CN203400612U - Flue gas purification system - Google Patents

Flue gas purification system Download PDF

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Publication number
CN203400612U
CN203400612U CN201320390689.4U CN201320390689U CN203400612U CN 203400612 U CN203400612 U CN 203400612U CN 201320390689 U CN201320390689 U CN 201320390689U CN 203400612 U CN203400612 U CN 203400612U
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China
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adsorption tower
flue gas
air inlet
gas
adsorption
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CN201320390689.4U
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Chinese (zh)
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王建辉
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HONGKONG NOROTAEIL ENVIROMENTAL PROTECTION TECHNOLOGY Co Ltd
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HONGKONG NOROTAEIL ENVIROMENTAL PROTECTION TECHNOLOGY Co Ltd
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Abstract

The utility model provides a flue gas purification system. The system comprises a pre-treatment system, a flue gas cooling system and an adsorption tower, wherein flue gas passes through a pipeline, enters the adsorption tower through the pre-treatment system, and is purified; the flue gas cooling system is arranged on a pipeline between the pre-treatment system and the adsorption tower, and comprises a flue gas cooler, an external air diluter, a first temperature sensor, a second temperature sensor and a first flue gas pipe; one end of the first flue gas pipe is fixedly arranged at the air inlet of the adsorption tower; an air inlet baffle is arranged at the air inlet of the adsorption tower; the other end of the first flue gas pipe is connected with the pre-treatment system; the external air diluter and the flue gas cooler are arranged on the first flue gas pipe; the flue gas cooler is positioned between the external air cooler and the adsorption tower; the first temperature sensor is positioned between the external air diluter and the flue gas cooler; the second temperature sensor is positioned between the flue gas cooler and the adsorption tower; a baffle which can be used for adjusting the air intake rate is arranged on the external air cooler. The system can avoid local hot spots generated by activated carbon or active coke in the adsorption tower.

Description

Flue gas purification system
Technical field
The utility model relates to a kind of flue gas purification system, particularly relate in a kind of sintering process of manufacturing for iron-smelter metal or fossil fuel (the coal)/coke in thermal power plant or the combustion process of its compound produce, the flue gas of discharge, or the cleaning system of the flue gas discharging during the burning of industry/life waste material.
Background technology
In the flue gas that produces, discharges in sintering process in the manufacture of iron-smelter metal or fossil fuel (the coal)/coke in thermal power plant or the combustion process of its compound, or in the flue gas that industry/life waste material discharges while burning, contained SOx(oxysulfide), NOx(nitrogen oxide), (pollution sources such as heavy metal), bioxin/furans containing tribute, have caused serious pollution to environment to heavy metal.In order to reduce the pollution of above-mentioned flue gas to environment; what prior art adopted is dry type flue gas purification system, in this system, after flue gas is processed by electrostatic precipitator, sack cleaner, desulphurization plant and denitration device successively; above-mentioned pollutant is effectively removed, and has reached the object of protection of the environment.
This system is used active carbon or activated coke to purify flue gas, but because flue gas itself has higher temperature, add flue gas by after blower fan adiabatic compression by post bake, when entering the flue-gas temperature of adsorption tower over 150 ℃, can make active carbon or activated coke in adsorption tower produce hot localised points, if flue-gas temperature continues over 150 ℃, make focus produce fiery point, active carbon or activated coke can continue oxidation, active carbon or activated coke were lost efficacy and even burn, thereby cause adsorption tower to damage.
Utility model content
The technical problems to be solved in the utility model is to provide a kind of flue gas purification system, also referred to as synthetic flue gas purification system (Synthetic Flue Gas Purification System), slightly be written as S-FGPS, this system adopts active carbon or activated coke to carry out purified treatment to flue gas, can avoid active carbon or activated coke in adsorption tower to produce hot localised points, the normal operation of assurance system.
The utility model flue gas purification system, comprise preprocessing system, flue-gas-cooling system and adsorption tower, flue gas is cleaned after preprocessing system enters adsorption tower by pipeline, described flue-gas-cooling system is arranged on the pipeline between preprocessing system and adsorption tower, described flue-gas-cooling system comprises gas cooler, outer gas diluter, the first temperature sensor and the second temperature sensor, the first fume pipe is the pipeline between preprocessing system and adsorption tower, one end of described the first fume pipe is fixedly mounted on the air inlet of adsorption tower, air inlet baffle plate is installed on the air inlet of described adsorption tower, the other end of the first fume pipe is connected with preprocessing system, described outer gas diluter is arranged on the first fume pipe, described gas cooler is also arranged on the first fume pipe, and gas cooler is between outer gas diluter and adsorption tower, described the first temperature sensor and the second temperature sensor are all installed on the first fume pipe, and the first temperature sensor is between outer gas diluter and gas cooler, the second temperature sensor is between gas cooler and adsorption tower, on the outer gas air inlet of described outer gas diluter, be provided with can adjusting air inflow quantity baffle plate.
The utility model flue gas purification system, wherein said preprocessing system comprises electrostatic precipitator and the first sack cleaner, the first fume pipe is connected with the outlet of the first sack cleaner, the import of electrostatic precipitator is connected with fume emission mouth, the gas outlet of adsorption tower is communicated with chimney, flue gas purification system also comprises the second fume pipe, one end of the second fume pipe is connected on the pre-treatment flue between electrostatic precipitator and the first sack cleaner, the other end of the second fume pipe is connected with chimney, on the second fume pipe, master shield is installed, master shield is also installed on the first fume pipe, master shield on the first fume pipe is between outer gas diluter and pre-treatment flue and the second fume pipe junction.The utility model flue gas purification system, wherein said gas cooler comprises housing and shower, the upper end of housing offers air inlet, the lower end of housing offers gas outlet, shower is arranged in housing, and some nozzles are installed on shower, and the outlet of nozzle all down, described nozzle can spray water droplet and compressed-air actuated mixture, and the diameter of water droplet is less than 60 microns.
The utility model flue gas purification system, also comprises three-temperature sensor, and described three-temperature sensor is arranged in adsorption tower.
The utility model flue gas purification system, wherein said adsorption tower comprises at least one adsorption module, at least one top storage tank and at least one bottom discharge tank, each adsorption module includes top storage bin, denitration chamber, desulfurization chamber and bottom storage bin, denitration chamber is positioned at desulfurization chamber top, between denitration chamber and desulfurization chamber, be provided with into ammonia chamber, enter the bottom of ammonia chamber and the top of desulfurization chamber is connected, enter indoor at least one the first air inlet doffer that is provided with of ammonia, between denitration chamber and desulfurization chamber, by the first air inlet doffer, be communicated with, the first air inlet doffer comprises bucket, lower bucket and tube connector, upper bucket and lower bucket be big up and small down infundibulate all, the upper end open of upper bucket is communicated with the bottom of denitration chamber, on lower bucket is sleeved on and struggles against, between lower bucket and upper bucket, be provided with gap, the lower ending opening of lower bucket is communicated with the upper end of tube connector, the lower end of tube connector is communicated with the top of desulfurization chamber, bottom storage bin is positioned at desulfurization chamber below, between bottom storage bin and desulfurization chamber, be provided with bottom compartment, in bottom compartment, be provided with at least one second air inlet doffer, the second air inlet doffer is identical with the first air inlet doffer structure, between bottom storage bin and desulfurization chamber, by the second air inlet doffer, be communicated with, the upper end open of the upper bucket of the second air inlet doffer is communicated with the bottom of desulfurization chamber, the lower end of the tube connector of the second air inlet doffer is communicated with bottom storage bin, top storage bin is positioned at the top of denitration chamber, the top of denitration chamber is provided with at least one blanking funnel, the upper end of blanking funnel is communicated with top storage bin, the lower ending opening of blanking funnel is positioned at the top of denitration chamber, top storage tank is positioned at storage bin top, top, and be communicated with top storage bin, bottom discharge tank is positioned at storage bin below, bottom, and be communicated with bottom storage bin, top storage tank is connected with the charging aperture of adsorption tower, bottom discharge tank is connected with the discharging opening of adsorption tower, bottom in bottom compartment offers gas approach, entering on ammonia chamber, to offer ammonia injection apparatus, top in denitration chamber offers exhanst gas outlet, gas approach is communicated with the air inlet of adsorption tower, exhanst gas outlet is communicated with the gas outlet of adsorption tower.
