CN105688626B - Flue gas desulfurization and denitration method including flue gas temperature control and device - Google Patents

Flue gas desulfurization and denitration method including flue gas temperature control and device Download PDF

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CN105688626B
CN105688626B CN201410710435.5A CN201410710435A CN105688626B CN 105688626 B CN105688626 B CN 105688626B CN 201410710435 A CN201410710435 A CN 201410710435A CN 105688626 B CN105688626 B CN 105688626B
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ammonia
spiral
air
pipeline
baffle plate
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CN201410710435.5A
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CN105688626A (en
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魏进超
叶恒棣
张震
孙英
刘昌齐
李俊华
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中冶长天国际工程有限责任公司
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Abstract

A kind of flue gas desulfurization and denitration method in activated carbon adsorber and device including flue gas temperature control are provided, this approach includes the following steps:I) the step of flue gas temperature control, it includes following sub-step:(1) first at the cold air inlet of the upstream position (P1) for the flue for conveying high-temperature flue gas to activated carbon adsorber, first time cooling is carried out to flue gas by being passed through cold air into the flue, (2) and then in the flue gas at the technique (operating) water nozzle of the downstream position (P2) for the position (P1) for being passed through cold air into flue cooling water or cold mist are sprayed into, the T3 for entering the flue-gas temperature of adsorption tower in setting is adjustedSettingIn range, such as T3SettingIn 105-150 DEG C of range;With II) desulphurization and denitration step.It is controlled into the flue-gas temperature in adsorption tower using cold wind, water spray is converted.

Description

Flue gas desulfurization and denitration method including flue gas temperature control and device

Technical field

The present invention relates to the flue gas desulfurization using activated carbon adsorber, method of denitration, it is more particularly related to The upstream or front end of activated carbon adsorber are to flue gas (sintering flue gas) while using spray cooling and converting the measure of cold wind cooling The flue-gas temperature into adsorption tower is controlled in 100~150 DEG C of ranges, the method for being preferably controlled in 120~140 DEG C of ranges, this Belong to sintering flue gas process field.

Background technology

For industrial smoke, the especially sintering device flue gas of steel and iron industry, using including activated carbon adsorber and parsing Large-scale dry desulfurization, denitrification apparatus and the technique of tower are more satisfactory.Activated carbon flue gases purification has and can take off simultaneously By-product resource, the features such as adsorbent can be recycled, denitrification efficiency is high, are realized in sulphur denitration, and right and wrong are often with there is development The desulfurization and denitrification integral technology of foreground.In the desulphurization and denitration device including activated carbon adsorber and Analytic Tower (or regenerator) In, activated carbon adsorber is used to from sintering flue gas or exhaust gas (the especially sintering flue gas of the sintering machine of steel and iron industry) absorption include sulphur Pollutant including oxide, nitrogen oxides and dioxin, and Analytic Tower is used for the hot recycling of activated carbon.

However, reaching tens meters of desulphurization denitration tower for height, the temperature of active carbon bed is controlled and is faced in adsorption tower Huge challenge.

For activated carbon method flue gases purification, the normal working temperature of active carbon bed is in activated carbon adsorber 100~160 DEG C, it is preferably controlled in 120~150 DEG C.

On the one hand, the activated carbon burning in bed in order to prevent, it is stringent control active carbon bed temperature less than 165 DEG C, it is excellent Choosing is less than 160 DEG C.This is because although the burning point of activated carbon at 430 DEG C or so, occurs chemical anti-in activated carbon surface It should be generally exothermic reaction, and containing a small amount of inflammable, combustion-supporting material in the dust in flue gas, and activated carbon itself is also carried secretly easily Combustion property dust.If without strictly controlling the temperature in adsorption tower, the presence of these flammable materials or inflammability dust with Shi Zaocheng security risks gently may then lead to activated carbon spontaneous combustion in tens meters of high adsorption towers, seriously then lead to dust explosion, this The appearance of two kinds of accidents is all catastrophic for large-scale desulphurization denitration tower apparatus.So for the sake of security, generally It is 165 DEG C that active carbon bed temperature alarming temperature, which is arranged,.The former flue gas temperature after booster fan pressurizes of sintering be generally 90 DEG C- 200 DEG C, be more generally that and oxygen content is high in sintering flue gas, bed temperature after activated carbon surface oxidation in tower between 100-180 DEG C Degree can be higher by 5-15 DEG C than input gas temperature, therefore in order to ensure the safe operation of desulfuring and denitrifying apparatus, need to inhale to entering The flue-gas temperature of attached tower is controlled, and the general alarm temperature that is arranged is 150 DEG C.In addition, before adsorption tower is stopped transport, it must keep living in tower Property charcoal bed temperature be less than 90 DEG C, need to cool down active carbon bed at this time, therefore in order to ensure stopping transport safely, also must Active carbon bed temperature is controlled.

On the other hand, need stringent control into the flue-gas temperature of adsorption tower when activated carbon flue gas purification system normal operation It is higher than or is not less than 100 DEG C, preferably higher than or not less than 110 DEG C.This is because if flue-gas temperature is less than 100 DEG C, enter The temperature of water vapour contained in sintering flue gas in bed easily becomes water and is aoxidized with sulphur close to dew point (or set point) Object reacts the acid for becoming strong corrosive, leads to the heavy corrosion of device and seriously reduces the effect of denitration, denitration.

Traditional flue gas cool-down method is the independent spray cooling into flue gas.This cooling means is in system normal operation Active carbon bed temperature can be effectively controlled, but smoke moisture can be caused excessively high for cooling before system shutdown, leads to activated carbon meeting A large amount of vapor in flue gas are adsorbed, activated carbon low-temperature denitration activity is reduced.

In general, activated carbon method flue gases purification has, desulphurization denitration rate is high, by-product resourcebility utilizes, activated carbon can The principle of the features such as recycling, desulphurization denitration are as follows:

In the surface SO of activated carbon2Sulfuric acid, reaction equation are formed by oxidative absorption:

2SO2+O2+2H2O→2H2SO4

If spraying into a small amount of ammonia in flue gas, SO can be accelerated2Absorption, reaction equation:

NH3+H2SO4→NH4HSO4

But it in order to achieve the effect that denitration while desulfurization, can generally be sprayed at adsorption tower smoke inlet more Ammonia, the ammonia needed for desulfurization should be met, while meeting the ammonia needed for denitration.Denitration reaction formula is:

4NO+O2+4NH3→4N2+6H2O

At the same time there is also side reactions below in reaction tower:

2NH3+H2SO4→(NH4)2SO4

And SO2With NH3Reaction rate ratio NO and NH3Reaction rate faster, SO2Presence inhibit denitration reaction Progress.In addition, the SO in flue gas3, HF and HCl also can and NH3Reaction, for denitration, these side reactions can increase greatly The dosage for having added ammonia, increases operating cost.

Invention content

The object of the present invention is to provide a kind of control methods of active carbon bed temperature, it can be ensured that system is running and stopping It realizes that safely and effectively temperature controls when fortune, prevents accident.In the upstream of activated carbon adsorber or front end to flue gas (sintering Flue gas) while using spray cooling and converting the measure of cold wind cooling to control the temperature of active carbon bed in adsorption tower 100 ~160 DEG C of ranges, the method for being preferably controlled in 120~150 DEG C of ranges.

Flue gas temperature control method used in this application uses simultaneously to carry out spray cooling to flue gas and converts cold wind to cool down. When adsorption tower works normally, if active carbon bed temperature is higher than 150 DEG C, set using before adsorption tower, after booster fan The injection point set, into former flue gas, penetrating atomized water cools down to flue gas, to reduce active carbon bed temperature.The work sprayed The amount of skill water is determined by exhaust gas volumn and flue-gas temperature.

Adsorption tower is normally stopped transport or (device is because of failure or safeguards and needs to shut down or water-cooling system failure in accident When), in order to reduce temperature in adsorption tower under conditions of not increasing humidity in tower, process water cooling system is closed, by former flue gas Flapper closure opens cold blast sliding valve, cold air is passed through into flue, to reduce active carbon bed temperature in adsorption tower.

In addition, the present invention also uses the means of the multidigit point injection Dilution air ammonia in activated carbon adsorber, its side Face is used to while taking into account the effect of desulfurization and denitration on the other hand also assist in the adjusting and/or control of temperature in adsorption tower. It can be said that the preferred scheme as the present invention, the flue-gas temperature in adsorption tower is controlled using the above means or measure, so as to It is adsorbed under ideal flue-gas temperature.

According to the first embodiment of the present invention, a kind of sintering flue gas desulfurization including flue gas temperature control, denitration side are provided Method, this approach includes the following steps:

I) the step of flue gas temperature control or the step of flue gas temperature adjustment, which includes following sub-step:

(1) lead at the cold air inlet of the upstream position P1 for the flue for conveying from high-temperature flue gas to activated carbon adsorber first It crosses into the flue and cold air is passed through to carry out first time cooling to flue gas,

(2) in the flue gas at the technique (operating) water nozzle of the downstream position P2 and then in the position P1 for being passed through cold air into flue Process water for cooling down sintering flue gas, i.e. cooling water or cold mist are sprayed into, enters the flue-gas temperature of adsorption tower to adjust and exists The T3 of settingSettingIn range, such as T3SettingAt 105-150 DEG C, preferably in 115-145 DEG C of range, more preferably at 120-140 DEG C Range;

II) desulphurization and denitration step:Pass through temperature control in the above 1) step or enters absorption through overregulating the flue gas of temperature One or more active carbon beds of adsorption tower, flue gas and the work being added from absorption tower top are flowed successively through after in the inlet plenum of tower Property charcoal carry out cross-current type contact, meanwhile, by dilute ammonia be passed through adsorption tower flue gas input channel neutralization be optionally passed through absorption In tower, the pollutant wherein contained by flue gas, the i.e. pollutant including oxysulfide, nitrogen oxides and dioxin are active Charcoal removes, and neat stress is entered in discharge chamber and is discharged later, has adsorbed the activated carbon of pollutant then from absorption tower bottom discharge;

III) activated carbon analyzing step:The activated carbon for having adsorbed pollutant is transferred to from the bottom of adsorption tower with top Heating zone and lower part cooling zone a kind of activated carbon Analytic Tower heating zone in, allow activated carbon to be parsed, be regenerated, and solve Activated carbon after analysis, regeneration is discharged after flowing down through cooling zone from desorption tower bottom;Wherein:Nitrogen is led in resolving Enter the top to Analytic Tower, and nitrogen is passed through to the lower part of Analytic Tower via the second nitrogen pipeline optionally together;Be passed through Nitrogen in Analytic Tower by from activated carbon thermal desorption include SO2And NH3Gas pollutant inside is from the heating zone of desorber It takes out of and is sent to acid making system i.e. relieving haperacidity area in centre portion between cooling zone and go relieving haperacidity.It is generated containing ammonia in relieving haperacidity area Waste water.

Preferably, in above step (1), in position, the first temperature measuring point and second is respectively set in the front side of P1 and rear side Temperature measuring point, flue-gas temperature T1 and T2 of the on-line measurement at the two temperature measuring points in flue, wherein in the mesh of the second temperature measuring point Scale value or setting value are T2SettingWherein T2SettingIt is the value within the scope of 150-180 DEG C, preferably 160-170 DEG C.

When actual measurement T1 is higher than T2SettingWhen value, start above-mentioned sub-step (1) and (2):According to T1 and T2SettingDifference carry out it is pre- It surveys and according to T2 and T2SettingDifference fed back the flow for carrying out cold wind in set-up procedure (1), so as to by T2 adjust or control exist T2Setting± a DEG C range, wherein a DEG C is at 2-10 DEG C.

When actual measurement T1 is less than T2SettingWhen value, cold blast sliding valve is closed in the operation for starting above-mentioned sub-step (2), stopping step (1) Door, only carries out follow-up step (2).

When system failure or orderly closedown, the supply of flue gas is cut off, only operates above-mentioned sub-step (1), and stop The only operation of sub-step (2), cold wind is passed through in adsorption tower.

Preferably, according to T1-T2SettingDifference △ T1, the flow of flue gas and the temperature of cold air be calculated and determined The flow of cold air in step (1) adjusts the aperture of cold wind valve, to which flue-gas temperature T2 is reduced to T2Setting± a DEG C model It encloses.

It may further be preferable that in above step (2), in position the downstream of P2, adsorption tower gas inlet it is upper Trip setting third temperature measuring point, the temperature T3 of on-line measurement flue gas in flue at third temperature measuring point, according to actual measurement T2 with the Desired value at three temperature measuring points or preset value T3SettingDifference carry out prediction and according to T3 and T3SettingDifference fed back to adjust T3 is adjusted or is controlled in T3 by the flow of whole spray technology waterSetting± b DEG C range, wherein T3SettingIt is preferably to exist at 100-150 DEG C 110-145 DEG C of range more preferably encloses interior value at 120-140 DEG C, and wherein b DEG C is at 2-10 DEG C.

Generally, T2SettingCompare T3SettingIt is 20-50 DEG C high, it is more preferably 25-45 DEG C high, it is more preferably 30-40 DEG C high.

Preferably, process water is or includes the ammonia-containing water from relieving haperacidity area.Including SO2And NH3(gas) pollution Object is transported in relieving haperacidity area after processing, obtains ammonia-containing water.By ammonia-containing water alternative techniques water or alternative techniques water A part.The NH in waste water can have both been utilized in this way3, reduce and be passed through pure NH in adsorption tower3The dosage of gas, and flue gas can be dropped Temperature, no waste water are arranged outside.

It may further be preferable that in step (II), dilution ammonia (i.e. Dilution air ammonia) is led to by ammonia and air Air is crossed with ammonia mixing arrangement (M) come what is obtained.

When adsorption tower is normally stopped transport or accident occurs for adsorbent equipment and/or water cooling plant (such as device is because of failure or dimension Shield needs to shut down or when water-cooling system failure), stop step (2) and spray water, while cutting off the supply of flue gas, only operating procedure (1) or starting step (1) (open cold blast sliding valve cold air is passed through into flue).Therefore the temperature of flue gas is reduced rapidly, in turn Reduce rapidly active carbon bed temperature in adsorption tower.So that it is guaranteed that the safety of adsorption tower is stopped transport, the generation of safety accident is avoided, with And avoid the destruction to equipment and the damage to activated carbon in adsorption tower bed.

Under normal circumstances, in normal operation, (1) into the flue of conveying high-temperature flue gas first by being passed through cold air To carry out first time cooling to flue gas, (2) and then sprays into process water (cooling water into flue gas in the downstream for being passed through cold air site Or cold mist) (such as water spray should be controlled so that the humidity of flue gas is less than 12wt%, is preferably shorter than 10wt%, is more preferable Less than 9wt%) reduce the temperature of flue gas.In addition, by into the flue gas entered in adsorption tower after entering in adsorption tower Dilution ammonia (i.e. Dilution air ammonia) is sprayed into, the temperature of flue gas in adsorption tower is also adjusted in lower degree.

When conveying come flue-gas temperature T1 it is higher, that is, be higher than T2SettingWhen, if relying on or being essentially relying in step (2) merely Water spray, which reduces flue-gas temperature, then can cause the humidity of flue gas higher, the subsequent adsorbtion operation in adsorption tower be influenced, at this point, should The intake of cold air (such as the air under environment temperature) is increased in above (1) step to reduce the temperature of flue gas, and Water spray in step (2) keeps relative stability.Thus it is ensured that into the flue gas in adsorption tower humidity and temperature it is opposite Stablize.

When the flue-gas temperature T1 that conveying comes is relatively low, that is, it is less than T2SettingWhen, then mainly or solely rely on spray in step (2) Cold water is greatly lowered the temperature of flue gas.In this way, remaining able to ensure the humidity for entering the flue gas in adsorption tower and temperature Stablize relatively.

When adsorption tower normally stops transport or accident occurs, (device is because of failure or safeguards and needs to shut down or water-cooling system failure When), in order to reduce temperature in adsorption tower under conditions of not increasing humidity in tower, stops step (2) water spray and (close process water Cooling system), while the supply (closing former gas baffle) of flue gas is cut off, only operating procedure (1) or starting step (1) (open cold blast sliding valve and be passed through cold air into flue), to reduce rapidly the temperature of flue gas, and then reduces rapidly in adsorption tower Active carbon bed temperature.So that it is guaranteed that the safety of adsorption tower is stopped transport, the generation of safety accident is avoided, and avoid breaking equipment The bad and damage to activated carbon in adsorption tower bed.

According to the second embodiment of the present invention, desulphurization and denitration device is provided or for the desulfurization, de- in above method Nitre device, it includes

1) adsorption tower,

2) flue is conveyed in the former flue gas of the flue gas input port upstream of adsorption tower, wherein being set on the upstream position P1 of flue There is cold air inlet, and be equipped with technique (operating) water nozzle on the downstream position P2 of flue,

3) air-cooler being connected with the cold air inlet on the positions P1,

4) the process water conveyance conduit being connected with the technique (operating) water nozzle on the positions P2, it is preferred that the process water conveys The other end for the ammonia-containing water basin or the process water conveyance conduit that the other end of pipeline is connected to relieving haperacidity area separates a branch And it is connected to the ammonia-containing water basin in relieving haperacidity area,

5) booster fan between the positions P1 and P2,

6) ammonia conveyance conduit 106, wherein:On the ammonia conveyance conduit (such as middle section position) be equipped with a kind of ammonia with The rear end of air mixing device (M), the ammonia conveyance conduit is respectively communicated to former flue gas conveying flue and/or extends to adsorption tower It is interior and be mounted with ammonia nozzle at its end, or multiple ammonia branches are separated from the latter end of the ammonia conveyance conduit, these Branch be respectively communicated to former flue gas conveying flue (102) and be optionally coupled to positioned at the air inlet of adsorption tower it is indoor one or Multiple ammonia nozzles in multiple ammonia nozzles and the optional clearance space between each active carbon bed of adsorption tower, and

7) desorber, it includes the heating zone on top and the cooling zone of lower part and positioned at middle area between the two.

Preferably, the first temperature measuring point and the second temperature measuring point is respectively set in the front-end and back-end of position P1.Preferably, In position the downstream of P2, adsorption tower gas inlet upstream be arranged third temperature measuring point.

Above-described ammonia and air mixing device (M) are to mix dress for the ammonia and air of activated carbon adsorber It sets, for obtaining dilution ammonia.

Preferably, above-described air-ammonia mixing arrangement (M) includes air pipeline, ammonia pipeline, air spiral Section, ammonia spiral section, mixing section and mixed gas outlet, wherein ammonia pipeline are inserted into from the side of the air pipeline of diameter bigger In (or extending into) air pipeline, then bends and extend a distance into (it L along airflow direction along air pipeline axis The e.g. 20-80% of mixing arrangement total length, more preferable 35-65%, such as L=0.2-2 meters, preferably 0.3-1.5 meters), ammonia The latter end of feed channel is ammonia spiral section, ammonia spiral section include the spiral plates institute that is longitudinally extended by the m in ammonia pipeline every The m spiral shape ammonia channel opened, in addition, air spiral section corresponding with ammonia spiral section include by between ammonia pipeline with The n volute type air channel that the n in the space spiral plates being longitudinally extended between air pipeline are separated, it is logical at both It is mixing section after the end in road, the end of mixing section is mixed gas outlet;Wherein:M=1-6 and n=1-8;With air spiral shell The hand of spiral for revolving section is opposite with the hand of spiral of ammonia spiral section.

In general, air spiral section and ammonia spiral section are concentric.

Preferably, m=1-4, n=1-6, more preferable m=2 or 3 and/or n=2,3,4 or 5.

Preferably, the mixing arrangement M further includes the first baffle plate and/or the second baffle plate being located in mixing section. Or the first baffle plate and/or the second baffle plate are equipped in mixing section.

Generally, the overall diameter of the ammonia pipeline is the 30-70% of the internal diameter of air pipeline, preferably 40-60%.

Preferably, the first baffle plate is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;With Two baffle plates are Circular plate structures, are placed within mixing duct, have gap to be mixed to allow between plectane excircle and mixing duct Gas passes through.

Preferably, the second baffle plate is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;First Baffle plate is Circular plate structure, is placed within mixing duct, has gap between plectane excircle and mixing duct to allow gaseous mixture Body passes through.

Preferably, the length of air spiral section is 0.7-2.8 times of the length of ammonia spiral section, preferably 0.8-2.5 times, More preferably 1-2.0 times, more preferable 1.2-1.8 times.

In addition, the length of mixing section is 0.4-1 times of the length of air spiral section, preferably 0.6-0.8 times.

Preferably, the first baffle plate and the second baffle plate as one group and repeat 2 to 3 groups of setting.Or, the first baffling Plate and the second baffle plate are arranged alternately and are respectively arranged 1-3, are preferably respectively arranged 2.

Air spiral section has the structure similar to spring or virtual spring with ammonia spiral section.The spiral of air spiral section The ratio between the respective screw pitch in spiral shape ammonia channel of shape air duct or ammonia spiral section and screw diameter (K/2R or k/2r) are 0.2-2:1, preferably 0.4-1.5:1, more preferable 0.6-1.0:1.

In the mixed process of air and ammonia, ammonia is passed into from ammonia entrance in device M, then passes through ammonia spiral Section.If ammonia is divided into stem portion in ammonia spiral section inlet, then along spiral tube runs, finally in ammonia spiral section Exit forms the ammonia air-flow of spiral.Air is passed into from air intake in the air pipeline of device, then passes through air spiral shell Revolve section.If being divided into stem portion in air spiral section inlet air, then along spiral tube runs, finally in air spiral Section exit forms the air draught of spiral.At mixing section, the ammonia air-flow of spiral and the air draught of reverse spiral are formed Strong convective motion, can be quickly mix, then mixed airflow passes through the first baffle plate and the second baffle plate.First Mixed airflow is become turbulent flow by baffle plate and the second baffle plate, is continued the mixed effect for reinforcing air and ammonia, is finally being mixed Gas outlet makes air and ammonia reach ideal mixed effect.

In addition, the first baffle plate and the second baffle plate are as one group and repeat 2 to 3 groups of setting;Or first baffle plate and Second baffle plate is arranged alternately and is respectively arranged 1-3, is preferably respectively arranged 2.

Ammonia becomes dilute ammonia after being mixed in the mixing arrangement with air, be then passed into the flue gas of adsorption tower into In exhaust gases passes before mouthful and in the adsorption tower.The active carbon desulfurization denitrating system includes activated carbon adsorber and parsing Tower.

The diameter of ammonia pipeline and air pipeline depends on the size scale of adsorption tower.The size scale of adsorption tower is bigger, Need the dilute ammonia amount being passed through bigger, then the diameter of ammonia pipeline and air pipeline is bigger.The overall diameter of ammonia pipeline is for example 5cm-80cm, such as 10-60cm, thickness of pipe wall are such as 1-2cm, such as 1.5cm.The overall diameter of air pipeline is such as 10cm- 120cm, such as 15-100cm, thickness of pipe wall are such as 1-2.5cm, such as 1.5 or 2.0cm.The total length of ammonia-air mixing device M It is 0.6-3.5 meters, it is preferably 1-3 meters, 1.5-2.5 meters more preferable.

Above-described air is with ammonia mixing arrangement by air pipeline, ammonia pipeline, air spiral section, ammonia spiral Section, mixing section and mixed gas outlet composition.Air is from air pipeline access equipment, and ammonia is from ammonia pipeline access equipment.It is empty Feed channel size is more than ammonia line size.Ammonia pipeline is inserted into air pipeline, then along air pipeline axis along Airflow direction extends a distance into that (it is, for example, the 20-80% of mixing arrangement total length, more preferable 35-65%, such as L= 0.2-2 meters, preferably 0.3-1.5 meters).In the ammonia pipeline being placed in air pipeline, along the ammonia spiral of air pipeline axis Section entrance starts to tail portion, belongs to ammonia spiral section.It is each if ammonia pipeline is divided into stem portion in ammonia spiral section Part extends back all along axis spiral, until ammonia spiral section exports, and between each part with spiral plate mutually every It opens.Air spiral section belongs to a part for air pipeline, terminates to the outlet of air spiral section since air spiral section entrance. In air spiral section, if the annulus between ammonia pipeline and air pipeline is divided into stem portion, each section is all along axis Line is extended back with the rotation direction spiral opposite with ammonia spiral pipeline section, until air spiral section exports, and each part Between be spaced from each other with spiral plate.Mixing section is to be located at after air spiral section immediately air spiral section, until mixed gas outlet A segment pipe, be internally provided with the first baffle plate, the second baffle plate, may also set up according to the first baffle plate and the second baffling Multigroup baffle plate of plate sequential arrangement.For example, the first baffle plate is annulus harden structure, Circular Plate outer circle connects with mixing duct inner wall It connects.Second baffle plate is Circular plate structure, is placed within mixing duct, has gap between plectane outer circle and mixing duct, can be held mixed Gas is closed to pass through.

Ammonia is mixed by " ammonia mixer " with the air that dilution air blasts, and NH is made3Concentration is less than lower explosion limit, is It prevents too low air temperature from condensing, needs to heat mixed gas, the dilution ammonia after heating is in adsorption column inlet Flue is uniformly sprayed by ammonia-spraying grid.

Activated carbon analytically be sent by top of tower, is discharged from tower bottom.Bringing-up section on Analytic Tower top, has adsorbed pollutant The activated carbon of matter is heated to 400 DEG C or more, and kept for 3 hours or more, the SO being tightly held by activated carbon2It is released, generates " sulfur-rich gas (SRG) ", SRG is delivered to relieving haperacidity workshop section and produces H2SO4.The NO being tightly held by activated carbonXIt is anti-that SCR or SNCR occurs It answers, while wherein bioxin is largely decomposed.Analytic Tower parsing institute's calorific requirement is provided by a hot-blast stove, and blast furnace gas is in warm In wind furnace after burning, heat smoke is sent into the shell side of Analytic Tower.Hot gas after heat exchange largely returns in hot air circulation blower (another Fraction is then outer to drain into air), hot-blast stove is sent by it and the high temperature hot gas newly burnt mixes.It is equipped with cooling in Analytic Tower lower part Section, blasts air and takes the heat of activated carbon out of.Cooling section is provided with cooling blower, blasts cold wind and cools down activated carbon, then It drains into air outside.Analytic Tower come out activated carbon by activated carbon sieve screening, by less than 1.2mm tiny active carbon particle and Dust removes, and the adsorption capacity of activated carbon can be improved.It is the strong activated carbon of adsorption capacity that activated carbon sieve, which shines upper object, and activity passes through 1# Activated carbon conveyer is delivered to adsorption tower and recycles, and screenings then enters ash cellar.It needs to be protected with nitrogen in resolving Shield, the SO that nitrogen will be parsed as carrier simultaneously2Equal pernicious gases are taken out of.Nitrogen is analytically passed through tower upper and lower part, Collect discharge, while the SO that will have been adsorbed in activated carbon among Analytic Tower2It takes out of, and send to acid making system and go relieving haperacidity.Nitrogen When being passed through above Analytic Tower, it is heated to 100 DEG C or so with nitrogen heater and is passed through in Analytic Tower again.

The present invention will produce a certain amount of containing NH primarily directed to relieving haperacidity workshop section in active carbon desulfurization3Waste water, this waste water Although amount is not too many, NH3Very high concentrations are dealt with very troublesome.The present invention can be very good to solve the problems, such as this, no But this part ammonia-containing water need not be handled, moreover it is possible to be efficiently used, be killed two birds with one stone.

Design and its absorbing process for flue gas (or exhaust gas) adsorption tower have had many documents to carry out in the prior art Disclose, see, for example, US5932179, JP2004209332A and JP3581090B2 (JP2002095930A) and JP3351658B2 (JPH08332347A), JP2005313035A.The application is no longer described in detail.

In the present invention, for adsorption tower, the design of single-tower muiti-bed layer, such as inlet plenum (A)-desulphurized aetivated carbon may be used Bed (a)-denitration activity charcoal bed (b)-discharge chamber (B) or such as inlet plenum (A)-desulphurized aetivated carbon bed (a)-desulphurization denitration Active carbon bed (b)-denitration activity charcoal bed (c)-discharge chamber (B);Or using the more bed designs of symmetrical double tower, such as outlet Room (B)-denitration activity charcoal bed (c)-desulphurization denitration active carbon bed (b)-desulphurized aetivated carbon bed (a)-inlet plenum (A)-is de- Sulphur active carbon bed (a)-desulphurization denitration active carbon bed (b)-denitration activity charcoal bed (c)-discharge chamber (B) or discharge chamber (B)-active carbon bed (d)-active carbon bed (c)-active carbon bed (b)-active carbon bed (a)-inlet plenum (A)-activated carbon Bed (a)-active carbon bed (b)-active carbon bed (c)-active carbon bed (d)-discharge chamber (B) or discharge chamber (B)-activity Charcoal bed (e)-active carbon bed (d)-active carbon bed (c)-active carbon bed (b)-active carbon bed (a)-inlet plenum (A)- Active carbon bed (a)-active carbon bed (b)-active carbon bed (c)-active carbon bed (d)-active carbon bed (e)-discharge chamber (B)。

In general, the tower height for the adsorption tower in the present invention is, such as 15-60 meters, preferably 20-50 meters, more preferably 25-45 meters.The tower height of adsorption tower refers to the height that activated carbon entrance at the top of adsorption tower is exported to from absorption tower bottom activated carbon, i.e., The height of the agent structure of tower.

In the present invention, Analytic Tower is not required particularly, the Analytic Tower of the prior art can be used in the present invention. Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type, and wherein activated carbon is inputted from tower top, is flowed downwardly through tube side, is then arrived Up to bottom of tower, and heat gas then flows through shell side, and heat gas enters from the side of tower, and hot friendship is carried out with the activated carbon for flowing through tube side It changes and cools down, then exported from the other side of tower.In the present invention, Analytic Tower is not required particularly, the prior art Analytic Tower can be used in the present invention.Preferably, Analytic Tower is the vertical Analytic Tower of shell pipe type (or package type) or pipe type, Wherein activated carbon is inputted from tower top, flows downwardly through the tube side of top heating zone, is then reached one and is in top heating zone under A cushion space between portion cooling zone, then flows through the tube side of lower part cooling zone, then reaches bottom of tower, and heat gas (or high-temperature hot-air) then flows through the shell side of heating zone, and the side of heat gas (400-450 DEG C) the analytically heating zone of tower enters, Indirect heat exchange is carried out with the activated carbon for flowing through heating zone tube side and is cooled down, and is then exported from the other side of the heating zone of tower.It is cold But the side of the wind analytically cooling zone of tower enters, with flow through the parsing of cooling zone tube side, regenerated activated carbon carry out it is indirect Heat exchange.After the indirect heat exchange, cooling wind is warming up to 120 ± 20 DEG C (such as 100-130 DEG C, such as from about 120 DEG C).

In general, the Analytic Tower being used in the present invention usually has 10-45 meters, preferably 15-40 meters, more preferable 20-35 The tower height of rice.Desorber usually has 6-100 meters2, preferably 8-50 meters2, it is 10-30 meters more preferable2, it is 15-20 meters further preferred2 Body cross-section product.

Design and regeneration method of active carbon for activated carbon Analytic Tower, have had many documents to carry out in the prior art It discloses, JP3217627B2 (JPH08155299A) discloses a kind of Analytic Tower (i.e. desorber), it uses double seal valve, leads to lazy Hermetic seal, screening, water cooling (referring to Fig. 3 in the patent).JP3485453B2 (JPH11104457A) discloses regenerator (ginseng See Figure 23 and 24), preheating section can be used, double seal valve leads to noble gas, air cooling or water cooling.JPS59142824A, which is disclosed, to be come It is used to preheat activated carbon from the gas of cooling section.Chinese patent application 201210050541.6 (Shanghai Ke Liu companies) discloses again The scheme that the energy of raw tower recycles, which use driers 2.JPS4918355B is disclosed using blast furnace gas (blast Furnace gas) carry out regenerated carbon.JPH08323144 A disclose the regenerator using fuel (heavy oil or light oil), use Air-heating furnace (referring to Fig. 2 of the patent, 11- hot-blast stoves, 12- fuel supply systems).Chinese utility model 201320075942.7 are related to heating device and have the emission-control equipment (coal-fired, air heating) of the heating device, referring to Fig. 2 in the utility model patent.

The Analytic Tower of the present invention is using air-cooled.

For the situation that Analytic Tower analytic ability is 10t activated carbons per hour, traditional handicraft keeps the temperature in Analytic Tower The coke-stove gas needed for 420 DEG C is about 400Nm3/ h, combustion air are about 2200Nm3/ h, outer thermal wind exhausting are about 2500Nm3/h;Institute Need cooling air 30000Nm3/ h, activated carbon temperature is 140 DEG C after cooling.

It " parses " and is used interchangeably with " regeneration " in this application.

In this application " optionally " indicate carry out or without." optional " indicate to be with or without.Analytic Tower and regeneration Tower is used interchangeably.Regeneration is used interchangeably with parsing.In addition, parsing and desorption are identical concepts." bringing-up section " and " heating Area " is identical concept." cooling section " and " cooling zone " are identical concepts.

Advantages of the present invention

1, compared with traditional cooling technology, methods and apparatus of the present invention has been always ensured that the safety of system, is adsorbing Accurately controlling for the temperature of flue gas is realized in tower (or reaction tower).The spray cooling used when normal operation does not increase substantially Treatment quantity, former smoke moisture variation or moisture fluctuation very little (< 1%), therefore to the low temperature active of activated carbon almost without shadow It rings.When system shutdown or failure, need to only open cold blast sliding valve can facilitate control active carbon bed temperature.

2, by using a kind of special air-ammonia mixing arrangement, air and ammonia can be allowed to reach ideal mixing Effect, it is ensured that ammonia is entered with suitable concentration in adsorption tower, it is ensured that the safe operation of adsorption tower, while ammonia is saved, it can carry The efficiency of the desulphurization and denitration of high adsorption tower reduces equipment operation cost, and the present apparatus is easy to operate, easy to operate.

3, the ammonia-containing water of the high concentration generated in the relieving haperacidity area (workshop section) of comprehensive utilization active carbon desulfurization system, both utilized NH in waste water3, the dosage for being passed into ammonia in adsorption tower is reduced, and can flue gas cool-down, no waste water be arranged, be avoided outside Handle the cost input of waste water.

Description of the drawings

Fig. 1 is desulfuring and denitrifying apparatus and the technological process for including activated carbon adsorber and regenerating active carbon tower of the prior art Schematic diagram.

Fig. 2A is the activated carbon adsorber of the present invention or the flue-gas temperature control process flow diagram of reaction tower.

Fig. 2 B are the schematic diagrames of the flue gas processing device including desulphurization denitration tower and Analytic Tower of the present invention.

Fig. 3 is including multiple (3) active carbon beds and implementing the single-tower muiti-bed stratotype suction of multistage spray ammonia for the present invention The schematic diagram of attached tower.

Fig. 4 is the signal of the adsorption tower of the more beds of symmetrical double tower (having clearance space between each bed) design of the present invention Figure.

Fig. 5 is the signal of the adsorption tower of the more beds of symmetrical double tower (gapless space between each bed) design of the present invention Figure.

Reference numeral

1:Adsorption tower or reaction tower;101,101a, 101b, 101c, a, b, c, d, e:Active carbon bed;102:Former flue gas or Former flue gas conveys flue;103:Neat stress;104:Activated carbon input port;104a:Active carbon material feeding valve;105:Activated carbon exports; 105b:Activated carbon blowdown valve;106:(dilution) ammonia;106a, 106b:Spray ammonia pipe array;106c:Air or hot-air;106d: Ammonia;507:Cold wind, 508:Process water transfer pipeline;509:Cold blast sliding valve;510:Baffle door;511:First temperature measuring point;512:The Two temperature measuring points;513:Third temperature measuring point;514:Booster fan;115, V1, V2 or V3:Ammonia valve;P1:Cold air inlet;P2:Work Skill (operating) water nozzle (water jet);M:Air/ammonia mixing arrangement.

2:Desorber;15:Activated carbon entrance to be regenerated;16:Regenerated carbon exports;

30:Activated carbon feed bin;

40:Activated carbon (AC) vibrating screen;401:Dust;

701:First activated carbon conveyer;702:Second activated carbon conveyer;

A:Inlet plenum;B:Discharge chamber;h:Adsorption section height.

Fig. 6 is the schematic diagram of air/ammonia mixing arrangement M of the present invention.

Fig. 7 is the partial schematic diagram of ammonia spiral section (610), wherein m=2.

Fig. 8 is the partial schematic diagram of ammonia spiral section (610) and air spiral section (609), wherein m=2, n=2.

Reference numeral

601, air intake;602, air pipeline;603, air pipeline spiral section entrance;604, ammonia spiral pipeline section enters Mouthful;605, ammonia entrance;606, ammonia pipeline;607, air spiral section spiral plate;608, ammonia spiral section spiral plate;609, empty Gas spiral section;610, ammonia spiral section;611, air pipeline spiral section exports;612, mixing section;613, ammonia spiral pipeline section Outlet;614, the first baffle plate;615, the second baffle plate;616, mixed gas outlet;617, mixed gas.

A, B, C and D:It is the space between ammonia pipeline and air pipeline of air spiral section (609) by spiral plate phase Four parts (four subchannels) mutually separated.

E, F, G and H:It is the ammonia pipeline of ammonia spiral section (610) by spiral plate four parts (four sons spaced apart from each other Channel).

Specific implementation mode

The SO in all embodiments, former flue gas2And NOxContent be respectively about 800mg/Nm3About 350mg/Nm3

The specific implementation mode of the present invention is described below:

Used mixing arrangement (M) includes air pipeline 602, ammonia pipeline 606, air spiral shell in the following embodiments Revolve section 609, ammonia spiral section 610, mixing section 612 and mixed gas outlet 616, wherein ammonia pipeline 606 is from diameter bigger The side of air pipeline 602 is inserted into (or extending into) air pipeline, then bending and along 602 axis of air pipeline along Airflow direction extends a distance into L, and (it is, for example, the 20-80% of mixing arrangement total length, more preferable 35-65%, such as L= 0.2-2 meters, preferably 0.3-1.5 meters), the latter end of ammonia pipeline 606 is ammonia spiral section 610, and ammonia spiral section 610 includes by ammonia The m spiral shape ammonia channel that the m spiral plates 608 being longitudinally extended in feed channel 606 are separated, in addition, with ammonia spiral 610 corresponding air spiral sections 609 of section include vertical by n in the space between ammonia pipeline 606 and air pipeline The n volute type air channel separated to the spiral plate 607 of extension is mixing section 612 after the end in both channels, The end of mixing section is mixed gas outlet 616;Wherein:M=1-6 and n=1-8, preferably m=1-4 and n=1-6, it is more excellent Choosing, m=2 or 3 and n=2,3,4 or 5;The hand of spiral of the hand of spiral and ammonia spiral section 610 of air spiral section 609 On the contrary.

In general, air spiral section 609 and ammonia spiral section 610 are concentric.

Preferably, m=1-4, n=1-6, more preferable m=2 or 3 and/or n=2,3,4 or 5.

Preferably, the first baffle plate 614 and/or the second baffle plate 615 are equipped in mixing section.Or, the first baffle plate 614 and second baffle plate 615 as one group and repeat setting 2 to 3 groups;Or first baffle plate 614 and the second baffle plate 615 hand over It is arranged for setting and respectively 1-3, is preferably respectively arranged 2.

Generally, the overall diameter of the ammonia pipeline 606 is the 30-70% of the internal diameter of air pipeline 602, more preferable 40-60%.

Preferably, the first baffle plate 614 is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall; Second baffle plate 615 is Circular plate structure, is placed within mixing duct, has gap between plectane excircle and mixing duct to allow Mixed gas passes through.

Preferably, the second baffle plate 615 is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall; First baffle plate 614 is Circular plate structure, is placed within mixing duct, has gap between plectane excircle and mixing duct to allow Mixed gas passes through.

In general, the length of air spiral section 609 is 0.7-2.8 times of the length of ammonia spiral section 610, preferably 0.8- 2.5 times, more preferable 1-2.0 times, more preferable 1.2-1.8 times.

In general, the length of mixing section 612 is 0.4-1 times, preferably 0.6-0.8 times of the length of air spiral section 609.

Air spiral section has the structure similar to spring or virtual spring with ammonia spiral section.The spiral of air spiral section The ratio between the respective screw pitch in spiral shape ammonia channel and screw diameter of shape air duct or ammonia spiral section (i.e. K/2R or k/2r) It is 0.2-2 respectively:1, preferably 0.4-1.5:1, more preferable 0.6-1.0:1.

Embodiment 1

Using flow shown in Fig. 1 and adsorption tower (as illustrated in fig. 1 and 2).

Activated carbon adsorption tower apparatus includes

1) adsorption tower (1),

2) flue 102 is conveyed in the former flue gas of the flue gas input port upstream of adsorption tower, wherein in the upstream position P1 of flue It is equipped with cold air inlet, and is equipped with technique (operating) water nozzle on the downstream position P2 of flue,

3) air-cooler 509 being connected with the cold air inlet on the positions P1,

4) the process water conveyance conduit 508 being connected with the technique (operating) water nozzle on the positions P2,

5) booster fan 514 between the positions P1 and P2, and

6) it is (as shown in Figure 6 with air mixing device M to be equipped with ammonia on the pipeline 106 for ammonia conveyance conduit 106 Ammonia-air mixing device M of the present invention.M=2 and n=2.The overall diameter of ammonia pipeline is 33cm, and thickness of pipe wall is 1.5cm.It is empty The overall diameter of feed channel is 55cm, and thickness of pipe wall is 2.0cm.The total length of ammonia-air mixing device M is 2.5 meters), from the pipe The multiple ammonia branches separated on road 106, these branches are connected respectively to the indoor one or more of air inlet positioned at adsorption tower Multiple ammonia nozzles in ammonia nozzle and clearance space between each active carbon bed.

In position, the first temperature measuring point and the second temperature measuring point is respectively set in the front side of P1 and rear side, and at the P2 of position Third temperature measuring point is arranged in the upstream of the gas inlet of adsorption tower in trip.In the upstream of the positions P1, one gas baffle door is set.

The tower height of adsorption tower is 24.5 meters.The flow 6.5 × 10 of heat smoke from sintering machine5Nm3/ h, humidity 8.1%.

Present embodiment 1 it is a kind of including flue gas temperature control in activated carbon adsorber flue gas desulfurization and denitration method it is basic Flow is as follows:

I) the step of flue gas temperature control or the step of flue gas temperature adjustment, which includes following sub-step:

(1) the upstream position P1 of the flue of high-temperature flue gas is being conveyed to activated carbon adsorber (that is, converting the site of cold wind first P1 at cold air inlet), first time cooling is carried out to flue gas by being passed through cold air (converting cold wind) into the flue,

(2) the technique (operating) water nozzle of the downstream position P2 (that is, site P2 of water spray) and then in the position P1 for being passed through cold air Cold mist is sprayed into flue gas of the place into flue to reduce the temperature of flue gas, flue gas continues towards adsorption tower along flue;With

(3) rear sprayed into the flue gas entered in adsorption tower and then in the inlet plenum for entering adsorption tower dilutes ammonia (i.e. Dilution air ammonia);

II) desulphurization and denitration step:Pass through temperature control in the above 1) step or enters absorption through overregulating the flue gas of temperature Flow through an active carbon bed (as illustrated in fig. 1 and 2) of adsorption tower (or reaction tower) after in the inlet plenum of tower, flue gas and from suction The activated carbon that attached tower top is added carries out cross-current type contact, pollutant (such as oxysulfide, nitrogen oxides, two wherein contained by flue gas Dislike English etc.) it is removed by activated carbon, neat stress is entered in discharge chamber and is discharged later, has adsorbed the activated carbon of pollutant then from suction Attached tower bottom discharge.

It is wherein T2 in the desired value or setting value of the second temperature measuring pointSetting=165 DEG C.On-line measurement is in the front end of position P1 The first temperature measuring point be in T1=346 DEG C of the flue-gas temperature in flue.Since actual measurement T1 is higher than T2SettingValue, according to T1 and T2Setting's Difference is predicted and is prejudged, due to T1 and T2SettingDifference it is larger, prediction or anticipation the result is that significantly increasing immediately cold The flow (significantly adjusting) of wind;And then significantly adjust air quantity after, on-line measurement in the rear end of position P1 second Temperature measuring point is in T2=186 DEG C of the flue-gas temperature in flue, accordingly according to T2 and T2SettingDifference fed back, due to T2 with T2SettingDifference it is smaller, therefore the flow (by a small margin adjust) of cold wind is further increased by a small margin, until actual measurement T2 is adjusted Section is controlled in T2Setting(165) it until within the scope of ± 5 DEG C, at this point, actual measurement T2 is stabilized in=165 DEG C or so, is sprayed into flue The technique water yield entered is stablized in 4.35m3/h。

Then, at the downstream of position P2, the third temperature measuring point set by the upstream of the gas inlet of adsorption tower, herein Desired value or preset value T3SettingIt is set to 155 DEG C.According to actual measurement T2 (i.e. 165 DEG C) and the desired value at third temperature measuring point Or preset value T3SettingDifference predicted and prejudged, since difference is slightly smaller, tune up by a small margin injection cold water flow.So Afterwards, and then T3=150 DEG C of the temperature of on-line measurement flue gas in flue at third temperature measuring point, according to actual measurement T3 and T3Setting's Difference is fed back to finely tune the flow of spray technology water (cold water), and T3 is controlled in T3Setting(150 DEG C) ± 3 DEG C of ranges, hereafter, It surveys T3 to stablize at 150 DEG C or so, the humidity of flue gas is 8.7%.

Then, the ammonia of Dilution air is sprayed into the flue gas entered in adsorption tower, slightly reduces the temperature of flue gas so that into The temperature for entering the flue gas in adsorption tower keeps relative stability at 146 DEG C or so.

Embodiment 2

Embodiment 1 is repeated, only adsorption tower shown in Fig. 3 is used to replace adsorption tower shown in Fig. 1.Adsorption tower Tower height is 24.5 meters.The flow 6.5 × 10 of heat smoke from sintering machine5Nm3/ h, humidity 8.1%.

Wherein flue-gas temperature in adsorption tower is made even for the flue-gas temperature in two clearance spaces between three beds Mean value.

Temperature (or active carbon bed temperature) into the flue gas in adsorption tower keeps relative stability at 140 DEG C or so.

Embodiment 3

Embodiment 1 is repeated, only adsorption tower shown in Fig. 4 is used to replace adsorption tower shown in Fig. 1.Adsorption tower Tower height is 30 meters.The flow 12 × 10 of heat smoke from sintering machine5Nm3/ h, humidity 8%.

Wherein flue-gas temperature in adsorption tower is that the flue-gas temperature in the clearance space between bed is averaged.

Temperature (or active carbon bed temperature) into the flue gas in adsorption tower keeps relative stability at 140 DEG C or so.

Embodiment 4

Embodiment 1 is repeated, only adsorption tower shown in Fig. 5 is used to replace adsorption tower shown in Fig. 1.Adsorption tower Tower height is 32 meters.The flow 10 × 10 of heat smoke from sintering machine5Nm3/ h, humidity 8%.

Wherein flue-gas temperature in adsorption tower is the indoor flue-gas temperature of air inlet.

Temperature (or active carbon bed temperature) into the flue gas in adsorption tower keeps relative stability at 150 DEG C or so.

Embodiment 5

When system normal operation, 145 DEG C of active carbon bed temperature, exhaust gas volumn 1 × 106Nm3/h.System is normally stopped transport at this time, The operation of water spray and spray ammonia stops, cold blast sliding valve standard-sized sheet, closes former baffle board door of flue, and booster fan normal operation sucks cold at this time Air quantity is 2 × 105Nm3Active carbon bed temperature is reduced to 75 DEG C after/h, 6h, can close booster fan at this time.Whole system is safely It stops operation.

Embodiment 6

Embodiment 1 is repeated, ammonia-air mixing device M of the invention shown in Fig. 6 is only used.M=4 and n= 4.The overall diameter of ammonia pipeline is 30cm, and thickness of pipe wall is 1.5cm.The overall diameter of air pipeline is 50cm, and thickness of pipe wall is 2.0cm. The total length of ammonia-air mixing device M is 2.1 meters.

The uniform mixing of ammonia and air improves the utilization ratio of ammonia, it is ensured that the safe operation of adsorption tower is saved simultaneously Ammonia can improve the efficiency of the desulphurization and denitration of adsorption tower, reduce equipment operation cost, and the mixing arrangement is static mixing Device, it is easy to operate.

Embodiment 7

Embodiment 6 is repeated, only in addition, using the ammonia-containing water generated in relieving haperacidity area (workshop section) as being injected into flue gas Process water a part, the process water of another part is pure water.

Not only the pure water dosage of a part had been saved, but also the ammonia of waste water is utilized, has reduced the dosage of ammonia, avoids simultaneously The processing for the ammonia-containing water that relieving haperacidity area generates and emission problem, save the cost of wastewater treatment.

Claims (80)

1. including sintering flue gas desulfurization, the method for denitration of flue gas temperature control, this approach includes the following steps:
I) the step of flue gas temperature control or the step of flue gas temperature adjustment, which includes following sub-step:
(1) pass through at the cold air inlet of the upstream position (P1) for the flue for conveying high-temperature flue gas to activated carbon adsorber first It is passed through cold air to carry out first time cooling to flue gas into the flue,
(2) and then in the flue gas at the technique (operating) water nozzle of the downstream position (P2) for the position (P1) for being passed through cold air into flue Process water for cooling down sintering flue gas, i.e. cooling water or cold mist are sprayed into, enters the flue-gas temperature of adsorption tower to adjust and exists The T3 of settingSettingIn range;
II) desulphurization and denitration step:In the above 1) step adsorption tower is entered by temperature control or the flue gas through overregulating temperature One or more active carbon beds of adsorption tower, flue gas and the activated carbon being added from absorption tower top are flowed successively through after in inlet plenum Cross-current type contact is carried out, meanwhile, the flue gas input channel neutralization that dilution ammonia is passed through to adsorption tower is optionally passed through in adsorption tower, Pollutant wherein contained by flue gas, the i.e. pollutant including oxysulfide, nitrogen oxides and dioxin, are taken off by activated carbon It removes, neat stress is entered in discharge chamber and is discharged later, has adsorbed the activated carbon of pollutant then from absorption tower bottom discharge;
III) activated carbon analyzing step:The activated carbon for having adsorbed pollutant is transferred to adding with top from the bottom of adsorption tower In a kind of heating zone of activated carbon Analytic Tower of the cooling zone of hot-zone and lower part, activated carbon is allowed to be parsed, be regenerated, and parse, Activated carbon after regeneration is discharged after flowing down through cooling zone from desorption tower bottom;Wherein:Nitrogen is passed through in resolving To the top of Analytic Tower, and nitrogen is passed through to the lower part of Analytic Tower via the second nitrogen pipeline optionally together;Be passed through solution Analyse tower in nitrogen by from activated carbon thermal desorption include SO2And NH3Gas pollutant inside from the heating zone of desorber and It takes out of and is sent to acid making system i.e. relieving haperacidity area in centre portion between cooling zone and go relieving haperacidity.
2. according to the method described in claim 1, it is characterized in that:T3SettingIn 105-150 DEG C of range.
3. according to the method described in claim 2, it is characterized in that:T3SettingIn 115-145 DEG C of range.
4. method according to any one of claim 1-3, wherein in above step (1), in the front side of position (P1) The first temperature measuring point and the second temperature measuring point, flue gas temperature of the on-line measurement at the two temperature measuring points in flue is respectively set with rear side T1 and T2 is spent, wherein the desired value or setting value in the second temperature measuring point are T2SettingWherein T2SettingIt is within the scope of 150-180 DEG C Value;
When actual measurement T1 is higher than T2SettingWhen value, start above-mentioned sub-step (1) and (2):According to T1 and T2SettingDifference carry out prediction and According to T2 and T2SettingDifference fed back the flow for carrying out cold wind in set-up procedure (1), so as to by T2 adjust or control in T2Setting ± a DEG C range, wherein a DEG C is at 2-10 DEG C;Or
When actual measurement T1 is less than T2SettingWhen value, cold wind valve is closed in the operation for starting above-mentioned sub-step (2), stopping step (1), Only carry out follow-up step (2);Or
When system failure or orderly closedown, the supply of flue gas is cut off, only operates above-mentioned sub-step (1), and stop son The operation of step (2), cold wind is passed through in adsorption tower.
5. according to the method described in claim 4, it is characterized in that:T2SettingIt is the value within the scope of 160-170 DEG C.
6. according to the method described in claim 4, wherein according to T1-T2SettingDifference △ T1, flue gas flow and cold air Temperature is calculated and determined the flow of the cold air in step (1), adjusts the aperture of cold wind valve, to by flue-gas temperature T2 It is reduced to T2Setting± a DEG C range.
7. according to the method described in claim 5, wherein according to T1-T2SettingDifference △ T1, flue gas flow and cold air Temperature is calculated and determined the flow of the cold air in step (1), adjusts the aperture of cold wind valve, to by flue-gas temperature T2 It is reduced to T2Setting± a DEG C range.
8. according to the method described in claim 4, wherein in above step (2), in the downstream of position (P2), in adsorption tower The upstream setting third temperature measuring point of gas inlet, the temperature T3 of on-line measurement flue gas in flue at third temperature measuring point, according to Survey T2 and the desired value or preset value T3 at third temperature measuring pointSettingDifference carry out prediction and according to T3 and T3SettingDifference It is fed back to adjust the flow of spray technology water, T3 is adjusted or is controlled in T3Setting± b DEG C range, wherein T3SettingIt is in 105- Value within the scope of 150 DEG C, and wherein b DEG C is at 2-10 DEG C.
9. according to the method described in any one of claim 5-7, wherein in above step (2), the downstream of position (P2), In the upstream of the gas inlet of adsorption tower, third temperature measuring point, the temperature of on-line measurement flue gas in flue at third temperature measuring point are set T3 is spent, according to actual measurement T2 and the desired value or preset value T3 at third temperature measuring pointSettingDifference carry out prediction and according to T3 with T3SettingDifference fed back to adjust the flow of spray technology water, T3 is adjusted or is controlled in T3Setting± b DEG C range, wherein T3SettingIt is the value within the scope of 105-150 DEG C, and wherein b DEG C is at 2-10 DEG C.
10. according to the method described in claim 8, wherein T3SettingIt is the value within the scope of 115-145 DEG C.
11. according to the method described in claim 9, wherein T3SettingIt is the value within the scope of 115-145 DEG C.
12. according to the method described in claim 8,10, any one of 11, wherein T2SettingCompare T3SettingIt is 20-50 DEG C high.
13. according to the method described in claim 9, wherein T2SettingCompare T3SettingIt is 20-50 DEG C high.
14. according to the method for claim 12, wherein T2SettingCompare T3SettingIt is 25-45 DEG C high.
15. according to the method for claim 13, wherein T2SettingCompare T3SettingIt is 25-45 DEG C high.
16. the method according to claims 14 or 15, wherein T2SettingCompare T3SettingIt is 30-40 DEG C high.
17. according to the method described in any one of claim 1-3,5-8,10-11,13-15, wherein process water be or including In the ammonia-containing water that relieving haperacidity area generates.
18. according to the method described in claim 4, wherein process water be or be included in relieving haperacidity area generation ammonia-containing water.
19. according to the method described in claim 9, wherein process water be or be included in relieving haperacidity area generation ammonia-containing water.
20. according to the method for claim 12, wherein process water be or be included in relieving haperacidity area generation ammonia-containing water.
21. according to the method described in any one of claim 1-3,5-8,10-11,13-15,18-20, wherein in step (II) in, dilution ammonia is obtained by ammonia and air by air-ammonia mixing arrangement (M), the mixing arrangement (M) packet It includes air pipeline (602), ammonia pipeline (606), air spiral section (609), ammonia spiral section (610), mixing section (612) and mixes Gas vent (616) is closed, wherein ammonia pipeline (606) is inserted into air pipeline from the side of the air pipeline (602) of diameter bigger In, it then bends and extends a distance into L, the end of ammonia pipeline (606) along airflow direction along air pipeline (602) axis Section is ammonia spiral section (610), and ammonia spiral section (610) includes by the m spiral plates being longitudinally extended in ammonia pipeline (606) (608) the m spiral shape ammonia channel separated, in addition, air spiral section (609) corresponding with ammonia spiral section (610) Include by being separated between the n spiral plates (607) that are longitudinally extended of the ammonia pipeline (606) in space between air pipeline N volute type air channel, be mixing section (612) after the end in both channels, the end of mixing section is gaseous mixture Body exports (616);Wherein:M=1-6 and n=1-8.
22. according to the method described in claim 4, wherein in step (II), dilution ammonia is to pass through sky by ammonia and air For gas-ammonia mixing arrangement (M) come what is obtained, which includes air pipeline (602), ammonia pipeline (606), air Spiral section (609), ammonia spiral section (610), mixing section (612) and mixed gas outlet (616), wherein ammonia pipeline (606) It is inserted into air pipeline, then bends and along air pipeline (602) axis from the side of the air pipeline (602) of diameter bigger L is extended a distance into along airflow direction, the latter end of ammonia pipeline (606) is ammonia spiral section (610), ammonia spiral section (610) include being led to by the m spiral shape ammonia that the m spiral plates (608) being longitudinally extended in ammonia pipeline (606) are separated Road, in addition, air spiral section (609) corresponding with ammonia spiral section (610) includes by between ammonia pipeline (606) and air The n volute type air channel that the n in the space spiral plates (607) being longitudinally extended between pipeline are separated, at both It is mixing section (612) after the end in channel, the end of mixing section is mixed gas outlet (616);Wherein:M=1-6 and n= 1-8。
23. according to the method described in claim 9, wherein in step (II), dilution ammonia is to pass through sky by ammonia and air For gas-ammonia mixing arrangement (M) come what is obtained, which includes air pipeline (602), ammonia pipeline (606), air Spiral section (609), ammonia spiral section (610), mixing section (612) and mixed gas outlet (616), wherein ammonia pipeline (606) It is inserted into air pipeline, then bends and along air pipeline (602) axis from the side of the air pipeline (602) of diameter bigger L is extended a distance into along airflow direction, the latter end of ammonia pipeline (606) is ammonia spiral section (610), ammonia spiral section (610) include being led to by the m spiral shape ammonia that the m spiral plates (608) being longitudinally extended in ammonia pipeline (606) are separated Road, in addition, air spiral section (609) corresponding with ammonia spiral section (610) includes by between ammonia pipeline (606) and air The n volute type air channel that the n in the space spiral plates (607) being longitudinally extended between pipeline are separated, at both It is mixing section (612) after the end in channel, the end of mixing section is mixed gas outlet (616);Wherein:M=1-6 and n= 1-8。
