in example 6, and 600m of treatment is carried out2The flue gas generated by the sintering machine passes through the activated carbon adsorption tower to be treated, and the flue gas contains pollutantsCarbon, the moisture content in the SRG gas discharged from the SRG gas outlet of the desorption tower is 100-3A/h (the moisture content in the prior art is about 600-750 m)3H) from 5 to 10% by volume of the SRG gas (moisture content of the prior art is from about 25 to 40% by volume of the SRG gas). The SRG gas enters an acid making process after being cooled, and the amount of waste water generated in the acid making process is 30-60% of the amount of waste water generated in the prior art.
And calculating heat quantity, wherein the quantity of the SRG gas is Q (wet basis state), in the prior art, the percentage content of the water vapor is 30%, the specific heat capacity Cp of the water vapor is 33.94J (mol/K), the decomposition temperature of the water vapor is 150 ℃, the target temperature of a heating section of the desorption tower is 430 ℃, and the discharge amount of the water vapor is 60% of the total amount. The hot blast stove efficiency is 80%.
Adopt the analytic tower structure of this application to handle, break away from the vapor decomposition district in the analytic tower earlier vapor, discharge from the vapor outlet to the moisture content in the SRG gas has been reduced. Meanwhile, the water in the activated carbon adsorbed with the pollutants is separated out in the water vapor heating section, so that the heat requirement is reduced in the heating process of the pollutant decomposition area, and the separated water vapor is not heated to 430 ℃; that is, the moisture is separated in advance, the heat supply is reduced, and the energy is saved.
The heat quantity reduced by the water vapor discharged in advance is Q30%/18 60% Cp (430-;
at 600m2For example, Q is 4000m3The reduction heat supply of the pollutant decomposing area of the activated carbon desorption tower is 40733kJ/h according to calculation by adopting the desorption tower.
The heat value of blast furnace gas is known to be 3500kJ/Nm3。
Heat is supplied to the pollutant decomposition area of the active carbon desorption tower through the hot blast stove, and after the desorption tower device is adopted, the amount of the blast furnace gas can be reduced to 40733/3500/80 percent and 14.5Nm3H is used as the reference value. Greatly reduces the use of fuel, saves energy and reduces the emission of pollutants.

Claims (20)