The utility model flue gas purification system, wherein said adsorption tower comprises absorption module and support, absorption module comprises at least one adsorption module group, at least 1 top storage tank and at least 1 bottom discharge tank, adsorption module group comprises 4 adsorption modules, 4 adsorption modules are divided into two-layer up and down, 2 every layer, the adsorption module adjacent with layer is fixedly connected with left and right between any two, between upper and lower two-layer adsorption module, be also fixedly connected with, the bottom of two adsorption modules of lower floor is connected with support with at least 1 movable part by a fixture, described movable part is positioned at the surrounding of fixture, fixture forms a fixed connection a little, movable part forms and is flexibly connected point, two parts up and down of described movable part can relatively move on horizontal plane, described in each, the top storage bin of adsorption module is all connected with four discharging openings of 1 tripper by 4 the second top fed pipes, each tripper charging aperture is all connected with top storage tank by 1 the first top fed pipe, the bottom storage bin of each adsorption module all logical charge tube is connected with bottom discharge tank.
The utility model flue gas purification system, wherein said absorption module comprises two adsorption module groups, before and after two adsorption module groups, arrange, between two adsorption module groups, air inlet pipe and escape pipe are set, one end of air inlet pipe is connected with the air inlet of adsorption tower, the other end of air inlet pipe is connected with the gas approach of each adsorption module, and one end of escape pipe is connected with the exhanst gas outlet of each adsorption module, and the other end of escape pipe is communicated with the gas outlet of adsorption tower.Absorption module is two when above, and absorption module between any two left and right is arranged side by side, and considers thermal expansion, has gap between two between adjacent absorption module.
The utility model flue gas purification system, wherein on the gas approach of adsorption module and exhanst gas outlet, be separately installed with indivedual baffle plate C and indivedual baffle plate D, the upper end of the lower end of indivedual baffle plate C and indivedual baffle plate D is all hinged on the sidewall of adsorption module, the top of indivedual baffle plate C is connected with the piston rod of a cylinder G by linkage, cylinder G can drive indivedual baffle plate C sealing gas approach, the bottom of indivedual baffle plate D is also connected with the piston rod of another cylinder G by linkage, and another cylinder G can drive indivedual baffle plate D sealing exhanst gas outlets.
The utility model flue gas purification system, also comprise regenerator and active device, the bottom discharge tank of described adsorption tower is connected with the charging aperture of active device, the discharging opening of described active device is connected with the charging aperture of regenerator, the discharging opening of described regenerator is connected with the top storage tank of adsorption tower, described active device comprises housing, transfer device and additive shower, and described additive shower is positioned at the top of transfer device, and the medicament of described additive shower spray is urea compounds.
The utility model flue gas purification system, also comprises fresh active carbon storage bin, and the discharging opening of described fresh active carbon storage bin is communicated with the charging aperture of regenerator.By fresh active carbon storage bin being connected to the charging aperture of regenerator, can remove moisture and fugitive constituent in fresh active carbon, increase its active function groups.
The utility model flue gas purification system, also comprise dust pelletizing system, described dust pelletizing system comprises first, second, the 3rd dust arrester and the second sack cleaner, the first dust arrester is arranged between active device and adsorption tower, the second dust arrester is arranged on the charging aperture of adsorption tower, the 3rd dust arrester is arranged on the charging aperture place of regenerator, first, second, the 3rd dust arrester structure is identical, include tubular shell, air inlet, feed pipe, gas outlet and discharging opening, air inlet is opened in the bottom of housing, gas outlet is opened in the top of housing, discharging opening is opened in the bottom of housing, feed pipe is arranged on the top of housing, the discharging opening of feed pipe is communicated with housing inner chamber, the charging aperture of feed pipe is connected with the bottom discharge tank of adsorption tower, discharging opening is connected with the charging aperture of active device, gas outlet is connected with the second sack cleaner by blower fan, air inlet is communicated with ambient atmosphere.
The utility model flue gas purification system, wherein said dust pelletizing system also comprises some dust shields, described dust shield is arranged on the top of conveying track, and described conveying track is the track of Transport Activity charcoal or activated coke, and described dust shield is connected with described sack cleaner by pipeline.
The utility model flue gas purification system, wherein said preprocessing system comprises electrostatic precipitator and the first sack cleaner, and described electrostatic precipitator is one-time dedusting device, and the first sack cleaner is final dusting device.
The utility model flue gas purification system, the active carbon that wherein said adsorption tower is used be by weight percent hundred for after brown coal 80% and bituminous coal 20% coordinates with tar, through charing, process final activated processing and making.
The utility model flue gas purification system, in wherein said adsorption tower, the flow velocity of smoke gas flow through desulfurization chamber and denitration chamber is 0.2-0.3m/sec.
The utility model flue gas purification system difference from prior art is that the utility model is by arranging flue-gas-cooling system, on the first fume pipe that passes into flue gas in adsorption tower, gas cooler is installed, outer gas diluter, the first temperature sensor, the second temperature sensor, by the first temperature sensor, detect and enter the flue-gas temperature in the first fume pipe, and to the flue gas of excess Temperature, carry out cooling by gas cooler and outer gas diluter, then by the second temperature sensor, detect cooled flue-gas temperature, assurance enters the critical-temperature that flue gas in adsorption tower is no more than active carbon or activated coke work, thereby can effectively avoid active carbon or activated coke in adsorption tower to produce hot localised points, avoid active carbon or activated coke to lose efficacy, burning, damage adsorption tower.
The utility model flue gas purification system, by the second fume pipe is set, when flue gas is after gas cooler and the cooling of outer gas diluter, while still surpassing critical-temperature, directly discharges overheated flue gas by the second fume pipe, avoids overheated flue gas to enter adsorption tower.By nozzle being set on the shower of gas cooler, nozzle sprays water droplet and compressed-air actuated mixture downwards, make cooling water form the fine liquid particles that is less than 60 microns, the flue gas entering with air inlet from upper end mixes, water droplet in mixture can play the effect to flue gas cool-down, water droplet, when giving flue gas cool-down, evaporates completely after being heated, thereby can not cause adsorption tower or smoke conveying duct to be corroded.By three-temperature sensor is installed in adsorption tower, can direct-detection to the temperature of active carbon or activated coke, avoid active carbon or activated coke to occur focus.
Below in conjunction with accompanying drawing, flue gas purification system of the present utility model is described further.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model flue gas purification system;
Fig. 2 is the structural representation of adsorption module in the utility model flue gas purification system;
Fig. 3 a is the structural representation of adsorption tower in the utility model flue gas purification system;
Fig. 3 b is the connection diagram of attached module and support in the utility model flue gas purification system;
Fig. 4 a is the turnover gas baffle arrangement schematic diagram of adsorption module in the utility model flue gas purification system;
Fig. 4 b is the stereogram of the turnover gas baffle plate of adsorption module in the utility model flue gas purification system;
Fig. 5 a is the stereogram (amplification) of the turnover gas baffle plate of adsorption module in the utility model flue gas purification system;
Fig. 5 b is the turnover gas baffle arrangement schematic diagram (amplification) of adsorption module in the utility model flue gas purification system;
Fig. 6 is the structural representation of the dust arrester of dust pelletizing system in the utility model flue gas purification system;
Fig. 7 is the active carbon delivery track dedusting schematic diagram of dust pelletizing system in the utility model flue gas purification system;
Fig. 8 is the schematic diagram of the flue-gas-cooling system of the utility model flue gas purification system;
Fig. 9 is the active carbon desulfurization power curve figure of the utility model flue gas purification system.