24. according to the method for claim 12, wherein in step (II), dilution ammonia is to pass through sky by ammonia and air For gas-ammonia mixing arrangement (M) come what is obtained, which includes air pipeline (602), ammonia pipeline (606), air Spiral section (609), ammonia spiral section (610), mixing section (612) and mixed gas outlet (616), wherein ammonia pipeline (606) It is inserted into air pipeline, then bends and along air pipeline (602) axis from the side of the air pipeline (602) of diameter bigger L is extended a distance into along airflow direction, the latter end of ammonia pipeline (606) is ammonia spiral section (610), ammonia spiral section (610) include being led to by the m spiral shape ammonia that the m spiral plates (608) being longitudinally extended in ammonia pipeline (606) are separated Road, in addition, air spiral section (609) corresponding with ammonia spiral section (610) includes by between ammonia pipeline (606) and air The n volute type air channel that the n in the space spiral plates (607) being longitudinally extended between pipeline are separated, at both It is mixing section (612) after the end in channel, the end of mixing section is mixed gas outlet (616);Wherein:M=1-6 and n= 1-8。
25. according to the method for claim 21, wherein m=1-4 and n=1-6.
26. according to the method described in any one of claim 22-24, wherein m=1-4 and n=1-6.
27. according to the method for claim 25, wherein m=2 or 3 and n=2,3,4 or 5.
28. according to the method for claim 26, wherein m=2 or 3 and n=2,3,4 or 5.
29. the method according to claim 27 or 28, the wherein spiral shell of the hand of spiral of air spiral section and ammonia spiral section It is opposite to revolve direction.
30. according to the method for claim 21, it is characterised in that:The mixing arrangement further includes the be located in mixing section One baffle plate (614) and/or the second baffle plate (615);And/or
The overall diameter of the ammonia pipeline (606) is the 30-70% of the internal diameter of air pipeline (602), and/or
The volute type air channel of air spiral section (609) or the respective spiral shell in spiral shape ammonia channel of ammonia spiral section (610) Away from being 0.2-2 with the ratio between screw diameter:1.
31. the method according to any one of claim 22-25,27-28, it is characterised in that:The mixing arrangement also wraps Include the first baffle plate (614) and/or the second baffle plate (615) in mixing section;And/or
The overall diameter of the ammonia pipeline (606) is the 30-70% of the internal diameter of air pipeline (602), and/or
The volute type air channel of air spiral section (609) or the respective spiral shell in spiral shape ammonia channel of ammonia spiral section (610) Away from being 0.2-2 with the ratio between screw diameter:1.
32. according to the method for claim 26, it is characterised in that:The mixing arrangement further includes the be located in mixing section One baffle plate (614) and/or the second baffle plate (615);And/or
The overall diameter of the ammonia pipeline (606) is the 30-70% of the internal diameter of air pipeline (602), and/or
The volute type air channel of air spiral section (609) or the respective spiral shell in spiral shape ammonia channel of ammonia spiral section (610) Away from being 0.2-2 with the ratio between screw diameter:1.
33. according to the method for claim 29, it is characterised in that:The mixing arrangement further includes the be located in mixing section One baffle plate (614) and/or the second baffle plate (615);And/or
The overall diameter of the ammonia pipeline (606) is the 30-70% of the internal diameter of air pipeline (602), and/or
The volute type air channel of air spiral section (609) or the respective spiral shell in spiral shape ammonia channel of ammonia spiral section (610) Away from being 0.2-2 with the ratio between screw diameter:1.
34. according to the method described in claim 30,32, any one of 33, it is characterised in that:Outside the ammonia pipeline (606) Diameter is the 40-60% of the internal diameter of air pipeline (602).
35. according to the method for claim 31, it is characterised in that:The overall diameter of the ammonia pipeline (606) is air pipeline (602) 40-60% of internal diameter.
36. according to the method described in claim 30,32,33, any one of 35, it is characterised in that:First baffle plate (614) is The excircle of annulus harden structure, Circular Plate is connect with mixing duct inner wall;It is Circular plate structure with the second baffle plate (615), is placed in Within mixing duct, there is gap between plectane excircle and mixing duct to allow mixed gas to pass through;Or
Second baffle plate (615) is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;First baffle plate (614) it is Circular plate structure, is placed within mixing duct have gap between plectane excircle and mixing duct to allow mixed gas Pass through.
37. according to the method for claim 31, it is characterised in that:First baffle plate (614) is annulus harden structure, Circular Plate Excircle connect with mixing duct inner wall;It is Circular plate structure with the second baffle plate (615), is placed within mixing duct, plectane There is gap between excircle and mixing duct to allow mixed gas to pass through;Or
Second baffle plate (615) is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;First baffle plate (614) it is Circular plate structure, is placed within mixing duct have gap between plectane excircle and mixing duct to allow mixed gas Pass through.
38. according to the method for claim 34, it is characterised in that:First baffle plate (614) is annulus harden structure, Circular Plate Excircle connect with mixing duct inner wall;It is Circular plate structure with the second baffle plate (615), is placed within mixing duct, plectane There is gap between excircle and mixing duct to allow mixed gas to pass through;Or
Second baffle plate (615) is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;First baffle plate (614) it is Circular plate structure, is placed within mixing duct have gap between plectane excircle and mixing duct to allow mixed gas Pass through.
39. according to the method for claim 21, it is characterised in that:The length of air spiral section (609) is ammonia spiral section (610) 0.8-2.5 times of length;And/or
The length of mixing section (12) is 0.4-1 times of the length of air spiral section (9).
40. according to the method described in claim 22-25,27-28,30,32-33,35,37, any one of 38, feature exists In:The length of air spiral section (609) is 0.8-2.5 times of the length of ammonia spiral section (610);And/or
The length of mixing section (12) is 0.4-1 times of the length of air spiral section (9).
41. according to the method for claim 26, it is characterised in that:The length of air spiral section (609) is ammonia spiral section (610) 0.8-2.5 times of length;And/or
The length of mixing section (12) is 0.4-1 times of the length of air spiral section (9).
42. according to the method for claim 31, it is characterised in that:The length of air spiral section (609) is ammonia spiral section (610) 0.8-2.5 times of length;And/or
The length of mixing section (12) is 0.4-1 times of the length of air spiral section (9).
43. according to the method for claim 36, it is characterised in that:The length of air spiral section (609) is ammonia spiral section (610) 0.8-2.5 times of length;And/or
The length of mixing section (12) is 0.4-1 times of the length of air spiral section (9).
44. according to the method described in any one of claim 39,41-43, it is characterised in that:The length of air spiral section (609) Degree is 1-1.5 times of the length of ammonia spiral section (610).
45. according to the method for claim 40, it is characterised in that:The length of air spiral section (609) is ammonia spiral section (610) 1-1.5 times of length.
46. according to the method described in claim 30,32,33,35,37,38,42, any one of 43, it is characterised in that:First Baffle plate (614) and the second baffle plate (615) as one group and repeat 2 to 3 groups of setting;Or,
First baffle plate (614) and the second baffle plate (615) are arranged alternately and are respectively arranged 1-3.
47. according to the method for claim 31, it is characterised in that:First baffle plate (614) and the second baffle plate (615) are made For one group and repeat 2 to 3 groups of setting;Or,
First baffle plate (614) and the second baffle plate (615) are arranged alternately and are respectively arranged 1-3.
48. according to the method for claim 36, it is characterised in that:First baffle plate (614) and the second baffle plate (615) are made For one group and repeat 2 to 3 groups of setting;Or,
First baffle plate (614) and the second baffle plate (615) are arranged alternately and are respectively arranged 1-3.
49. according to the method for claim 46, it is characterised in that:First baffle plate (614) and the second baffle plate (615) are handed over It is arranged for setting and respectively 2.
50. the method according to claim 47 or 48, it is characterised in that:First baffle plate (614) and the second baffle plate (615) it is arranged alternately and is respectively arranged 2.
51. desulfurization and denitrification apparatus or in any one of above claim 1-50 the methods desulfurization and denitration dress It sets, it includes
1) tower height of adsorption tower (1), adsorption tower is 15-60 meters;
2) in the former flue gas of the flue gas input port upstream of adsorption tower conveying flue (102), wherein in the upstream position (P1) of flue It is equipped with cold air inlet, and is equipped with technique (operating) water nozzle on the downstream position (P2) of flue,
3) air-cooler (509) being connected with the cold air inlet on the position (P1),
4) the process water conveyance conduit (508) being connected with the technique (operating) water nozzle on the position (P2),
5) booster fan (514) between the position (P1) and (P2),
6) ammonia transfer pipeline (106), wherein:A kind of ammonia and air mixing device (M) are equipped on the pipeline (106), it should The rear end of pipeline (106) is respectively communicated to conveying flue (102) and/or extends in adsorption tower and be mounted with ammonia at its end Gas jets, or multiple ammonia branches are separated from the latter end of the pipeline (106), these branches are respectively communicated to conveying flue (102) it and is optionally coupled to be located at optional positioned at the indoor one or more ammonia nozzles of the air inlet of adsorption tower (1) Multiple ammonia nozzles in clearance space between each active carbon bed of adsorption tower (1);With
7) desorber (2), it includes the heating zone on top and the cooling zone of lower part and positioned at middle area between the two.
52. desulphurization and denitration device according to claim 51, wherein:The tower height of adsorption tower is 20-50 meters;Process water is defeated The ammonia-containing water basin for sending the other end of pipeline (508) to be connected to relieving haperacidity area.
53. the desulphurization and denitration device according to claim 51 or 52, wherein:Distinguish in the front-end and back-end of position (P1) First temperature measuring point and the second temperature measuring point are set.
54. desulphurization and denitration device according to claim 53, wherein:In the downstream of position (P2), in the flue gas of adsorption tower Third temperature measuring point is arranged in the upstream of import.
55. according to the desulphurization and denitration device described in claim 51,52, any one of 54, it is characterised in that:The mixing arrangement (M) include air pipeline (602), ammonia pipeline (606), air spiral section (609), ammonia spiral section (610), mixing section (612) it is inserted into from the side of the air pipeline (602) of diameter bigger with mixed gas outlet (616), wherein ammonia pipeline (606) In air pipeline, then bends and extend a distance into L, ammonia pipeline along airflow direction along air pipeline (602) axis (606) latter end is ammonia spiral section (610), and ammonia spiral section (610) includes being prolonged by m in ammonia pipeline (606) is longitudinal The m spiral shape ammonia channel that the spiral plate (608) stretched is separated, in addition, air spiral shell corresponding with ammonia spiral section (610) Rotation section (609) includes by between a spiral plates being longitudinally extended of n of the ammonia pipeline (606) in space air pipeline between (607) the n volute type air channel separated is mixing section (612), the end of mixing section after the end in both channels End is mixed gas outlet (616);Wherein:M=1-6 and n=1-8.
56. desulphurization and denitration device according to claim 53, it is characterised in that:The mixing arrangement (M) includes air pipeline (602), ammonia pipeline (606), air spiral section (609), ammonia spiral section (610), mixing section (612) and mixed gas outlet (616), wherein ammonia pipeline (606) is inserted into from the side of the air pipeline (602) of diameter bigger in air pipeline, is then bent And L is extended a distance into along airflow direction along air pipeline (602) axis, the latter end of ammonia pipeline (606) is ammonia spiral shell Revolve section (610), ammonia spiral section (610) include spiral plates (608) institute that is longitudinally extended by the m in ammonia pipeline (606) every The m spiral shape ammonia channel opened, in addition, air spiral section (609) corresponding with ammonia spiral section (610) include by between The n spiral that the n in the space between air pipeline spiral plates (607) being longitudinally extended of ammonia pipeline (606) are separated Shape air duct is mixing section (612) after the end in both channels, and the end of mixing section is mixed gas outlet (616);Wherein:M=1-6 and n=1-8.
57. desulphurization and denitration device according to claim 55, it is characterised in that:M=1-4 and n=1-6.
58. desulphurization and denitration device according to claim 56, it is characterised in that:M=1-4 and n=1-6.
59. the desulphurization and denitration device according to claim 57 or 58, it is characterised in that:M=2 or 3 and n=2,3,4 or 5。
60. desulphurization and denitration device according to claim 59, it is characterised in that:The hand of spiral and ammonia of air spiral section The hand of spiral of gas spiral section is opposite.
61. desulphurization and denitration device according to claim 55, it is characterised in that:The mixing arrangement further includes being located to mix Close the first baffle plate (614) and/or the second baffle plate (615) in section;And/or
The overall diameter of the ammonia pipeline (606) is the 30-70% of the internal diameter of air pipeline (602);And/or
The volute type air channel of air spiral section (609) or the respective spiral shell in spiral shape ammonia channel of ammonia spiral section (610) Away from being 0.2-2 with the ratio between screw diameter:1.
62. the desulphurization and denitration device according to claim 56-58, any one of 60, it is characterised in that:The mixing dress Set further includes the first baffle plate (614) being located in mixing section and/or the second baffle plate (615);And/or
The overall diameter of the ammonia pipeline (606) is the 30-70% of the internal diameter of air pipeline (602);And/or
The volute type air channel of air spiral section (609) or the respective spiral shell in spiral shape ammonia channel of ammonia spiral section (610) Away from being 0.2-2 with the ratio between screw diameter:1.
63. desulphurization and denitration device according to claim 59, it is characterised in that:The mixing arrangement further includes being located to mix Close the first baffle plate (614) and/or the second baffle plate (615) in section;And/or
The overall diameter of the ammonia pipeline (606) is the 30-70% of the internal diameter of air pipeline (602);And/or
The volute type air channel of air spiral section (609) or the respective spiral shell in spiral shape ammonia channel of ammonia spiral section (610) Away from being 0.2-2 with the ratio between screw diameter:1.
64. the desulphurization and denitration device according to claim 61 or 63, it is characterised in that:The ammonia pipeline (606) it is outer straight Diameter is the 40-60% of the internal diameter of air pipeline (602).
65. desulphurization and denitration device according to claim 62, it is characterised in that:The overall diameter of the ammonia pipeline (606) is The 40-60% of the internal diameter of air pipeline (602).
66. according to the desulphurization and denitration device described in claim 61,63, any one of 65, it is characterised in that:First baffle plate (614) it is annulus harden structure, the excircle of Circular Plate is connect with mixing duct inner wall;It is plectane knot with the second baffle plate (615) Structure is placed within mixing duct, has gap between plectane excircle and mixing duct to allow mixed gas to pass through;Or
Second baffle plate (615) is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;First baffle plate (614) it is Circular plate structure, is placed within mixing duct have gap between plectane excircle and mixing duct to allow mixed gas Pass through.
67. desulphurization and denitration device according to claim 62, it is characterised in that:First baffle plate (614) is that annulus is hardened The excircle of structure, Circular Plate is connect with mixing duct inner wall;It is Circular plate structure with the second baffle plate (615), is placed in mixing duct Within, there is gap between plectane excircle and mixing duct to allow mixed gas to pass through;Or
Second baffle plate (615) is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;First baffle plate (614) it is Circular plate structure, is placed within mixing duct have gap between plectane excircle and mixing duct to allow mixed gas Pass through.
68. desulphurization and denitration device according to claim 64, it is characterised in that:First baffle plate (614) is that annulus is hardened The excircle of structure, Circular Plate is connect with mixing duct inner wall;It is Circular plate structure with the second baffle plate (615), is placed in mixing duct Within, there is gap between plectane excircle and mixing duct to allow mixed gas to pass through;Or
Second baffle plate (615) is annulus harden structure, and the excircle of Circular Plate is connect with mixing duct inner wall;First baffle plate (614) it is Circular plate structure, is placed within mixing duct have gap between plectane excircle and mixing duct to allow mixed gas Pass through.
69. desulphurization and denitration device according to claim 55, it is characterised in that:The length of air spiral section (609) is ammonia 0.8-2.5 times of the length of gas spiral section (610);And/or
The length of mixing section (612) is 0.4-1 times of the length of air spiral section (609).
70. the desulphurization and denitration device according to claim 56-58,60,61,63,65,67, any one of 68, feature It is:The length of air spiral section (609) is 0.8-2.5 times of the length of ammonia spiral section (610);And/or
The length of mixing section (612) is 0.4-1 times of the length of air spiral section (609).
71. desulphurization and denitration device according to claim 62, it is characterised in that:The length of air spiral section (609) is ammonia 0.8-2.5 times of the length of gas spiral section (610);And/or
The length of mixing section (612) is 0.4-1 times of the length of air spiral section (609).
72. desulphurization and denitration device according to claim 66, it is characterised in that:The length of air spiral section (609) is ammonia 0.8-2.5 times of the length of gas spiral section (610);And/or
The length of mixing section (612) is 0.4-1 times of the length of air spiral section (609).
73. according to the desulphurization and denitration device described in claim 69,71, any one of 72, it is characterised in that:Air spiral The length of section (609) is 1-1.5 times of the length of ammonia spiral section (610).
74. desulphurization and denitration device according to claim 70, it is characterised in that:The length of air spiral section (609) is ammonia 1-1.5 times of the length of gas spiral section (610).
75. according to the desulphurization and denitration device described in claim 61,63,65,67,68, any one of 72, it is characterised in that: First baffle plate (614) and the second baffle plate (615) as one group and repeat 2 to 3 groups of setting;Or,
First baffle plate (614) and the second baffle plate (615) are arranged alternately and are respectively arranged 1-3.
76. desulphurization and denitration device according to claim 62, it is characterised in that:First baffle plate (614) and the second baffling Plate (615) is as one group and repeats 2 to 3 groups of setting;Or,
First baffle plate (614) and the second baffle plate (615) are arranged alternately and are respectively arranged 1-3.
77. desulphurization and denitration device according to claim 64, it is characterised in that:First baffle plate (614) and the second baffling Plate (615) is as one group and repeats 2 to 3 groups of setting;Or,
First baffle plate (614) and the second baffle plate (615) are arranged alternately and are respectively arranged 1-3.
78. desulphurization and denitration device according to claim 66, it is characterised in that:First baffle plate (614) and the second baffling Plate (615) is as one group and repeats 2 to 3 groups of setting;Or,
First baffle plate (614) and the second baffle plate (615) are arranged alternately and are respectively arranged 1-3.
79. according to the desulphurization and denitration device described in claim 75, it is characterised in that:First baffle plate (614) and the second baffling Plate (615) is arranged alternately and is respectively arranged 2.
80. the desulphurization and denitration device according to any one of claim 76-78, it is characterised in that:First baffle plate (614) it is arranged alternately with the second baffle plate (615) and is respectively arranged 2.
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CN108187445B (en) * 2018-02-09 2020-05-22 中冶长天国际工程有限责任公司 Flue gas purification method and device comprising flue gas temperature control
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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102580707A (en) * 2012-02-29 2012-07-18 上海克硫环保科技股份有限公司 Simple heat exchange type active carbon coke purifying and regenerating process system and active carbon coke purifying and regenerating process method
CN103657320A (en) * 2013-11-26 2014-03-26 江苏海宏机械制造有限公司 Flue gas dust-removal desulfurizing system
CN203620507U (en) * 2013-11-11 2014-06-04 新兴常胜环保科技实业有限公司 Novel dry method post-treatment system

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2005028210A (en) * 2003-07-07 2005-02-03 Mitsubishi Heavy Ind Ltd Exhaust gas treatment system

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102580707A (en) * 2012-02-29 2012-07-18 上海克硫环保科技股份有限公司 Simple heat exchange type active carbon coke purifying and regenerating process system and active carbon coke purifying and regenerating process method
CN203620507U (en) * 2013-11-11 2014-06-04 新兴常胜环保科技实业有限公司 Novel dry method post-treatment system
CN103657320A (en) * 2013-11-26 2014-03-26 江苏海宏机械制造有限公司 Flue gas dust-removal desulfurizing system

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