1. An active carbon treatment system for improving the utilization rate of waste heat and the denitration rate comprises an active carbon adsorption tower (1) and an active carbon desorption tower (2); the method is characterized in that: the active carbon adsorption tower (1) is a two-stage adsorption tower and comprises a first-stage adsorption tower (101) and a second-stage adsorption tower (102); the active carbon treatment system also comprises a raw flue gas conveying pipeline (L1), a first flue gas heat exchanger (3), a second flue gas heat exchanger (4), a primary treatment flue gas conveying pipeline (L2), a first active carbon conveying device (D1), a second active carbon conveying device (D2) and a third active carbon conveying device (D3); wherein: the original flue gas conveying pipeline (L1) is connected to a flue gas inlet of the first-stage adsorption tower (101); the flue gas outlet of the first-stage adsorption tower (101) is connected to the flue gas inlet of the second-stage adsorption tower (102) through a primary treatment flue gas conveying pipeline (L2); the first flue gas heat exchanger (3) is arranged on the raw flue gas conveying pipeline (L1); the second flue gas heat exchanger (4) is arranged on the primary treatment flue gas conveying pipeline (L2); the first activated carbon conveying device (D1) is connected with an activated carbon outlet of the activated carbon desorption tower (2) and an activated carbon inlet of the second-stage adsorption tower (102); the second activated carbon conveying device (D2) is connected with the activated carbon outlet of the second-stage adsorption tower (102) and the activated carbon inlet of the first-stage adsorption tower (101); the third activated carbon conveying device (D3) is connected with the activated carbon outlet of the first-stage adsorption tower (101) and the activated carbon inlet of the activated carbon desorption tower (2);
the gas outlet of the first flue gas heat exchanger (3) is connected to the gas inlet of the second flue gas heat exchanger (4) through a first heat exchanger medium conveying pipeline (L14), and the gas outlet of the second flue gas heat exchanger (4) is connected to the gas inlet of the first flue gas heat exchanger (3) through a second heat exchanger medium conveying pipeline (L15);
the activated carbon desorption tower (2) is provided with a heating section (5) and a cooling section (6) from top to bottom; a heating section gas inlet (501) is arranged at the lower part of the heating section (5), and a heating section gas outlet (502) is arranged at the upper part of the heating section (5); the device also comprises a hot blast stove (7); a hot air inlet (701) and a hot air outlet (702) are arranged on the hot air furnace (7); a first pipeline (L3) led out from a hot air outlet (702) of the hot blast stove (7) is connected to a heating section gas inlet (501) of the activated carbon desorption tower (2), and a second pipeline (L4) led out from a heating section gas outlet (502) is connected to a hot air inlet (701) of the hot blast stove (7); a branch, i.e. a third duct (L5), branches off from the second duct (L4), and the third duct (L5) is connected to the flue gas inlet of the preliminary treatment flue gas conveying duct (L2) or the second-stage adsorption tower (102).
2. The activated carbon treatment system of claim 1, wherein: the activated carbon desorption tower (2) comprises a preheating zone (A1), a steam decomposition zone (A2), a pollutant decomposition zone (A3), a cooling zone (A4), a first transition section (A5) and a second transition section (A6) which are arranged from top to bottom; wherein: the lower part of the preheating zone (A1) is provided with a preheating zone gas inlet (A101) and a preheating zone gas outlet (A102); the lower part of the water vapor decomposition area (A2) is provided with a water vapor decomposition area gas inlet (A201) and a water vapor decomposition area gas outlet (A202); the lower part of the pollutant decomposition area (A3) is provided with a pollutant decomposition area gas inlet (A301) and a pollutant decomposition area gas outlet (A302); the lower part of the cooling area (A4) is provided with a cooling area gas inlet (A401) and a cooling area gas outlet (A402); a first transition section (A5) is arranged between the water vapor decomposition zone (A2) and the pollutant decomposition zone (A3); a second transition section (A6) is arranged between the pollutant decomposition zone (A3) and the cooling zone (A4); a water vapor outlet (A7) is arranged on the side wall of the first transition section (A5); the side wall of the second transition section (A6) is provided with an SRG gas outlet (A8).
3. The activated carbon treatment system of claim 2, wherein: the device also comprises a hot blast stove (7); a hot air inlet (701) and a hot air outlet (702) are arranged on the hot air furnace (7); the cooling zone gas inlet (A401) is connected with a cooling gas conveying pipeline (L6); a first pipeline (L3) leading out from a hot air outlet (702) of the hot blast stove (7) is connected to a pollutant decomposing area gas inlet (A301); the pollutant decomposition zone gas outlet (a302) is connected to the water vapour decomposition zone gas inlet (a201) by a fourth conduit (L7); the gas outlet (a202) of the water vapour decomposition zone is connected to the hot air inlet (701) of the hot blast stove (7) by a second conduit (L4).
4. The activated carbon treatment system of claim 3, wherein: the cooling zone gas outlet (a402) is connected to the preheating zone gas inlet (a101) via a fifth conduit (L8).