The specific embodiment
Flue gas purification system, in the flue gas producing during by the burning of the fossil fuel of iron-smelter sintering process or Coal-fired power plant and compound thereof, or in the flue gas of incinerator discharge, contained oxysulfide, nitrogen oxide, tribute, bioxin/furans and dust catching the integrated system of removing, as shown in Figure 1, the utility model flue gas purification system comprises preprocessing system, flue-gas-cooling system and adsorption tower, regenerator 6 and active device 5, dust pelletizing system and fresh active carbon storage bin 4o, flue gas is cleaned after preprocessing system enters adsorption tower 4 by pipeline, flue gas after purification is discharged by chimney 7.
Preprocessing system of the present utility model comprises electrostatic precipitator 1 and the first sack cleaner 2, and electrostatic precipitator 1 is one-time dedusting device, and the first sack cleaner 2 is final dusting device.The density 3-5g/Nm containing in flue gas 3dust, by electrostatic precipitator 1, by the corona discharge that applies positive high voltage and produce, density is dropped to 40mg/Nm 3below trapping afterwards.Flue gas aspirates and delivers in electrostatic precipitator 1 by the air-introduced machine (1a) of rear end.Flue gas is removed after dust by electrostatic precipitator 1 is preliminary, by the booster fan 2b of rear end, aspirates and delivers in sack cleaner 2.
The fine dust that alkali and chloride produce, the alkali salt existing with gaseous state and SO 3and fine dust and the composite pollution material thereof such as other sticky dusts, the front end by sack cleaner sprays the modes such as nertralizer with quantitative spraying device 2d, trap, neutralize and remove.Nertralizer is used agstone or lime stone solution.
While carrying out secondary dust removal with the first sack cleaner 2, in order to improve arresting efficiency, the flow velocity of process filter maintains 0.8-1.3m/sec conventionally, and preferred flow velocity is 0.9-1.1m/sec.
The fine dust and the polluter that by the first sack cleaner 2, trap and remove, the pollution sources that are caught in are by the compressed-air actuated air pulse of the program having arranged, from deduster, separate and fall, conveying device and gathering-device by bottom separately deal with, and the air inlet that a part is delivered to the front end of the first sack cleaner 2 by path (2f) reuses.
When the temperature when flue gas enters adsorption module surpasses 150 ℃, high temperature makes the active carbon of adsorption module inside maintain superheat state, cause emergencies such as " focuses ", security and the durability of adsorption module can be affected, so need to the intake air temperature of flue gas be dropped to below 150 ℃ by flue-gas-cooling system.
Flue-gas-cooling system is arranged on the pipeline between preprocessing system and adsorption tower, shown in Fig. 8, flue-gas-cooling system comprises gas cooler 3, outer gas diluter 2c, the first temperature sensor 11, the second temperature sensor 12, three-temperature sensor, the first fume pipe 13 and the second fume pipe 2e.Flue gas is through after pre-treating technology, and the dust that may have influence on adsorption tower performance and efficiency is removed, and this flue gas is delivered in gas cooler 3 by the first fume pipe 13 by the negative pressure of booster fan 2b front end and the malleation of rear end subsequently.One end of the first fume pipe 13 is fixedly mounted on the air inlet of adsorption tower 4, air inlet baffle plate is installed on the air inlet of adsorption tower 4, air inlet baffle plate can regulate the air inflow of air inlet, the other end of the first fume pipe 13 is communicated with the gas outlet of sack cleaner 2, outer gas diluter 2c is arranged on the first fume pipe 13, gas cooler 3 is also arranged on the first fume pipe 13, and gas cooler 3 is between outer gas diluter 2c and adsorption tower 4, the first temperature sensor 11 and the second temperature sensor 12 are all installed on the first fume pipe 13, and the first temperature sensor 11 is between outer gas diluter 2c and gas cooler 3, the second temperature sensor 12 is between gas cooler 3 and adsorption tower 4, three-temperature sensor is arranged in adsorption tower 4.On the outer gas air inlet of outer gas diluter 2c, be provided with can adjusting air inflow quantity baffle plate.One end of the second fume pipe 2e is connected on the pre-treatment flue between electrostatic precipitator 1 and the first sack cleaner 2, the other end of the second fume pipe 2e is connected with chimney 7, on the second fume pipe 2e, master shield is installed, on the first fume pipe 13, master shield is also installed, the master shield on the first fume pipe 13 is between outer gas diluter 2c and pre-treatment flue and the second fume pipe 2e junction.Gas cooler 3 in the utility model comprises housing and shower, the upper end of housing offers air inlet, the lower end of housing offers gas outlet, shower is arranged in housing, some nozzles are installed on shower, all down, nozzle can spray water droplet and compressed-air actuated mixture in the outlet of nozzle, and wherein the diameter of water droplet is less than 60 microns.
Above-mentioned flue-gas-cooling system carries out when cooling, according to the following step, carrying out to flue gas:
1, flue gas is entered in adsorption tower 4 from the first fume pipe 13;
When the flue-gas temperature 2, detecting when the first temperature sensor 11 is no more than 150 ℃, close the outer gas air inlet of outer gas diluter 2c, gas cooler 3 does not carry out cooling to flue gas simultaneously;
When the flue-gas temperature 3, detecting when the first temperature sensor 11 surpasses 150 ℃, gas cooler 3 starts, and the flue-gas temperature that the second temperature sensor 12 is detected is no more than 150 ℃;
When the flue-gas temperature 4, detecting when the second temperature sensor 12 surpasses 150 ℃, should continue to start gas cooler 3, and the air inlet of simultaneously opening outer gas diluter 2c to the first fume pipe 13 is interior supplement outside gas, to flue gas dilution cooling, the flue-gas temperature that the second temperature sensor 12 is detected is no more than 150 ℃.
In step 4, by controlling the unlatching size of the baffle plate of outer gas diluter 2c air inlet, control the outer gas that enters the first fume pipe 13, make flue-gas temperature that the second temperature sensor 12 detects a little less than 150 ℃.After if gas cooler 3 is all opened with outer gas diluter 2c, when the temperature that the second temperature sensor 12 detects still continues to surpass 150 ℃, close the master shield on the first fume pipe 13, open the master shield on the second fume pipe 2e, make flue gas directly enter chimney 7 from the second fume pipe 2e, open outer gas diluter 2c simultaneously, close gas cooler 3, make outer gas enter adsorption tower 4 by the first fume pipe 13.
It in accompanying drawing 8, is the example that application flue-gas-cooling system of the present utility model regulates flue-gas temperature.
Take iron-smelter sinter fume as example, the reason that temperature rises has two kinds, the first, in sintering machine, because doing equipment operation and the raw material condition in man-hour, cause temperature to rise, the second, the flue gas of being discharged by sintering machine by two pressure fan adiabatic compression, causes temperature to rise in the process through electrostatic precipitator and sack cleaner.
Conventionally, flue-gas temperature is the highest when rising to 150 ℃, the first temperature sensor 11 detects abnormal temperature, gas cooler 3 is dripped with compressed-air actuated mixture and is reduced flue-gas temperature by water spray, the second temperature sensor 12 is confirmed, assurance is delivered to flue-gas temperature in adsorption tower 4 and has been dropped to below 150 ℃, makes flue gas through normal flue gas processing procedure.After spraying the high-pressure delivery pump of water by gas cooler 3 interior installations and mixing with compressed air in nozzle, lean on this pressure to gush out to be less than the water droplet of 60 microns, and cooled flue gas, and can not cause the impacts such as adsorption tower 4 or flue gas delivery pipe road are corroded.