5. The activated carbon treatment system of claim 4, wherein: the activated carbon desorption tower (2) further comprises a nitrogen conveying pipeline (L9) for introducing nitrogen to the upper part of the activated carbon desorption tower (2), the nitrogen conveying pipeline (L9) is connected to the desorption tower (2), and the connecting position of the nitrogen conveying pipeline (L9) and the activated carbon desorption tower (2) is positioned above the preheating zone (A1).
6. The activated carbon treatment system of claim 5, wherein: a nitrogen heat exchanger (A9) is arranged on the nitrogen conveying pipeline (L9), and a preheating zone gas outlet (A102) is connected to the inlet of a heating medium channel of the nitrogen heat exchanger (A9) through a sixth pipeline (L10); and/or
The water vapor outlet (A7) is conveyed to the raw flue gas conveying pipeline (L1) through a seventh pipeline (L11); the SRG gas outlet (A8) is delivered to the acid making system via SRG gas delivery line (L12).
7. The activated carbon treatment system of claim 6, wherein: a cooling air fan (A10) is arranged on the cooling gas conveying pipeline (L6); a hot air fan (A11) is arranged on the first pipeline (L3); an air supplement port (703) is also arranged on the hot blast stove (7); and/or
The device also comprises a chimney (8); the flue gas outlet of the second stage adsorption tower (102) is connected to the stack (8) via an eighth duct (L13).
8. The activated carbon treatment system of any one of claims 1 to 7, wherein: a fan (9) is arranged on the first heat exchanger medium conveying pipeline (L14) and/or the second heat exchanger medium conveying pipeline (L15); and/or
A water outlet (10) is arranged on the first heat exchanger medium conveying pipeline (L14); a water filling port (11) is arranged on the second heat exchanger medium conveying pipeline (L15).
9. The activated carbon treatment system of any one of claims 1 to 7, wherein: a first temperature detection device (P1) is arranged on the original flue gas conveying pipeline (L1), and the first temperature detection device (P1) is arranged at the downstream of the first flue gas heat exchanger (3); a second temperature detection device (P2) is arranged on the primary treatment flue gas conveying pipeline (L2), and the second temperature detection device (P2) is arranged at the downstream of the second flue gas heat exchanger (4); and/or
The first-stage adsorption tower (101) is a desulfurization tower, and the second-stage adsorption tower (102) is a denitration tower.
10. The activated carbon treatment system of claim 8, wherein: a first temperature detection device (P1) is arranged on the original flue gas conveying pipeline (L1), and the first temperature detection device (P1) is arranged at the downstream of the first flue gas heat exchanger (3); a second temperature detection device (P2) is arranged on the primary treatment flue gas conveying pipeline (L2), and the second temperature detection device (P2) is arranged at the downstream of the second flue gas heat exchanger (4); and/or
The first-stage adsorption tower (101) is a desulfurization tower, and the second-stage adsorption tower (102) is a denitration tower.
11. A method of using the activated carbon treatment system of any one of claims 1-10 to increase waste heat utilization and denitration rate, the method comprising the steps of:
1) fresh activated carbon obtained by the desorption of the activated carbon desorption tower (2) is conveyed to an activated carbon inlet of the second-stage adsorption tower (102) through a first activated carbon conveying device (D1); the activated carbon is discharged from an activated carbon outlet of the second-stage adsorption tower (102) from top to bottom in the second-stage adsorption tower (102), and then the activated carbon discharged from the second-stage adsorption tower (102) is conveyed to the first-stage adsorption tower (101) through a second activated carbon conveying device (D2); the activated carbon is discharged from an activated carbon outlet of the first-stage adsorption tower (101) from top to bottom in the first-stage adsorption tower (101), and the activated carbon discharged from the first-stage adsorption tower (101) is conveyed to an activated carbon desorption tower (2) for desorption and regeneration through a third activated carbon conveying device (D3);
2) raw flue gas is conveyed to a first-stage adsorption tower (101) through a raw flue gas conveying pipeline (L1), the raw flue gas is subjected to desulfurization treatment in the first-stage adsorption tower (101), the flue gas treated by the first-stage adsorption tower (101) is conveyed to a second-stage adsorption tower (102) through a primary treatment flue gas conveying pipeline (L2), the primary treatment flue gas is subjected to denitration treatment in the second-stage adsorption tower (102), and the flue gas treated by the first-stage adsorption tower (101) and the second-stage adsorption tower (102) is discharged from a chimney (8);
wherein: in a first flue gas heat exchanger (3) on a raw flue gas conveying pipeline (L1), raw flue gas exchanges heat with a medium in the first flue gas heat exchanger (3), the raw flue gas releases heat in the first flue gas heat exchanger (3), the medium absorbs the heat in the first flue gas heat exchanger (3), and the raw flue gas after releasing the heat and reducing the temperature enters a first-stage adsorption tower (101); the medium absorbing heat is conveyed to a second flue gas heat exchanger (4) through a first heat exchanger medium conveying pipeline (L14);
in a second flue gas heat exchanger (4) of the primary treatment flue gas conveying pipeline (L2), heat exchange is carried out between primary treatment flue gas treated by a first-stage adsorption tower (101) and a medium in the second flue gas heat exchanger (4), the medium absorbing heat from a first flue gas heat exchanger (3) releases heat in the second flue gas heat exchanger (4), the primary treatment flue gas absorbs heat in the second flue gas heat exchanger (4), and the primary treatment flue gas heated by absorbing heat enters a second-stage adsorption tower (102); the medium after heat release is circulated to the first flue gas heat exchanger (3) through a second heat exchanger medium conveying pipeline (L15).
12. The method of claim 11, wherein: the method further comprises the following steps:
3) the hot blast stove (7) heats hot blast, the hot blast enters the heating section (5) of the activated carbon desorption tower (2) from a heating section gas inlet (501) of the activated carbon desorption tower (2) through a first pipeline (L3), the hot blast exchanges heat with activated carbon in the activated carbon desorption tower (2) to heat the activated carbon in the activated carbon desorption tower (2), and then the hot blast is discharged from a heating section gas outlet (502) and then enters the hot blast stove (7) through a second pipeline (L4) to continue heating and circulating; a branch is branched from the second pipeline (L4) and is a third pipeline (L5), and a part of the hot air which is discharged from the gas outlet (502) of the heating section and subjected to heat exchange is conveyed to the primary treatment flue gas conveying pipeline (L2) or the flue gas inlet of the second-stage adsorption tower (102) through the third pipeline (L5).
13. The method of claim 12, wherein: the activated carbon desorption tower (2) comprises a preheating zone (A1), a steam decomposition zone (A2), a pollutant decomposition zone (A3), a cooling zone (A4), a first transition section (A5) and a second transition section (A6) which are arranged from top to bottom; wherein: the lower part of the preheating zone (A1) is provided with a preheating zone gas inlet (A101) and a preheating zone gas outlet (A102); the lower part of the water vapor decomposition area (A2) is provided with a water vapor decomposition area gas inlet (A201) and a water vapor decomposition area gas outlet (A202); the lower part of the pollutant decomposition area (A3) is provided with a pollutant decomposition area gas inlet (A301) and a pollutant decomposition area gas outlet (A302); the lower part of the cooling area (A4) is provided with a cooling area gas inlet (A401) and a cooling area gas outlet (A402); a first transition section (A5) is arranged between the water vapor decomposition zone (A2) and the pollutant decomposition zone (A3); a second transition section (A6) is arranged between the pollutant decomposition zone (A3) and the cooling zone (A4); a water vapor outlet (A7) is arranged on the side wall of the first transition section (A5); the side wall of the second transition section (A6) is provided with an SRG gas outlet (A8);
the method further comprises the following steps: 4) the activated carbon discharged from the first-stage adsorption tower (101) sequentially passes through a preheating zone (A1), a steam decomposition zone (A2), a first transition section (A5), a pollutant decomposition zone (A3), a second transition section (A6) and a cooling zone (A4) in an activated carbon desorption tower (2); after entering an activated carbon desorption tower (2), the activated carbon containing the pollutants is preheated in a preheating zone (A1), then moisture is removed in a steam decomposition zone (A2), and the moisture removed from the activated carbon is directly discharged from a steam outlet (A7) on the side wall of a first transition section (A5); then, the water-removed active carbon containing the pollutants is decomposed and the pollutants are removed in a pollutant decomposition area (A3), and the pollutants are discharged from an SRG gas outlet (A8) on the side wall of the second transition section (A6); the activated carbon is then cooled by passing it through a cooling zone (a4) to obtain fresh activated carbon.
14. The method of claim 13, wherein: the method further comprises the following steps:
5) cooling gas enters a cooling zone (A4) of the activated carbon desorption tower (2) from a cooling zone gas inlet (A401) through a cooling gas conveying pipeline (L6), and gas discharged from a cooling zone gas outlet (A402) is conveyed to a preheating zone (A1) through a fifth pipeline (L8);
the hot blast stove (7) heats hot blast, the hot blast enters a pollutant decomposition area (A3) of the activated carbon desorption tower (2) from a gas inlet (A301) of the pollutant decomposition area of the activated carbon desorption tower (2) through a first pipeline (L3), the hot blast exchanges heat with activated carbon in the pollutant decomposition area (A3), the activated carbon in the activated carbon desorption tower (2) is heated, and pollutants of the activated carbon are removed; then the gas is discharged from a gas outlet (A302) of the pollutant decomposition area and is conveyed to a steam decomposition area (A2) from a gas inlet (A201) of the steam decomposition area through a fourth pipeline (L7), and the hot air continuously exchanges heat with the activated carbon in the steam decomposition area (A2) to remove the moisture in the activated carbon; then the gas is discharged from a gas outlet (A202) of the water vapor decomposition area and enters a hot air furnace (7) from a hot air inlet (701) of the hot air furnace (7) through a second pipeline (L4) to continue heating circulation;