If flue-gas-cooling system detects the flue-gas temperature that enters adsorption tower 4 while being up to the situation of 200 ℃, also can be cooled to normal temperature by flue-gas-cooling system.This cooling system reduces temperature by gas cooler 3 preliminary (for the first time), then by outer gas diluter 2c, further reduces temperature for the second time.
To iron-smelter sinter fume, during work, the intake air temperature condition of native system 180 ℃ of 90 – normally, the highest 200 ℃.
In order to successfully manage different temperature conditions and effectively to use this flue-gas-cooling system, use step specific as follows:
Step 1: the Cooling Process in the gas cooler 3 of adsorption tower 4 front ends.When the temperature that the first temperature sensor of adsorption tower 4 front ends detects surpasses 150 ℃, as first step, with the gas cooler 3 of adsorption tower front end, start to spray air-water mixture.The purpose of design of water-cooled is by small water droplet, flue-gas temperature to be cooled to below 150 ℃.The temperature difference between the variation of water consumption and actual temperature and design temperature is proportional.
Step 2: be outer gas dilution that synchronize with step 1, sack cleaner 2 rear ends.In gas cooler 3 after water-cooled, the temperature that the second temperature sensor 12 of adsorption tower 4 front ends detects does not but lower all the time, in this case, as second step, with the outer gas diluter 2c of sack cleaner 2 rear ends, supplement and carry out outer gas dilution operation.When the temperature that the second temperature sensor 12 detects surpasses 150 ℃, externally the air inlet baffle plate of gas diluter 2c is adjusted immediately, to introduced outer gas and mixed with flue gas by outer gas diluter 2c.
Step 3: during emergency by the second fume pipe 2e directly by high-temperature flue gas to chimney, and only permitted in outer gas introducing adsorption tower.After water-cooled and outer gas dilution, the temperature that adsorption tower front end the second temperature sensor 12 detects declines still abundant not, continue to maintain more than 150 ℃, in this case, need to high-temperature flue gas be directly delivered to chimney by the second fume pipe 2e in sack cleaner 2 the place aheads, and only permitted outer gas and introduce in adsorption tower 4 by outer gas diluter 2c, overheated to prevent adsorption tower.
Step 4: return to normal operation.The temperature that adsorption tower front end the second temperature sensor 12 detects is during lower than 150 ℃, and bypass mode of operation will return to normal operation mode.
In flue-gas temperature rises between very little and short-term, have intermittently, only use outer gas diluter, with the outer gas of its introducing, and after flue gas dilution, reduce temperature.
Shown in Fig. 2, in the utility model, adsorption tower 4 comprises an adsorption module, a top storage tank 4s and a bottom discharge tank 4k, adsorption module includes top storage bin 4c, denitration chamber 4b, desulfurization chamber 4a and bottom storage bin 4l, denitration chamber 4b is positioned at desulfurization chamber 4a top, between denitration chamber 4b and desulfurization chamber 4a, be provided with into ammonia chamber 4g, the bottom of entering ammonia chamber 4g is connected with the top of desulfurization chamber 4a, enter and in the 4g of ammonia chamber, be provided with 4 the first air inlet doffer 4h, between denitration chamber 4b and desulfurization chamber 4a, by 4 the first air inlet doffer 4h, be communicated with, each first air inlet doffer 4h includes bucket 4h1, lower bucket 4h2 and tube connector 4h3, upper bucket 4h1 and lower bucket 4h2 be big up and small down infundibulate all, the upper end open of upper bucket 4h1 is communicated with the bottom of denitration chamber 4b, lower bucket 4h2 is sleeved on bucket 4h1, between lower bucket 4h2 and upper bucket 4h1, be provided with gap, so that flue gas enters the gap of active carbon or activated coke particle from the gap between bucket 4h1 and lower bucket 4h2.The lower ending opening of lower bucket 4h2 is communicated with the upper end of tube connector 4h3, the lower end of tube connector 4h3 is communicated with the top of desulfurization chamber 4a, thereby active carbon is entered in desulfurization chamber 4a through the first air inlet doffer 4h from denitration chamber 4b, and the flue gas on desulfurization chamber 4a top, through entering after the 4g of ammonia chamber, can enter in the 4b of denitration chamber by the gap between upper bucket 4h1 and lower bucket 4h2.
Bottom storage bin 4l is positioned at desulfurization chamber 4a below, between bottom storage bin 4l and desulfurization chamber 4a, be provided with the 4e of bottom compartment, in the 4e of bottom compartment, be provided with 4 the second air inlet doffer 4f, the second air inlet doffer 4f is identical with the first air inlet doffer 4h structure, between bottom storage bin 4l and desulfurization chamber 4a, by the second air inlet doffer 4f, be communicated with, the upper end open of the upper bucket of the second air inlet doffer 4f is communicated with the bottom of desulfurization chamber 4a, the lower end of the tube connector of the second air inlet doffer 4f is communicated with bottom storage bin 4l, so that flue gas gap between bucket and lower bucket from the second air inlet doffer 4f enters in desulfurization chamber 4a.
Top storage bin 4c is positioned at the top of denitration chamber 4b, the top of denitration chamber 4b is provided with 4 blanking funnel 4n, the upper end of blanking funnel 4n is communicated with top storage bin 4c, the lower ending opening of blanking funnel 4n is positioned at the top of denitration chamber 4b, so that the active carbon in the storage bin 4c of top can be in blanking funnel 4n enters denitration chamber 4b.Top storage tank 4s is positioned at top storage bin 4c top, and is communicated with top storage bin 4c.Bottom discharge tank 4k is positioned at storage bin 4l below, bottom, and is communicated with bottom storage bin 4l, and top storage tank 4s is connected with the charging aperture of adsorption tower, and bottom discharge tank 4k is connected with the discharging opening of adsorption tower.In the bottom of the 4e of bottom compartment, offer gas approach 4d, entering on the 4g of ammonia chamber to offer ammonia injection apparatus, top at denitration chamber 4b offers exhanst gas outlet 4i, and gas approach 4d is communicated with the air inlet of adsorption tower 4, and exhanst gas outlet 4i is communicated with the gas outlet of adsorption tower 4.
Flue gas is in flue-gas-cooling system is adjusted to adsorption tower after optimum treatmenting temperature scope, by air inlet, enter the gas approach 4d of adsorption tower 4 interior adsorption modules, at the 4e of bottom compartment, by the upper bucket of 4 the second air inlet doffer 4f that are evenly distributed and the gap between lower bucket, deliver to the desulfurization layer of desulfurization chamber 4a.The time stopping at desulfurization layer is according to some difference of the proterties of flue gas, best is that 0.2-0.3m/sec and inlet gas concentration are while being 150-220ppm through flow velocity, need the 4-7 time of staying of second, when inlet gas concentration is greater than 150-220ppm, the time of staying that need to be longer, if while surpassing this flow velocity 0.2-0.3m/sec, the dust of active carbon itself can disperse and be mixed in flue gas, the flue gas of meeting removing pollutant, in addition, flow velocity increase can cause the differential pressure of active carbon layer to increase.At desulfurization layer, by the adsorption function of active carbon or activated coke, remove the pollution sources such as oxysulfide, tribute, bioxin/furans.
Flue gas from desulfurization layer out after, the denitration floor that enters denitration chamber 4b through the first air inlet doffer 4h, is removed nitrogen oxide by catalysis by active carbon.Specifically, flue gas from desulfurization layer out, module enter ammonia chamber 4g in mix with ammonia, then enter the bottom of denitration layer.Ammonia is to discharge from ammonia storage tank 4w with gaseous state, in atomizer 4x, carry out heat exchange and heat up with steam, then the outer gas phase heating up with another kind of mode in blender 4x ' is mixed mutually, and then the ammonia chamber 4g that enters in module mixes with flue gas by the ejection of ammonia injection apparatus is rear.The spray flux of ammonia is decided by the equivalent proportion of ammonia and nitrogen oxide, does not have the residue ammonia that can induce reaction with nitrogen oxide to regulate, in order to avoid surpass the standard value in environment permissible range.The time stopping at denitration layer is according to some difference of the proterties of flue gas, and best is 0.2-0.3m/sec and inlet gas concentration while being 150-220ppm through flow velocity, needs the 6-9 time of staying of second, when inlet gas concentration is greater than 150-220ppm, and the time of staying that need to be longer.In the 4b of denitration chamber, the nitrogen oxide in flue gas produces chemical reaction with ammonia selectively by the catalysis of active carbon, and resolves into water and nitrogen (N 2), then together pass through the exhanst gas outlet of adsorption module with the flue gas purifying, then by adsorption tower gas outlet, discharged, finally flow to chimney 7.
In order to improve the operating efficiency of adsorption tower 4, with respect to the adsorption tower 4 of above-described embodiment, do following improvement.In the present embodiment, adsorption tower 4 comprises absorption module and support, absorption module comprises two adsorption module groups, 1 top storage tank 4s and 4 bottom discharge tank 4k, adsorption module group comprises 4 adsorption modules, 4 adsorption modules are divided into two-layer up and down, 2 every layer, the adsorption module adjacent with layer is fixedly connected with left and right between any two, between upper and lower two-layer adsorption module, be also fixedly connected with, shown in Fig. 3 b, the bottom of two adsorption modules of lower floor is connected with support with at least 1 movable part (being 5 movable parts in the present embodiment) by a fixture, movable part 31 is positioned at the surrounding of fixture 30, fixture 30 forms a fixed connection a little, movable part 31 forms and is flexibly connected point, two parts up and down of movable part can relatively move on horizontal plane, in the present embodiment, fixture is bolt, movable part is lower plate, pillar and ball bearing, lower plate is fixedly mounted on the upper surface of support, pillar is fixedly mounted on the bottom of the adsorption module that is positioned at below, and be positioned at the top of lower plate, ball bearing is equipped with roll mode in pillar lower end, ball bearing is pressed on the upper surface of lower plate.Shown in figure 2, the top storage bin 4c of each adsorption module is all connected with four discharging openings of 1 tripper 4j by 4 the second top fed pipe 4m, each tripper 4j is all connected with top storage tank 4s by 1 the first top fed pipe 4t, described in each the bottom storage bin 4l of adsorption module all logical charge tube be connected with bottom discharge tank 4k.
As shown in Figure 3 a, when processing a large amount of flue gas, normally 6m is wide, 6m long for the size of single-bit module, and maximum is also that 7.2m is wide, and 7.2m is long, adsorption tower comprises two of left and right absorption module, if absorption module is two, consider thermal expansion when above, should leave suitable interval, therefore, in the present embodiment, between two absorption modules, there is certain interval.Each absorption module includes two adsorption module groups, and namely an adsorption tower includes 16 adsorption modules.Before and after two adsorption module groups, arrange, air inlet pipe 4q and escape pipe 4r are set between two adsorption module groups, one end of air inlet pipe 4q is connected with the air inlet of adsorption tower, the other end of air inlet pipe 4q is connected with the gas approach 4d of each adsorption module, one end of escape pipe 4r is connected with the exhanst gas outlet 4i of each adsorption module, and the other end of escape pipe 4r is communicated with the gas outlet of adsorption tower 4.By two storage tanks are only set on adsorption tower, have greatly reduced like this each module and had indivedual regulative modes of storage tank (" module, a storage tank ") separately in the hidden danger of machinery, operating aspect.And the bifurcated of active carbon material feeding pipeline and conveying equipment and distributor become simpler, distance becomes the shortest.Three-temperature sensor is all installed in each adsorption module.On the gas approach 4d of each adsorption module and exhanst gas outlet 4i, be separately installed with indivedual baffle plate C and indivedual baffle plate D, the upper end of the lower end of indivedual baffle plate C and indivedual baffle plate D is all hinged on the sidewall of adsorption module.The top of indivedual baffle plate C is connected with the piston rod of a cylinder G by linkage, and cylinder G drives indivedual baffle plate C to rotate around hinging pin shaft by linkage, opens or seal gas approach 4d; The bottom of indivedual baffle plate D is also connected with the piston rod of another cylinder G by linkage, and another cylinder G drives indivedual baffle plate D to rotate around hinging pin shaft by linkage, opens or seal exhanst gas outlet 4i.The linkage that connects indivedual baffle plate C and D in the present embodiment is the connecting rod of an approximate V-arrangement, the middle part of connecting rod is hinged on the sidewall of the adsorption module below indivedual baffle plate C or indivedual baffle plate D, the upper end of connecting rod is connected with the top of indivedual baffle plate C or indivedual baffle plate D, and the lower end of connecting rod is hinged with the piston rod of corresponding cylinder G.
Adsorption module is due to structure and the loading of filling the active carbon in it is subject to vertically, the impact of horizontal loading, during running, the temperature of flue gas makes its inside usually maintain the temperature conditions of 120-150 ℃, therefore need to think about the impact of loading and thermal expansion, then using optimal module number as its base unit.In the present embodiment with 8 adsorption modules, the absorption module of take is base unit, between the absorption module of two of left and right, leave expansion joint space, by expansion joint, the air inlet pipe of two absorption modules is connected with escape pipe, and the bottom of adsorption module is connected with support with five movable parts by a fixture, above-mentioned thermal expansion is dropped to minimum on the impact of adsorption tower mechanical performance, when emergency occurs, (when " focus " occurs) guarantees the absolute construction that other adsorption towers are immune.
For fear of interrupting the running of whole system while there is hidden danger adsorption tower is inner, after taking measures and dealing with problems, the more inefficient method restarting, the utility model takes following method so that whole system can remain the mode of normal operation.The steps include: adsorption module to be detected when abnormal when three-temperature sensor, report to the police and pass to central control room with abnormal symbol, after " focus " situation is confirmed, immediately indivedual baffle plate D of indivedual baffle plate C of the gas approach of abnormal adsorption module and exhanst gas outlet are turned off simultaneously.As shown in accompanying drawing 4a, 4b, 5a, 5b, indivedual baffle plate C of module, D is usually respectively arranged on the upper and lower end of import and outlet, it during normal operation, is the state of opening, but, as emergency occurs, by the cylinder G that controls indivedual baffle plates, start indivedual baffle plates, peristome is closed and is sealed flue gas turnover, to cut off the air-flow that flows to inside modules.In addition, abnormal interruption adsorption module is to the charging of active carbon and discharging.Other all adsorption modules are but still running well, specifically, under the state of normally opening at indivedual baffle plates, flue gas proper flow, the charging of active carbon and discharging are also very normal.With flue gas turnover in upper module, be interrupted, but kindling material likely continues oxidation, therefore need nitrogen injection, stop the expansion of " focus ", and the process of monitor temperature decline.Through having determined after confirmation that temperature in abnormal adsorption module has dropped to normal range (NR) and " focus " gone out to the greatest extent, indivedual baffle plate C of the adsorption module that this is abnormal, the state that the movement of D and active carbon will be in closing/interrupting, stops injecting nitrogen.Abnormal module will be confirmed by maintenance of equipment or during factory day-off, and take adequate measures to be restored to the original state later.
The bottom discharge tank 4k of adsorption tower 4 is connected with the charging aperture of active device 5, the discharging opening of active device 5 is connected with the charging aperture of regenerator 6, the discharging opening of regenerator 6 is connected with the top storage tank 4s of adsorption tower 4, active device 5 comprises housing, transfer device and additive shower, additive shower is fixedly mounted in housing, and additive shower is positioned at the top of transfer device, active carbon is from the charging aperture of active device 5 enters, by transfer device (as belt conveyor), be transplanted on the discharging opening of active device 5, in this process, additive shower is to spraying agent on active carbon, the medicament of additive shower spray is urea compounds.The discharging opening of fresh active carbon storage bin 4o is communicated with the charging aperture of regenerator 6.
The active carbon of discharging from adsorption module is processed through regeneration to regenerator 6, and the pollution sources such as oxysulfide, tribute and bioxin/furans that are adsorbed on active carbon become concentrated gas; Oxysulfide is made business sulfuric acid in sulfuric acid manufacturing equipment 6f, and other pollution sources are processed in sewage treatment equipment.Bioxin in regenerating active carbon process, high temperature in regenerator (400-450 ℃) and no oxygen (O 2) condition under decompose completely, eliminate.
Active carbon through regenerating in regenerator 6, its most pollution sources have been resolved and have decomposed, conventionally the micropollution source less than 1wt% remains in wherein, discharging opening place at regenerator 6 arranges sieve 6e, thereby the active carbon size after assurance regeneration is just transported in adsorption tower 4 and re-uses more than maintaining 2.8mm.The dust arrester 4u that the active carbon of regeneration and new active carbon together arrange by adsorption tower top is housed in the storage tank 4s of top after removing fine dust.Active carbon moves down against gravity from top storage tank along the pipeline being connected with top storage bin 4c, action by switch baffle plate on pipeline and pipeline remains airtight successively, and then the second top fed pipe 4m via module top enters in the storage bin 4c of top.Be contained in after the active carbon material feeding in the storage bin of top, at denitration chamber 4b, by catalysis, carry out denitration (denitrogenation), at desulfurization chamber 4a, by adsorption function, carry out desulfurization, in these denitrations and sweetening process, active carbon suitably stays for some time, and then in order to regenerate, from the desulfurization chamber 4a of module, discharges.Active carbon temporarily leaves in bottom storage bin 4l and bottom discharge tank 4k after discharging from desulfurization chamber 4a according to the time of programming on time, then with carrying equipment, discharges.
Active carbon after active device 5 sprays and the fresh active carbon of supplying from fresh active carbon storage bin 4o are together delivered to regenerator 6, in order to regenerate, from top through heating zone 6a temperature, raise, and start to resolve when temperature surpasses 300 ℃.Heating zone temperature be raised to 400-450 ℃ and from active carbon, resolve, decompose the concentrated sulfur dioxide of formation, together through degas zone 6b, be delivered to sulfuric acid manufacturing equipment 6f with other resolved pollution sources.Active carbon completes after parsing in degas zone, move down into bottom coohng district 6c, the outer gas of being introduced by pressure fan carries out cooling, in addition gas is obtained thermal source and is heated up by heat exchange in the process of cooling active carbon, about 200-250 ℃, be heated to again 500-600 ℃ in heat riser 6d after, move on to heating zone 6a, the temperature of active carbon is raise, finally from regenerator, deliver to atmosphere.Active carbon is from regenerator is discharged, and through the 6e that sifts out, the active carbon that is only greater than 2.8mm enters in adsorption tower again, the active carbon micro mist leaching or other collection of granule less than 2.8mm, re-uses from sieve.According to the amounts of activated carbon from system filtering, from fresh active carbon storage bin 4o, supply the fresh active carbon of same amount.
Active carbon in adsorption module is as the medium of removing pollution sources in flue gas, need to form benign cycle, in other words, in adsorption tower, by round and smooth discharging and charging, the pollution sources in adsorption tower are extracted out and regenerated rapidly, then the active carbon of regeneration is fed intake again, and the active carbon of discharging in adsorption tower is when stop, for fear of phenomenons such as dewfall and corrosion, occur, the discharge rate of active carbon and internal circulating load, with iron-smelter sinter fume sulphur oxide concentration, 220ppm is as the criterion, and comparing with the active carbon total amount of whole module should be within the scope of 0.15-0.2wt%; Active carbon is carried the maximum machine ability of equipment, and comparing with active carbon total amount should be within the scope of 0.3 – 0.4wt%; Sulfoxide concentration is higher, and the machine capability of internal circulating load and conveying equipment should be improved accordingly.Active carbon is under the state of the pollution sources such as absorption oxysulfide, when stopping for a long time in adsorption tower 4, regenerator 6 and other storage tanks, for fear of occurring in phenomenons such as the following dewfall/corrosion of acid dew point, heater, insulation are taked to and/or with measures such as nitrogen fillings in the outside of container, reduce and the contacting of oxygen.Active carbon has high abrasiveness, for fear of the mechanical wear generation of carrying equipment activated carbon granule to be pulverized completely or weakened, should select friction can be dropped to minimum equipment.Conventionally to use the low abrasiveness such as bucket conveyor, flexible rubber conveyer belt to carry equipment.When carrying active carbon, likely there is hidden danger in forward and backward technique, therefore the surge tank of suitable capacity need to be installed to pooling feature can be provided; Active carbon and be attracted to pollution sources wherein in adsorption tower 4, regenerator 6 and other storage tanks during long-term stop, takes heater, insulation and/or with measures such as nitrogen fillings, in order to avoid in phenomenon generations such as the following dewfall/corrosion of acid dew point to container.
For fear of the active carbon circulating, reduce the performance of system, for active carbon can be brought into play absorption and catalysis smoothly, the micro mist, the size that because of mechanical wear and chemical erosion, produce need to be removed from system less than the active carbons unnecessary or that de-orbit such as activated carbon granule of 2.8mm, therefore, dust pelletizing system need to be set.Dust pelletizing system of the present utility model comprises first, second, third dust arrester 4v/4u/6h and the second sack cleaner, the first dust arrester 4v is arranged between active device 5 and adsorption tower 4, the second dust arrester 4u is arranged on the charging aperture of adsorption tower, and the 3rd dust arrester 6h is arranged on the charging aperture place of regenerator 6.Shown in Fig. 6, first, second, third dust arrester includes tubular shell 41, air inlet 42, charging aperture 43, gas outlet 44 and discharging opening 45, air inlet is opened in the bottom of housing 41, gas outlet 44 is opened in the top of housing 41, discharging opening 45 is opened in the bottom of housing 41, feed pipe 43 is arranged on the top of housing 41, and the discharging opening of feed pipe 43 is communicated with housing 41 inner chambers.The charging aperture of the feed pipe of the first deduster 4v is connected with the bottom discharge tank 4k of adsorption tower 4, and discharging opening 45 is connected with the charging aperture of active device 5.The gas outlet of each dust arrester is all connected with the second sack cleaner by blower fan, and air inlet is all communicated with ambient atmosphere.Dust pelletizing system also comprises some dust shields, and dust shield is arranged on the top of conveying track, and conveying track is the track of Transport Activity charcoal or activated coke, and dust shield is connected with sack cleaner by pipeline.
As shown in Figure 6, the opposite direction that the direction that the gas b of dust arrester China and foreign countries introduces and active carbon a fall, the outer gas of consequent active carbon flying dust and introducing together moves along pipeline, delivers in the second sack cleaner.For fear of dust, when carrying, overstock on transfer pipeline, need deduster to carry by force with speed more than about 20m/sec with other pressure fans.
At the delivery track of active carbon often by active carbon dust bulk deposition, need to be by its suction trapping before floating dust precipitation.As shown in Figure 7, be contained in the dust that the active carbon d in the active carbon bucket of top produces in movement, and the flying dust between empty bucket e, after the dust shield f trapping by track top, by flue, g carries, and finally delivers to control of dust with processing in sack cleaner.And, to carry at a high speed, so as not on pipeline dust accumulation.After pollution sources being removed in regenerator less than the activated carbon granule of 2.8mm, by sieve, collect and re-use as fuel.Depart from micro mist and the activated carbon granule of carrying equipment, conventionally by carrying built-in dust shield on the conveying track of equipping to collect, if its collection rate is low and effect is very little, separately establish vacuum handling equipment and pipeline, to can collect if desired micro mist and the activated carbon granule of many places.
The active carbon that the utility model is used is to be, after brown coal 80% and bituminous coal 20% coordinate with tar (pitch), through charing, to process by percentage by weight, finally through activation processing, makes.Certainly, the utility model also can be used other active carbons or activated coke.
Existing active carbon, active carbon of the present utility model and the active carbon of the present utility model after chemokinesis have been carried out to the test to oxysulfide adsorption capacity, and measured the oxysulfide being adsorbed in active carbon.Result of the test is presented in accompanying drawing 9.The active carbon of the present utility model activating after chemical addition agent sprays is stronger than other two kinds of active carbons to the adsorption capacity of oxysulfide.After it should be noted that active carbon of the present utility model activates, in absorption and parsing circulation repeatedly, its oxysulfide adsorption capacity remains well, never goes down.This result of the test shows, the active carbon using in flue gas purification system its machinery and chemical characteristic in circulation technology are repeatedly faded.Active carbon of the present utility model after chemokinesis will improve following functions: improve SWC(desulfurization load factor); By keeping chemical group, reduce active carbon wearing and tearing; Avoid the inner clogging of adsorption tower to occur; In the denitrification process of adsorption tower, reduce ammonia consumption.
Above-described embodiment is described preferred embodiment of the present utility model; not scope of the present utility model is limited; do not departing under the prerequisite of the utility model design spirit; various distortion and improvement that those of ordinary skills make the technical solution of the utility model, all should fall in the definite protection domain of the utility model claims.

Claims (15)

1. a flue gas purification system, comprise preprocessing system and adsorption tower, flue gas is cleaned after preprocessing system enters adsorption tower (4) by pipeline, it is characterized in that: also comprise flue-gas-cooling system, described flue-gas-cooling system is arranged on the pipeline between preprocessing system and adsorption tower, described flue-gas-cooling system comprises gas cooler (3), outer gas diluter (2c), the first temperature sensor (11) and the second temperature sensor (12), the first fume pipe (13) is the pipeline between preprocessing system and adsorption tower, one end of described the first fume pipe (13) is fixedly mounted on the air inlet of adsorption tower (4), on the air inlet of described adsorption tower (4), air inlet baffle plate is installed, the other end of the first fume pipe (13) is connected with preprocessing system, described outer gas diluter (2c) is arranged on the first fume pipe (13), described gas cooler (3) is also arranged on the first fume pipe (13), and gas cooler (3) is positioned between outer gas diluter (2c) and adsorption tower (4), described the first temperature sensor (11) and the second temperature sensor (12) are all installed on the first fume pipe (13), and the first temperature sensor (11) is positioned between outer gas diluter (2c) and gas cooler (3), the second temperature sensor (12) is positioned between gas cooler (3) and adsorption tower (4), on the outer gas air inlet of described outer gas diluter (2c), be provided with can adjusting air inflow quantity baffle plate.
2. flue gas purification system according to claim 1, it is characterized in that: described preprocessing system comprises electrostatic precipitator (1) and the first sack cleaner (2), described the first fume pipe (13) is connected with the outlet of the first sack cleaner (2), the import of described electrostatic precipitator (1) is connected with fume emission mouth, the gas outlet of described adsorption tower (4) is communicated with chimney (7), described flue gas purification system also comprises the second fume pipe (2e), one end of described the second fume pipe (2e) is connected on the pre-treatment fume pipe between electrostatic precipitator (1) and the first sack cleaner (2), the other end of described the second fume pipe (2e) is connected with chimney (7), on described the second fume pipe (2e), master shield is installed, on described the first fume pipe (13), master shield is also installed, master shield on described the first fume pipe (13) is positioned at outer gas diluter (2c) and pre-treatment fume pipe and the second fume pipe (13, 2e) between junction.
3. flue gas purification system according to claim 2, it is characterized in that: described gas cooler (3) comprises housing and shower, the upper end of described housing offers air inlet, the lower end of housing offers gas outlet, described shower is arranged in housing, and some nozzles are installed on described shower, and the outlet of described nozzle all down, described nozzle can spray water droplet and compressed-air actuated mixture, and the diameter of described water droplet is less than 60 microns.
4. flue gas purification system according to claim 3, is characterized in that: also comprise three-temperature sensor, described three-temperature sensor is arranged in adsorption tower (4).
5. flue gas purification system according to claim 1, is characterized in that:
Described adsorption tower (4) comprises at least one adsorption module, at least one top storage tank (4s) and at least one bottom discharge tank (4k), described each adsorption module includes top storage bin (4c), denitration chamber (4b), desulfurization chamber (4a) and bottom storage bin (4l), described denitration chamber (4b) is positioned at desulfurization chamber (4a) top, between described denitration chamber (4b) and desulfurization chamber (4a), be provided with into ammonia chamber (4g), the bottom of entering ammonia chamber (4g) is connected with the top of desulfurization chamber (4a), describedly enter in ammonia chamber (4g) to be provided with at least one first air inlet doffer (4h), between described denitration chamber (4b) and desulfurization chamber (4a), by the first air inlet doffer (4h), be communicated with, described the first air inlet doffer (4h) comprises bucket (4h1), lower bucket (4h2) and tube connector (4h3), described upper bucket (4h1) and lower bucket (4h2) be big up and small down infundibulate all, the upper end open of described upper bucket (4h1) is communicated with the bottom of denitration chamber (4b), described lower bucket (4h2) is sleeved on bucket (4h1), between lower bucket (4h2) and upper bucket (4h1), be provided with gap, the lower ending opening of lower bucket (4h2) is communicated with the upper end of tube connector (4h3), the lower end of tube connector (4h3) is communicated with the top of desulfurization chamber (4a), described bottom storage bin (4l) is positioned at desulfurization chamber (4a) below, between described bottom storage bin (4l) and desulfurization chamber (4a), be provided with bottom compartment (4e), in described bottom compartment (4e), be provided with at least one second air inlet doffer (4f), described the second air inlet doffer (4f) is identical with the first air inlet doffer (4h) structure, between described bottom storage bin (4l) and desulfurization chamber (4a), by the second air inlet doffer (4f), be communicated with, the upper end open of the upper bucket of described the second air inlet doffer (4f) is communicated with the bottom of desulfurization chamber (4a), the lower end of the tube connector of the second air inlet doffer (4f) is communicated with bottom storage bin (4l), described top storage bin (4c) is positioned at the top of denitration chamber (4b), the top of described denitration chamber (4b) is provided with at least one blanking funnel (4n), the upper end of described blanking funnel (4n) is communicated with top storage bin (4c), the lower ending opening of blanking funnel (4n) is positioned at the top of denitration chamber (4b), described top storage tank (4s) is positioned at top storage bin (4c) top, and be communicated with top storage bin (4c), described bottom discharge tank (4k) is positioned at bottom storage bin (4l) below, and be communicated with bottom storage bin (4l), described top storage tank (4s) is connected with the charging aperture of adsorption tower, described bottom discharge tank (4k) is connected with the discharging opening of adsorption tower, in the bottom of described bottom compartment (4e), offer gas approach (4d), described, enter on ammonia chamber (4g) to offer ammonia injection apparatus, at the top of denitration chamber (4b), offer exhanst gas outlet (4i), described gas approach (4d) is communicated with the air inlet of adsorption tower (4), described exhanst gas outlet (4i) is communicated with the gas outlet of adsorption tower (4).
6. flue gas purification system according to claim 5, it is characterized in that: described adsorption tower (4) comprises absorption module and support, described absorption module comprises at least one adsorption module group, at least 1 top storage tank (4s) and at least 1 bottom discharge tank (4k), described adsorption module group comprises 4 adsorption modules, 4 adsorption modules are divided into two-layer up and down, 2 every layer, the adsorption module adjacent with layer is fixedly connected with left and right between any two, between upper and lower two-layer adsorption module, be also fixedly connected with, the bottom of two adsorption modules of lower floor is connected with support with at least 1 movable part by a fixture, described movable part is positioned at the surrounding of fixture, fixture forms a fixed connection a little, movable part forms and is flexibly connected point, two parts up and down of described movable part can relatively move on horizontal plane, described in each, the top storage bin (4c) of adsorption module is all connected with four discharging openings of 1 tripper (4j) by 4 the second top fed pipes (4m), each tripper (4j) charging aperture is all connected with top storage tank (4s) by 1 the first top fed pipe (4t), described in each the bottom storage bin (4l) of adsorption module all logical charge tube be connected with bottom discharge tank (4k).
7. flue gas purification system according to claim 6, it is characterized in that: described absorption module comprises two adsorption module groups, before and after two adsorption module groups, arrange, air inlet pipe (4q) and escape pipe (4r) are set between two adsorption module groups, one end of described air inlet pipe (4q) is connected with the air inlet of adsorption tower, the other end of air inlet pipe (4q) is connected with the gas approach (4d) of each adsorption module, one end of described escape pipe (4r) is connected with the exhanst gas outlet (4i) of each adsorption module, the other end of described escape pipe (4r) is communicated with the gas outlet of adsorption tower (4).
8. flue gas purification system according to claim 7, is characterized in that: when described absorption module is when more than two, absorption module between any two left and right is arranged side by side, and has gap between two between adjacent absorption module.
9. flue gas purification system according to claim 8, it is characterized in that: also comprise regenerator (6) and active device (5), the bottom discharge tank (4k) of described adsorption tower (4) is connected with the charging aperture of active device (5), the discharging opening of described active device (5) is connected with the charging aperture of regenerator (6), the discharging opening of described regenerator (6) is connected with the top storage tank (4s) of adsorption tower (4), described active device (5) comprises housing, transfer device and additive shower, described additive shower is positioned at the top of transfer device, the medicament of described additive shower spray is urea compounds.
10. flue gas purification system according to claim 9, is characterized in that: also comprise fresh active carbon storage bin (4o), the discharging opening of described fresh active carbon storage bin (4o) is communicated with the charging aperture of regenerator (6).
11. flue gas purification systems according to claim 10, it is characterized in that: also comprise dust pelletizing system, described dust pelletizing system comprises first, second, the 3rd dust arrester (4v, 4u, 6h) He the second sack cleaner, described the first dust arrester (4v) is arranged between active device (5) and adsorption tower (4), described the second dust arrester (4u) is arranged on the charging aperture of adsorption tower, described the 3rd dust arrester (6h) is arranged on the charging aperture place of regenerator (6), described first, second, the 3rd dust arrester (4v, 4u, 6h) structure is identical, include tubular shell (41), air inlet (42), feed pipe (43), gas outlet (44) and discharging opening (45), described air inlet is opened in the bottom of housing (41), gas outlet (44) is opened in the top of housing (41), discharging opening (45) is opened in the bottom of housing (41), feed pipe (43) is arranged on the top of housing (41), the discharging opening of feed pipe (43) is communicated with housing (41) inner chamber, the charging aperture of described feed pipe (43) is connected with the bottom discharge tank (4k) of adsorption tower (4), described discharging opening (45) is connected with the charging aperture of active device (5), described gas outlet (44) is connected with the second sack cleaner by blower fan, described air inlet (42) is communicated with ambient atmosphere.
12. flue gas purification systems according to claim 11, it is characterized in that: described dust pelletizing system also comprises some dust shields, described dust shield is arranged on the top of conveying track, described conveying track is the track of Transport Activity charcoal or activated coke, and described dust shield is connected with described the second sack cleaner by pipeline.
13. flue gas purification systems according to claim 12, it is characterized in that: described preprocessing system comprises electrostatic precipitator and the first sack cleaner (2), described electrostatic precipitator (1) is one-time dedusting device, and the first sack cleaner (2) is final dusting device.
14. flue gas purification systems according to claim 13, is characterized in that: the flow velocity of the interior smoke gas flow of described adsorption tower (4) through desulfurization chamber and denitration chamber is 0.2-0.3m/sec.
15. flue gas purification systems according to claim 7, it is characterized in that: on the gas approach of described adsorption module (4d) and exhanst gas outlet (4i), be separately installed with indivedual baffle plate C and indivedual baffle plate D, the upper end of the lower end of indivedual baffle plate C and indivedual baffle plate D is all hinged on the sidewall of adsorption module, the top of described indivedual baffle plate C is connected with the piston rod of a cylinder G by linkage, described cylinder G can drive indivedual baffle plate C sealing gas approach (4d), the bottom of indivedual baffle plate D is also connected with the piston rod of another cylinder G by linkage, another cylinder G can drive indivedual baffle plate D sealing exhanst gas outlets (4i).
CN201320390689.4U 2013-07-02 2013-07-02 Flue gas purification system Withdrawn - After Issue CN203400612U (en)

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103446830A (en) * 2013-07-02 2013-12-18 香港诺曼泰壹环保科技有限公司 Flue gas purifying system
CN104289067A (en) * 2014-10-20 2015-01-21 江苏维尔思环境工程有限公司 Desulfurization, denitrification and dust removing device
CN105276999A (en) * 2014-05-30 2016-01-27 宝山钢铁股份有限公司 Sintering flue gas waste heat utilization and deep purification method and system thereof
CN110115925A (en) * 2018-02-06 2019-08-13 中国石化工程建设有限公司 A kind of process and device reducing activated coke adsorption column inlet flue-gas temperature
CN110339657A (en) * 2018-04-03 2019-10-18 中国石化工程建设有限公司 A kind of regeneration fume from catalytic cracking dry purification process and device
CN108480042B (en) * 2018-03-08 2021-01-26 马鞍山钢铁股份有限公司 Flue gas dust removal device and dust removal process thereof

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103446830A (en) * 2013-07-02 2013-12-18 香港诺曼泰壹环保科技有限公司 Flue gas purifying system
CN103446830B (en) * 2013-07-02 2015-07-01 香港诺曼泰壹环保科技有限公司 Flue gas purifying system
CN105276999A (en) * 2014-05-30 2016-01-27 宝山钢铁股份有限公司 Sintering flue gas waste heat utilization and deep purification method and system thereof
CN104289067A (en) * 2014-10-20 2015-01-21 江苏维尔思环境工程有限公司 Desulfurization, denitrification and dust removing device
CN104289067B (en) * 2014-10-20 2016-04-20 江苏维尔思环境工程有限公司 Desulfurization removing nitric cleaner
CN110115925A (en) * 2018-02-06 2019-08-13 中国石化工程建设有限公司 A kind of process and device reducing activated coke adsorption column inlet flue-gas temperature
CN108480042B (en) * 2018-03-08 2021-01-26 马鞍山钢铁股份有限公司 Flue gas dust removal device and dust removal process thereof
CN110339657A (en) * 2018-04-03 2019-10-18 中国石化工程建设有限公司 A kind of regeneration fume from catalytic cracking dry purification process and device

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