a branch is branched from the second pipeline (L4) and is a third pipeline (L5), and a part of the hot air which is discharged from the gas outlet (A202) of the water vapor decomposition zone and subjected to heat exchange is conveyed to the primary treatment flue gas conveying pipeline (L2) or the flue gas inlet of the second-stage adsorption tower (102) through the third pipeline (L5).
15. The method of claim 14, wherein: the gas discharged from the gas outlet (A102) of the preheating zone is conveyed to the inlet of the heating medium channel of the nitrogen heat exchanger (A9) through a sixth pipeline (L10) to heat the nitrogen; and/or
The gas discharged from the water vapor outlet (A7) is conveyed to the raw flue gas conveying pipeline (L1) through a seventh pipeline (L11); SRG gas exiting SRG gas outlet (A8) is transported to the acid making system via SRG gas transport line (L12).
16. The method according to any one of claims 12-15, wherein: hot air which is discharged from a gas outlet (502) of the heating section or a gas outlet (A202) of the steam decomposition area and subjected to heat exchange; wherein the hot air with the volume fraction of 0.5-30 percent is conveyed to the flue gas inlet of the primary treatment flue gas conveying pipeline (L2) or the second-stage adsorption tower (102) through a third pipeline (L5).
17. The method of claim 16, wherein: wherein the hot air with the volume fraction of 1-20 percent is conveyed to a primary treatment flue gas conveying pipeline (L2) or a flue gas inlet of the second-stage adsorption tower (102) through a third pipeline (L5).
18. The method of claim 17, wherein: wherein the hot air with the volume fraction of 2-15 percent is conveyed to a primary treatment flue gas conveying pipeline (L2) or a flue gas inlet of the second-stage adsorption tower (102) through a third pipeline (L5).
19. The method of any one of claims 14-15, 17-18, wherein: the first temperature detection device (P1) detects the temperature of the original flue gas in the original flue gas conveying pipeline (L1) after heat exchange, and the temperature of the flue gas entering the first-stage adsorption tower (101) is 100-120 ℃ through the following steps (I) and/or (II);
adjusting the amount of water added from a drain (10) on a first heat exchanger medium conveying pipeline (L14);
adjusting the amount of water discharged from a water feeding port (11) on a second heat exchanger medium conveying pipeline (L15);
and/or
The second temperature detection device (P2) detects the temperature of the flue gas after the primary treatment in the second flue gas heat exchanger (4), and the temperature of the flue gas entering the second-stage adsorption tower (102) is 140-155 ℃ through the following steps of (i), (ii) and (iii);
adjusting the amount of water added from a drain (10) on a first heat exchanger medium conveying pipeline (L14);
adjusting the amount of water discharged from a water feeding port (11) on a second heat exchanger medium conveying pipeline (L15);
regulating the amount of hot air which is discharged from a gas outlet (502) of the heating section or a gas outlet (A202) of the water vapor decomposition area and subjected to heat exchange, and conveying the hot air to a primary treatment flue gas conveying pipeline (L2) or a flue gas inlet of a second-stage adsorption tower (102) through a third pipeline (L5).
20. The method of claim 16, wherein: the first temperature detection device (P1) detects the temperature of the original flue gas in the original flue gas conveying pipeline (L1) after heat exchange, and the temperature of the flue gas entering the first-stage adsorption tower (101) is 100-120 ℃ through the following steps (I) and/or (II);
adjusting the amount of water added from a drain (10) on a first heat exchanger medium conveying pipeline (L14);
adjusting the amount of water discharged from a water feeding port (11) on a second heat exchanger medium conveying pipeline (L15);
and/or
The second temperature detection device (P2) detects the temperature of the flue gas after the primary treatment in the second flue gas heat exchanger (4), and the temperature of the flue gas entering the second-stage adsorption tower (102) is 140-155 ℃ through the following steps of (i), (ii) and (iii);
adjusting the amount of water added from a drain (10) on a first heat exchanger medium conveying pipeline (L14);
adjusting the amount of water discharged from a water feeding port (11) on a second heat exchanger medium conveying pipeline (L15);
regulating the amount of hot air which is discharged from a gas outlet (502) of the heating section or a gas outlet (A202) of the water vapor decomposition area and subjected to heat exchange, and conveying the hot air to a primary treatment flue gas conveying pipeline (L2) or a flue gas inlet of a second-stage adsorption tower (102) through a third pipeline (L5).
CN201810762472.9A 2018-07-12 2018-07-12 Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof Active CN108939808B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201810762472.9A CN108939808B (en) 2018-07-12 2018-07-12 Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201810762472.9A CN108939808B (en) 2018-07-12 2018-07-12 Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof

Publications (2)

Publication Number Publication Date
CN108939808A CN108939808A (en) 2018-12-07
CN108939808B true CN108939808B (en) 2020-09-11

Family

ID=64483903

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201810762472.9A Active CN108939808B (en) 2018-07-12 2018-07-12 Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof

Country Status (1)

Country Link
CN (1) CN108939808B (en)

Families Citing this family (11)

* 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
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
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
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
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
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
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
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
CN116351207B (en) * 2023-06-01 2023-08-29 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 (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
MXPA06015023A (en) * 2006-12-19 2008-10-09 Mexicano Inst Petrol Use of adsorbent microporous carbon material, for reducing benzene content in hydrocarbon flows.

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Also Published As

Publication number Publication date
CN108939808A (en) 2018-12-07

Similar Documents

Publication Publication Date Title
CN108939808B (en) Activated carbon treatment system for improving waste heat utilization rate and denitration rate and use method thereof
CN108939807B (en) Flue gas purification device for improving waste heat utilization rate and denitration rate and use method thereof
RU2685136C1 (en) Method of flue gas desulphurization and denitration and a device
CN108745331B (en) Novel activated carbon analysis tower and activated carbon analysis process
CN105080332B (en) Agglomerates of sintered pellets reclamation system and process
WO2018000888A1 (en) Flue gas desulfurization and denitrification method and device capable of preventing corrosion
CN105944564A (en) Coke oven flue gas waste heat recycling, desulfuration and denitration integrated system and method
CN105688873B (en) Activated carbon Thermal desorption method and its device
CN105698550A (en) Sintering flue gas purification system and method achieving energy conservation and emission reduction
CN109569183B (en) Comprehensive circulation treatment method and treatment device for flue gas of double-series sintering system
CN104190389A (en) Thermal regeneration method and device of activated carbon
CN111203083B (en) Sintering flue gas desulfurization and denitrification process
CN105688667A (en) Method for carrying out denitration on sintering flue gas by utilizing sensible heat of blast furnace slag
CN109174070B (en) Activated carbon analysis tower and activated carbon analysis method
CN206240258U (en) Prevent the flue gas desulfurization and denitrification device of corrosion
CN208177248U (en) It is a kind of based on active carbon/coke coke oven flue gas system for desulfuration and denitration
CN204952658U (en) Sintering pelletizing flue gas resource system
CN109499556B (en) Anti-scaling activated carbon desorption tower and desorption method thereof
CN208893900U (en) A kind of active carbon processing system improving utilization rate of waste heat and denitrification rate
CN204193957U (en) The hot recycling device of active carbon
CN208583143U (en) Afterheat utilizing system
CN113731101B (en) Garbage incineration flue gas treatment system and flue gas treatment method based on activated carbon separation and analysis
CN212651583U (en) Dual cycle formula active carbon separation is analytic msw incineration flue gas processing system
CN208894235U (en) A kind of novel absorbent charcoal Analytic Tower
CN111318147B (en) Sintering flue gas desulfurization and denitrification circulation system

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant