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CN109136544A - A kind of low NO of grate-kiln pelletizingxProduction technology and its system - Google Patents

A kind of low NO of grate-kiln pelletizingxProduction technology and its system Download PDF

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Publication number
CN109136544A
CN109136544A CN201811055262.2A CN201811055262A CN109136544A CN 109136544 A CN109136544 A CN 109136544A CN 201811055262 A CN201811055262 A CN 201811055262A CN 109136544 A CN109136544 A CN 109136544A
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sections
section
ddd
drying zone
preheating
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CN109136544B (en
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胡兵
陆彪
叶恒棣
储太山
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Zhongye Changtian International Engineering Co Ltd
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Zhongye Changtian International Engineering Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating
    • C22B1/20—Sintering; Agglomerating in sintering machines with movable grates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8696—Controlling the catalytic process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/90—Injecting reactants
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/16—Sintering; Agglomerating
    • C22B1/216—Sintering; Agglomerating in rotary furnaces
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/26—Cooling of roasted, sintered, or agglomerated ores
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Metallurgy (AREA)
  • Analytical Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Manufacturing & Machinery (AREA)
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  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Materials Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treating Waste Gases (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Abstract

The present invention provides a kind of grate-kiln pelletizing low NOxProduction technology, for the production technology in down-draft drying zone (DDD), the position above green-ball sprays into reduction activator, reduction activator and NO contained in the hot wind entered in down-draft drying zone (DDD) from rotary kiln (2)xSCR denitration is realized in reaction.In preferably, increases and spray into the excessive reduction activator with catalytic action in (< 950 DEG C) of the suitable temperature section preheated above two sections of (PH) charge levels.Technical solution of the present invention solves the above-mentioned technical problem faced, have " it is with low investment, operating cost is low, the escaping of ammonia is few, NOxEmission reduction effect is significant " the characteristics of.

Description

A kind of low NO of grate-kiln pelletizingxProduction technology and its system
Technical field
The present invention relates to a kind of grate-kiln pelletizing production technologies, and in particular to a kind of grate-kiln pelletizing Low NOx(nitrogen oxides) production technology and production system belong to pelletizing production, environmental protection technical field.
Background technique
Pellet is the main iron-containing charge of China's blast furnace ironmaking, and China's pellet yield in 2015 is 128,000,000 tons.Phase Than sinter, since low energy consumption, environment is relatively friendly for pelletizing production process, and product is with intensity is good, grade is high, metallurgical performance Good advantage, increasing And Coke-saving can be played, improve ironmaking technology economic indicator, reduce pig iron cost, mention by being applied in blast furnace process The effect of high economic benefit, therefore pellet is greatly developed recent years in China.
For China's pelletizing production based on grate kiln technique, yield accounts for 60% or more of pelletizing total output.In recent years Come, with increasingly sophisticated, the raising (maturing temperature is caused to increase) of bloodstone ratio, low-rank fuel of iron ore raw material and fuel Scale utilize, the application of the nitrogenous coke-stove gas of gas base rotary kiln etc. so that many enterprise pelletizing production process NOxConcentration of emission It is in rising trend；In addition increasingly harsh, the NO that Environmental Protection in China requiresxDischarge is included into the checking system of discharge, from 2015, Pelletizing production NOx(with NO2Meter) emission limit 300mg/m3, so that Some Enterprises need to add denitration facility and are just able to satisfy country Discharge standard.
Although a large amount of work has been done in environmental protection by pelletizing enterprise, dedusting and desulfurization have obtained effective control, Neng Gouman Sufficient emission request, but current NOxAt high cost, complex process is removed, under the environment of steel form depression, this gives pelletizing industry New challenge is brought, Some Enterprises are because of NOxExceeded a large amount of underproduction of having to, or even face and shut down.From current most of ball From the point of view of group's condition of production, NOxGenerally discharge exceeded 30~100mg/m3If NO can be reduced from source and processxIt generates, So as to meet emission request, then end denitration cleaning equipment can be saved, meaning weight is produced to grate-kiln pelletizing Greatly, be conducive to further increase the vitality and competitiveness of pelletizing enterprise.
The method of existing removing nitrogen oxides in effluent mainly selective catalytic reduction technique (SCR) and non-selective is urged Change reduction technique (SNCR).Wherein, temperature plays a leading role to SNCR denitration technology.It is generally acknowledged that temperature range be 800 DEG C~ 1100 DEG C are more suitable for, when the temperature is excessively high, NH3Oxidation generates NO, and the concentration that may cause NO increases, and leads to NOxRemoval efficiency It reduces；When the temperature is too low, NH3Reaction rate decline, NOxRemoval efficiency can also decline, while NH3Escape amount also will increase. Usually the temperature range of preheating two sections (PH) is 850 DEG C~1000 DEG C, meets the condition of SNCR denitration method, but needs to optimize control System can be only achieved optimal emission reduction effect.
The selectivity of SCR denitration technology refers in the effect of catalyst and under oxygen existence condition, NH3Preferential and NOxHair It survives former elimination reaction, generates N2And H2O, and the oxygen in flue gas of getting along well carries out oxidation reaction.
Grate-kiln pelletizing production technology in the prior art is as shown in figure 3, drying grate is divided into blasting drying period (UDD), two sections down-draft drying zone (DDD), preheated one-section (TPH) and preheating (PH), it is cold that ring cold machine is divided into ring cold one section of (C1), ring Two sections (C2) and ring are cold three sections (C3).Wherein, the wind of ring cold one section (C1) is directly entered agglomerates mine in rotary kiln (Kiln), Then preheated two sections (PH) are blown into down-draft drying zone (DDD) to green-ball progress exhausting drying, then through taking out after heating pre- hot-bulb Wind dryer section (DDD) discharges (handle before discharge by gas cleaning) outward；The wind of ring cold two sections (C2) enters preheated one-section (TPH) it is discharged outward after heating pre- hot-bulb；It is dry to green-ball progress air blast that the wind of ring cold three sections (C3) enters blasting drying period (UDD) It is dry, to realize the closed cycle of drying grate-rotary kiln-circular cooler air circulation.
106268270 A of Publication No. CN, publication date are on January 4th, 2017, a kind of entitled " grate kiln The patent document of denitrating system " discloses a kind of grate kiln denitrating system, and this method passes through in the second preheating section Chamber increases denitrification apparatus, and nozzle spray direction is identical as the flow direction of flue gas.Although the technology a degree of can be reduced NOxDischarge amount, but reduce limited extent, the reduction dosage of spray is more difficult to control, excessively then causes NH3Environment is polluted in escape, Cross few then NOxDischarge still cannot reach the requirement of discharge.
Grate-kiln pelletizing can generate a certain number of NO during producing acid pelletx, according to enterprise's atmosphere Requirement of the pollutant emission limit to pellet roasting equipment, grate-kiln pelletizing NOx(with NO2Meter) discharge standard must be low In 300mg/m3, from the point of view of current most of pelletizing production situation, NOxGenerally discharge exceeded 30~100mg/m3。NOxProduction Life is mostly derived from two kinds of forms of fuel type and heating power type, although can reduce rotary kiln by reducing coal gas or coal dust straying quatity Temperature, and use lower NOxRaw material and the measures such as fuel reduce grate-kiln pelletizing production process NOxGeneration Amount, but require to seem excessively harsh to the buying of crude fuel, the optimization of process system and the selection of change system, once production Process is unstable, and it will cause NOxIt is exceeded.
In order to meet grate-kiln pelletizing production process NOxEmission request, the energy-saving and emission-reduction for responding country are called, It the characteristics of inventing more advanced air circulation, while utilize system itself, must be realized low from process flow NOxPelletizing production.
Summary of the invention
For situation existing in the prior art, in order to solve pelletizing production process NOxDischarge is not up to standard and in end It adds the enterprises such as denitrification apparatus somewhat expensive and is difficult to the problem of receiving, this patent is proposed by optimizing and revising down-draft drying zone (DDD) green-ball temperature (300~450 DEG C), while reduction activator is sprayed at down-draft drying zone (DDD), to meet NOxPass through material Layer when under the catalytic action of green-ball with NH3Reaction generates N2, realize SCR denitration.In preferably, increase in preheating two (< 950 DEG C) of suitable temperature section above section (PH) charge level sprays into the excessive reduction activator for having catalytic action, so that one The NO dividedxAt high temperature rapidly and NH3Reaction generates N2, to realize NOxEmission reduction, preheated two sections of excessive reduction activator (PH) enter down-draft drying zone (DDD), administered by the collaboration of the two, can significantly reduce grate kiln oxygen Pellet production process NOxDischarge.Technical solution of the present invention solves the above-mentioned technical problem faced, has " with low investment, fortune Row is at low cost, the escaping of ammonia is few, NOxEmission reduction effect is significant " the characteristics of.
The first embodiment provided according to the present invention provides a kind of grate-kiln pelletizing low NOxProduce work Skill.
A kind of low NO of grate-kiln pelletizingxProduction technology, the production technology the following steps are included:
1) green-ball is successively added by two sections of blasting drying period, down-draft drying zone, preheated one-section and preheating on drying grate Heat, subsequently into rotary kiln by roasting, then on ring cold machine successively by ring is one section cold, ring cold two sections and cold three sections of ring into Row cooling, obtains acid pellet；
2) cooling wind temperature after cold one section of ring increases, and then the wind by the cold one section of discharge of ring is delivered to rotary kiln internal reference With pellet roasting, the hot wind discharged from rotary kiln is delivered to two sections of preheating of drying grate；The hot wind preheating two sections in and green-ball It is delivered to down-draft drying zone after carrying out heat exchange, then the exhaust outlet discharge of down-draft drying zone；
3) it is increased by cold two sections of ring of cooling wind temperature, the wind of the cold two sections of discharges of ring is delivered to the preheating one of drying grate Section, and heat exchange is carried out with green-ball in preheated one-section, green-ball is preheated, is then discharged from the exhaust outlet of preheated one-section；
4) it is increased by cold three sections of ring of cooling wind temperature, the air blast that the wind of the cold three sections of discharges of ring is delivered to drying grate is done Dry section, and heat exchange is carried out with green-ball in blasting drying period, then it is discharged from the exhaust outlet of blasting drying period；
In down-draft drying zone, position above green-ball sprays into reduction activator, reduction activator with from rotary kiln Into NO contained in the hot wind in down-draft drying zonexSCR denitration is realized in reaction.
Preferably, the wind of the cold two sections of discharges of ring to be delivered to preheated one-section and the down-draft drying zone of drying grate.Ring cold two It is 250-500 DEG C that the wind of section discharge, which adjusts the temperature in down-draft drying zone, preferably 300-450 DEG C, more preferably 350-420 ℃。
Preferably, the position above green-ball sprays into reduction activator in two sections of preheating.Reduction activator with into Enter NO contained in the hot wind in two sections of preheatingxSNCR denitration is realized in reaction.
Preferably, the temperature in two sections of preheating is 800-1100 DEG C, preferably 850-1050 DEG C, more preferably 900- 1000℃。
Preferably, being equipped with reduction activator atomising device in two sections of preheating.Reduction activator atomising device includes more A nozzle.
It a length of a of two sections of preheating, width b, is highly c, the exhaust gas volumn that input preheats two sections is S, will preheat two sections along length It spends direction and sets n section.Each section is equipped with nozzle.Set the height distance of mineral aggregate charge level in nozzle distance drying grate For h.Detect the NOx flow Q in the unit time in two sections of input preheating1, calculating processing flow is Q1Be needed for NOx also The theoretical amount U of former activator0, reduction activator and NOxThe reaction time of reaction is t, passes through following calculating:
Preheat horizontal velocity V distinguished and admirable in two sections of drying grates1Are as follows:
Preheat vertical speed V distinguished and admirable in two sections of drying grates2Are as follows:
Preheat two sections of drying grate setting section number n are as follows:
Preheat each siding-to-siding block length d of two sections of drying grates setting are as follows:
The height distance h of mineral aggregate charge level in nozzle distance drying grate are as follows:
The straying quatity for controlling reduction activator in each section, in the unit time,
1st section reduction activator straying quatity U1Are as follows:
2nd section reduction activator straying quatity U2Are as follows:
……
N-th of section reduction activator straying quatity UnAre as follows:
Preferably, the straying quatity of reduction activator is U in down-draft drying zone, exhausting is inputted in the detection unit time NOx flow Q in dryer section2, the theoretical amount U of reduction activator needed for calculating processing flow NOx0', it detects from pre- Two sections of reduction activation agent fluxes escaped into down-draft drying zone of heat are U ', then spray into the unit time in down-draft drying zone The straying quatity of reduction activator is U=U0’-U’。
In the present invention, it preheats in the SNCR denitration reaction in two sections, U0=k1*Q1；Wherein, k1For according to two sections of preheating The ammonia nitrogen ratio (NSR) of interior SNCR denitration reaction calculates gained coefficient.
In the present invention, in the SCR denitration reaction in down-draft drying zone, U0'=k2*Q2；Wherein, k2It is dry according to exhausting The ammonia nitrogen ratio (NSR) of SCR denitration reaction calculates gained coefficient in dry section.
In the present invention, k1To calculate gained coefficient according to the ammonia nitrogen ratio (NSR) of SNCR denitration reaction in two sections of preheating, In two sections of preheating, the amount of the reducing agent of penetrating according to SNCR denitration react in the flow of nitrogen oxides determine.k2For according to pumping The ammonia nitrogen ratio (NSR) of SCR denitration reaction calculates gained coefficient, in down-draft drying zone, the reducing agent of penetrating in wind dryer section Amount is determined according to the flow of the nitrogen oxides in SCR denitration reaction.k1、k2It is related with the concentration of reducing agent.Such as reductant concentration When (mass concentration) is 1-10%, k1And k2In the range of 1-30, within the scope of preferably 1-20, within the scope of more preferably 2-10. As reductant concentration be 10-20% when, k1And k2In the range of 0.5-20, within the scope of preferably 1-15, more preferably 2-10 model In enclosing.As reductant concentration be 20-50% when, k1And k2In the range of 0.2-15, within the scope of preferably 0.5-12, more preferably For within the scope of 1-10.As reductant concentration be 50-100% when, k1And k2In the range of 0.1-10, preferably 0.3-8 range It is interior, within the scope of more preferably 0.5-5.
In the present invention, reduction activator and NOxThe reaction time t of reaction be more than or equal to 0.5 second, preferably 0.6-2 seconds, More preferably 0.7-1.5 seconds, more preferably 0.8-1.2 seconds.
In the present invention, the reduction activator includes reducing agent and auxiliary agent.
Preferably, reducing agent is one of ammonia, ammonium hydroxide, urea or a variety of.Auxiliary agent is NaCl, containing vanadium solution, Jie One of hole/micropore nanophase materials are a variety of.
Preferably, it is empty to spray into compression while spraying into reduction activator in cold two sections of down-draft drying zone and/or ring Gas.
Preferably, being sprayed into down-draft drying zone and/or cold two sections of ring again after water dilution is added in reduction activator.
In the present invention, the salting liquid of vanadium, such as ammonium metavanadate or oxygen vanadium sulphate solution etc. are contained containing vanadium solution.
Second of the embodiment provided according to the present invention provides a kind of grate-kiln pelletizing low NOxProduction system System.
A kind of low NO of grate-kiln pelletizingxProduction system is used for production technology described in the first embodiment Pelletizing production system, which includes: drying grate, rotary kiln, ring cold machine.Wherein: moved towards according to technique, the drying grate according to It is secondary to be provided with two sections of blasting drying period, down-draft drying zone, preheated one-section and preheating.Ring cold machine is disposed with that ring is one section cold, ring Cold two sections and cold three sections of ring.Two sections of preheating of the tail end connection drying grate of rotary kiln connect the ring cold one of ring cold machine with the other end Section.
Wherein: cold one section of the air outlet of ring is connected to the air inlet of rotary kiln via first pipe.The air outlet of rotary kiln The air inlet of two sections of preheating is connected to via second pipe.The air outlet of two sections of preheating is connected to exhausting drying by third pipeline The air inlet of section；
Cold two sections of the air outlet of ring is connected to the air inlet of preheated one-section via the 4th pipeline.Cold three sections of the air outlet warp of ring The air inlet of blasting drying period is connected to by the 5th pipeline.
Reduction activator atomising device is equipped in down-draft drying zone.Reduction activator atomising device includes nozzle.Nozzle is set Set the top inside down-draft drying zone.
Preferably, it is the 6th pipeline that the 4th pipeline, which separates a branch,.6th pipeline be connected to down-draft drying zone into Air port.
Preferably, being equipped with reduction activator atomising device in two sections of preheating.Reduction activator atomising device includes nozzle. The top of two intersegmental parts of preheating is arranged in nozzle.
In the present invention, reduction activator atomising device further includes reducing agent holding vessel, auxiliary agent holding vessel, auxiliary agent delivery pipe Road, water conveyance conduit, reduction activator conveyance conduit.Auxiliary agent conveyance conduit connects reducing agent holding vessel and auxiliary agent holding vessel.Water Conveyance conduit is connected to reducing agent holding vessel.Reduction activator conveyance conduit connects reducing agent holding vessel and nozzle.
Preferably, reduction activator conveyance conduit is equipped with flow control valve.
Preferably, the production system further includes compressed air storage tank, airflow pipe.Airflow pipe connection Compressed air storage tank and nozzle.
In the present invention, one or more nozzles are equipped in down-draft drying zone.
Preferably, being equipped with multiple nozzles in down-draft drying zone, multiple nozzles are evenly arranged in the length in down-draft drying zone It spends in direction and width direction.
In the present invention, two sections are preheated and sets n section along its length, one or more sprays are equipped in each section Mouth.
Preferably, in each section in the width direction on be uniformly provided with multiple nozzles.
Preferably, being equipped with temperature-detecting device in down-draft drying zone.Third pipeline is filled equipped with the first NOx flow detection It sets.Third pipeline is equipped with reduction activator flow detector.6th pipeline is equipped with the 2nd NOx flow detector.
Preferably, second pipe is equipped with flue gas flow monitoring device.Second pipe is equipped with the 3rd NOx flow detection Device.
Preferably, the 7th pipeline connection being connect with the air outlet of down-draft drying zone, the air outlet company with preheated one-section The 8th pipeline connect is connected to chimney after passing through desulfurization process device and/or deduster after merging.
Preferably, third pipeline is equipped with deduster.
In the present invention, cold one section of the air inlet of ring, cold two sections of the air inlet of ring and cold three sections of the air inlet of ring be and wind Machine is connected.The air outlet of blasting drying period is connected to chimney by the 9th pipeline.
In the present invention, in down-draft drying zone, reduction activator atomising device, spray is arranged in the position above green-ball Enter reduction activator, is reaction bedding using the green-ball in down-draft drying zone on drying grate, using the hot environment of flue gas itself, Reduction activator is sprayed into, so that SCR denitration reaction occurs for the nitrogen oxides in reduction activator and flue gas, is removed in flue gas NOx, so that the concentration and total amount of nitrogen oxides greatly reduce from the flue gas that down-draft drying zone is discharged, protect environment.It is existing Flue gas and green-ball in down-draft drying zone will be inputted in technology and carries out direct emission after heat exchange, lead to nitrogen oxidation in the flue gas of discharge Object content is higher, does not conform to and accords with new discharge standard.In the technical solution of the application, input down-draft drying zone in flue gas, first, Green-ball on the flue gas and drying grate carries out heat exchange, plays the role of preheating green-ball；Second, it is reaction bedding using green-ball, Using the high-temperature characteristic of the flue gas, reduction activator is sprayed into, SCR denitration reaction occurs in down-draft drying zone, is removed in flue gas Nitrogen oxides.
In the present invention, a part in the wind of the cold two sections of discharges of ring is delivered to down-draft drying zone, the purpose of conveying and Standard is that the temperature controlled in down-draft drying zone is 250-500 DEG C, preferably 300-450 DEG C, more preferably 350-420 DEG C.This Apply for inventor by further investigation discovery, this temperature range is best SCR reaction temperature, guarantees the denitration in down-draft drying zone Efficiency (compared with low temperature environment carries out SCR denitration, denitration efficiency improves 30%-60%).In the prior art, due to inputting exhausting Flue gas in dryer section is the flue gas after two sections of heat exchange of preheating, when which is delivered to down-draft drying zone again, flue-gas temperature It reduces, generally 200-250 DEG C or so, the flue gas of this temperature cannot effectively carry out SCR denitration reaction in down-draft drying zone, Therefore, a part in the wind (temperature is generally 700-1000 DEG C or so) of the cold two sections of discharges of ring is delivered to exhausting and done by the present invention Dry section, the temperature in down-draft drying zone is adjusted, its temperature environment is made to control the temperature reacted in optimum SCR, it is dry to improve exhausting Denitration efficiency in dry section.
Atomization reduction activator spray into and preheating two sections (PH) escape occurs following anti-in down-draft drying zone (DDD) It answers:
NO+NO2+2NH3→2N2+3H2O.......... (1),
2NO+4NH3+O2→3N2+6H2O......... (2),
4NH3+2NO+2O2→3N2+6H2O......... (3),
By above-mentioned reaction, two sections of (PH) NH of preheating can be not only reduced3Escape, and NO may be implementedx85% or more Removal efficiency.
In the present invention, in two sections of preheating, reduction activator atomising device is added in the position above green-ball, sprays into Reduction activator reducing agent is reacted with NOx contained in the hot wind entered in two sections of preheating, realizes SNCR denitration.The technical program Using green-ball in two sections of preheating as reaction bedding, the flue gas that roasting in kilns generates will be turned round and carry out heat with green-ball at two sections of preheating Exchange while preheating green-ball, sprays into reducing agent, reacts so that reducing agent carries out SNCR denitration with the nitrogen oxides in flue gas, Since the flue gas discharged from rotary kiln is directly entered two sections of preheating, this flue-gas temperature is higher, and generally 800-1100 DEG C, existing skill Using the green-ball in the smoke pre-heating drying grate in art, the present invention is preheating two sections of penetrating reducing agents, is utilizing the flue gas and green-ball While carrying out heat exchange, the nitrogen oxides in flue gas is handled, to reduce the content of nitrogen oxides in effluent.The mist of penetrating Change reduction activator and following reaction occur in two sections of preheating (PH):
4NO+4NH3+O2→4N2+6H2O.......... (1),
6NO+4NH3→5N2+6H2O......... (2),
2NO2+4NH3+O2→3N2+6H2O......... (3),
6NO2+8NH3→7N2+12H2O.........(4)。
By above-mentioned reaction, the NO in flue gas may be implementedx(NO and NO2) it is converted into N2, effectively reduce NO in flue gasx Discharge amount.In addition, unreacted reducing agent activator, which can also blast down-draft drying zone (DDD) as SCR method, takes off NOxAlso Former agent, thus improves NOxRemoval efficiency, and as far as possible reduce NH3Escape.
In the present invention, the rationally penetrating position of control reduction activator, and the straying quatity of each corresponding penetrating position. The flue gas being discharged from rotary kiln enters two sections of preheating from the tail portion of drying grate, is then discharged from two sections of preheating of bottom.Therefore, Glide path of the flue gas in two sections of preheating is parabola or class parabola, and the present invention is by reasonably calculating and being laid out, the 1st A section reduction activator straying quatity U1Are as follows:2nd section reduction activator straying quatity U2Are as follows:..., n-th of section reduction activator straying quatity UnAre as follows:From above-mentioned The straying quatity that the calculation formula of straying quatity can be seen that the 1st section is maximum, then successively reduces, most there is the spray in a section Enter amount minimum.Reduction activator is sprayed into using this technique, since closer to the position of rotary kiln, flue gas just enters preheating two Section, higher in height and position, the concentration of nitrogen oxides in effluent is also higher, this position sprays into larger amount of reduction activator, this When the time longest reacted with nitrogen oxides in effluent of reduction activator, efficiency also highest；With the flowing of flue gas, slowly to original The direction for managing rotary kiln is mobile, and the position of flue gas in the height direction also reduces, sprays into less amount of reduction activator at this time, know Road rearmost position (close to the position of preheated one-section), sprays into minimal amount of reduction activator.This design, that is, ensure that reduction activation Agent is sufficiently reacted with nitrogen oxides, is also improved the reactivity and utilization rate of reduction activator, is reduced the escape of reduction activator； Cost is reduced, while protecting environment.Because the reducing agent in reduction activator is generally ammonium hydroxide, ammonia or urea etc., all it is The substance of highly volatile and escape, in case of escaping, taste is pungent, and is easy to happen work safety accident.
The present invention is also provided with SCR denitration reaction device in down-draft drying zone, while by regulation, guaranteeing down-draft drying zone Interior temperature, using the technique and system of the application, even if escaping out partial reduction activator, the portion of escape from preheating two sections Divide reduction activator as flue gas enters down-draft drying zone, which continues to be catalyzed and be gone back in down-draft drying zone Former effect carries out SCR reaction in down-draft drying zone, consumes the reduction activator of escape, further improves reduction and lives The utilization rate of agent, also ensures production safety.
The present invention is respectively provided with reduction activator atomising device in two sections of preheating and down-draft drying zone, and purpose is first is that pass through twice Process carries out denitration process to the flue gas that rotary kiln discharges, and removes the nitrogen oxides in flue gas to greatest extent, lowers flue gas row Release the content of nitrogen oxides；Purpose is second is that the reducing agent due to use is readily volatilized, if only spraying into also at two sections of preheating All there is the volatilization of a part in former activator, reducing agent therein, the reducing agent for escape of volatilizing is dry as flue gas enters exhausting Section, if the reducing agent escaped out that volatilizees just will directly be arranged to atmosphere without being further processed, greatly pollutes environment.This SCR denitration reaction process and device are added in invention in down-draft drying zone, so that the reducing agent escaped out is in down-draft drying zone It consumes, and generates the effect of denitration, make full use of the reducing agent, while avoiding the outlet of reducing agent.
In the present invention, the 1st section is proximate to the position in two sections of preheating of rotary kiln, interior according to this to push away, and the n-th section is former Manage the position in two sections of preheating of rotary kiln (namely close to the position of preheated one-section).The length of two sections of preheating refers to along green-ball Traffic direction in drying grate, length of this section on drying grate.Two sections of width of preheating refers in horizontal direction, falls in and chain Comb machine length direction, the width of two sections of preheating.The height of two sections of preheating refers in the vertical direction, preheats two sections of height.
In the present invention, temperature-detecting device is used to detect the temperature in down-draft drying zone, guarantees SCR in down-draft drying zone The progress of denitration reaction.If temperature is too low in down-draft drying zone, increase from the cigarette in ring cold two sections of inputs down-draft drying zone Tolerance；If temperature is excessively high in down-draft drying zone, reduces or stop from the exhaust gas volumn in ring cold two sections of inputs down-draft drying zone. By temperature-detecting device, guarantees that the temperature in down-draft drying zone is the condition of optimum SCR denitration reaction, guarantee denitration effect Rate.
In the present invention, the first NOx flow detector, reduction activator flow detector, the 2nd NOx flow detection The setting of device is according to actual needs, to adjust reduction activation in time for the smoke condition in real-time control down-draft drying zone The straying quatity of agent avoids the waste and escape of reduction activator.First NOx flow detector detects in the unit time from preheating NOx flow in two sections of input down-draft drying zones, the 2nd NOx flow detector detect in the unit time from the cold two sections of inputs of ring NOx flow in down-draft drying zone, from two sections of NOx flows inputted in down-draft drying zones of preheating and unit time in the unit time The sum of interior NOx flow from ring cold two sections of inputs down-draft drying zone flows for the NOx inputted in down-draft drying zone in the unit time Measure Q2。
In the present invention, the setting of flue gas flow monitoring device, the 3rd NOx flow detector is for real-time control Smoke condition in two sections of preheating adjusts the straying quatity of reduction activator in time, avoids reduction activator according to actual needs Waste and escape.The exhaust gas volumn that the detection input of flue gas flow monitoring device preheats two sections is S, the inspection of the 3rd NOx flow detector Survey the NOx flow Q in the unit time in two sections of input preheating1。
The art of this patent is equally applicable to pelletizing belt type roasting machine and other Pelletizing Process with the technical characterstic.
In this application, generally, the length of drying grate be 10-150 meters, preferably 20-80 meters, preferably 30-70 meters, More preferably 40-60 meters.Generally, the length of rotary kiln is 20-60 meters, preferably 25-50 meters, 30-45 meters more preferable, such as 35 Or 40 meters.
Compared with prior art, technical solution of the present invention has following advantageous effects:
1, in the technical solution of the application, the flue gas in down-draft drying zone is inputted, is reaction bedding using green-ball, utilizes this The high-temperature characteristic of flue gas sprays into reduction activator, and SCR denitration reaction occurs in down-draft drying zone, removes the nitrogen oxygen in flue gas Compound.
2, a part in the wind (temperature is generally 700-1000 DEG C or so) of the cold two sections of discharges of ring is delivered to by the present invention Down-draft drying zone adjusts the temperature in down-draft drying zone, its temperature environment is made to control the temperature reacted in optimum SCR, improves Denitration efficiency in down-draft drying zone.
3, reduction activator atomising device is arranged in preheated one-section in the present invention, by the process to the flue gas of rotary kiln discharge Denitration process is carried out, the nitrogen oxides in flue gas is removed, lowers the content that flue gas emission goes out nitrogen oxides.
4, in the present invention, the rationally penetrating position of control reduction activator, and the penetrating of each corresponding penetrating position Amount.It ensure that reduction activator is sufficiently reacted with nitrogen oxides, also improve the reactivity and utilization rate of reduction activator, reduce The escape of reduction activator；Cost is reduced, while protecting environment.
Detailed description of the invention
Fig. 1 is a kind of low NO of grate-kiln pelletizing of the present inventionxDown-draft drying zone sprays into reduction activation in production technology The process flow chart of agent；
Fig. 2 is a kind of low NO of grate-kiln pelletizing of the present inventionxTwo sections of sprays in down-draft drying zone and preheating in production technology Enter the process flow chart of reduction activator；
Fig. 3 is the structural schematic diagram of grate-kiln pelletizing production system in the prior art；
Fig. 4 is a kind of low NO of grate-kiln pelletizing of the present inventionxThe structural schematic diagram of production system；
Fig. 5 is a kind of low NO of grate-kiln pelletizing of the present inventionxIn production system down-draft drying zone and preheating two sections Structural schematic diagram equipped with reduction activator atomising device；
Fig. 6 is the structural schematic diagram of reduction activator atomising device of the present invention；
Fig. 7 is a kind of low NO of grate-kiln pelletizing of the present inventionxTwo sections and reduction activator mist are preheated in production system Disguise the structural schematic diagram set；
Fig. 8 is a kind of low NO of grate-kiln pelletizing of the present inventionxThe control of the straying quatity of reduction activator in production system Schematic diagram processed；In figure: a is the length for preheating two sections, wide, the c that b is two sections of preheating are the height for preheating two sections, and S is defeated in the unit time Enter the exhaust gas volumn of two sections of preheating, h is the height distance of mineral aggregate charge level in nozzle distance drying grate, V1For in two sections of drying grates of preheating Distinguished and admirable horizontal velocity, V2For vertical speed distinguished and admirable in two sections of drying grates of preheating, d is each of two sections of drying grates settings of preheating A siding-to-siding block length.
Appended drawing reference:
1: drying grate；UDD: blasting drying period；DDD: down-draft drying zone；TPH: preheated one-section；PH: two sections of preheating；2: returning Rotary kiln；201: the air inlet of rotary kiln；202: the air outlet of rotary kiln；C: ring cold machine；C1: cold one section of ring；C1a: cold one section of ring Air inlet；C1b: cold one section of the air outlet of ring；C2: cold two sections of ring；C2a: cold two sections of the air inlet of ring；C2b: cold two sections of ring Air outlet；C3: cold three sections of ring；C3a: cold three sections of the air inlet of ring；C3b: cold three sections of the air outlet of ring；301: preheating two sections into Air port；302: the air outlet of two sections of preheating；303: the air inlet of down-draft drying zone；304: the air outlet of down-draft drying zone；305: The air inlet of preheated one-section；306: the air outlet of preheated one-section；307: the air inlet of blasting drying period；308: blasting drying period Air outlet；4: reduction activator atomising device；401: nozzle；402: reducing agent holding vessel；403: auxiliary agent holding vessel；404: flow Control valve；5: compressed air storage tank；601: temperature-detecting device；602: the one NOx flow detectors；603: reduction activation Agent flux detection device；604: the two NOx flow detectors；605: flue gas flow monitoring device；The inspection of 606: the three NOx flows Survey device；7: chimney；8: deduster；9: blower；L1: first pipe；L2: second pipe；L3: third pipeline；L4: the four pipe Road；L5: the five pipeline；L6: the six pipeline；L7: auxiliary agent conveyance conduit；L8: water conveyance conduit；L9: reduction activator delivery pipe Road；L10: airflow pipe；The connection of L11: the seven pipeline；L12: the eight pipeline；L13: the nine pipeline.
Specific embodiment
The low NO of a kind of grate-kiln pelletizing provided according to the present inventionxProduction system.
A kind of low NO of grate-kiln pelletizingxProduction system, the system include: drying grate 1, rotary kiln 2, ring cold machine C.Wherein: being moved towards according to technique, the drying grate 1 is disposed with blasting drying period UDD, down-draft drying zone DDD, preheated one-section Two sections of PH of TPH and preheating.Ring cold machine C is disposed with the cold one section of C1 of ring, the cold two sections of C2 of ring and the cold three sections of C3 of ring.Rotary kiln 2 The cold one section of C1 of ring that two sections of PH of preheating of tail end connection drying grate 1 connect ring cold machine C with the other end.
Wherein: the air outlet C1b of the cold one section of C1 of ring is connected to the air inlet 201 of rotary kiln 2 via first pipe L1.Revolution The air outlet 202 of kiln 2 is connected to the air inlet 301 of two sections of PH of preheating via second pipe L2.Preheat the air outlet 302 of two sections of PH The air inlet 303 of down-draft drying zone DDD is connected to by third pipeline L3；
The air outlet C2b of the cold two sections of C2 of ring is connected to the air inlet 305 of preheated one-section TPH via the 4th pipeline L4.Ring is cold The air outlet C3b of three sections of C3 is connected to the air inlet 307 of blasting drying period UDD via the 5th pipeline L5.
Reduction activator atomising device 4 is equipped in the DDD of down-draft drying zone.Reduction activator atomising device 4 includes nozzle 401.The top inside the DDD of down-draft drying zone is arranged in nozzle 401.
Preferably, it is the 6th pipeline L6 that the 4th pipeline L4, which separates a branch,.It is dry that 6th pipeline L6 is connected to exhausting The air inlet 303 of section DDD.
Preferably, being equipped with reduction activator atomising device 4 in two sections of PH of preheating.Reduction activator atomising device 4 includes Nozzle 401.The top inside two sections of PH of preheating is arranged in nozzle 401.
In the present invention, reduction activator atomising device 4 further includes reducing agent holding vessel 402, auxiliary agent holding vessel 403, helps Agent conveyance conduit L7, water conveyance conduit L8, reduction activator conveyance conduit L9.Auxiliary agent conveyance conduit L7 connection reducing agent holding vessel 402 and auxiliary agent holding vessel 403.Water conveyance conduit L8 is connected to reducing agent holding vessel 402.The L9 connection of reduction activator conveyance conduit Reducing agent holding vessel 402 and nozzle 401.
Preferably, reduction activator conveyance conduit L9 is equipped with flow control valve 404.
Preferably, the production system further includes compressed air storage tank 5, airflow pipe L10.Airflow pipe L10 connection compressed air storage tank 5 and nozzle 401.
In the present invention, one or more nozzles 401 are equipped in the DDD of down-draft drying zone.
Preferably, being equipped with multiple nozzles 401 in the DDD of down-draft drying zone, it is dry that multiple nozzles 401 are evenly arranged in exhausting On length direction and width direction in section DDD.
In the present invention, two sections of PH are preheated and set n section along its length, one or more is equipped in each section Nozzle 401.
Preferably, in each section in the width direction on be uniformly provided with multiple nozzles 401.
Preferably, being equipped with temperature-detecting device 601 in the DDD of down-draft drying zone.Third pipeline L3 is flowed equipped with the first NOx Amount detecting device 602.Third pipeline L3 is equipped with reduction activator flow detector 603.6th pipeline L6 is equipped with second NOx flow detector 604.
Preferably, second pipe L2 is equipped with flue gas flow monitoring device 605.Second pipe L2 is equipped with the 3rd NOx Flow detector 606.
Preferably, the 7th pipeline connection L11 and preheated one-section that are connect with the air outlet 304 of down-draft drying zone DDD The 8th pipeline L12 that the air outlet 306 of TPH connects is connected to cigarette after passing through desulfurization process device and/or deduster after merging Chimney 7.
Preferably, third pipeline L3 is equipped with deduster 8.
In the present invention, the air inlet C2a and the cold three sections of C3 of ring of the cold two sections of C2 of air inlet C1a, ring of the cold one section of C1 of ring Air inlet C3a is connected with blower 9.The air outlet 308 of blasting drying period UDD is connected to chimney 7 by the 9th pipeline L13.
Embodiment 1
As shown in figure 4, a kind of low NO of grate-kiln pelletizingxProduction system, the system include: drying grate 1, revolution Kiln 2, ring cold machine C.Wherein: being moved towards according to technique, the drying grate 1 is disposed with blasting drying period UDD, down-draft drying zone DDD, preheated one-section TPH and two sections of PH of preheating.Ring cold machine C is disposed with the cold one section of C1 of ring, the cold two sections of C2 of ring and cold three sections of ring C3.The cold one section of C1 of ring that two sections of PH of preheating of the tail end connection drying grate 1 of rotary kiln 2 connect ring cold machine C with the other end.
Wherein: the air outlet C1b of the cold one section of C1 of ring is connected to the air inlet 201 of rotary kiln 2 via first pipe L1.Revolution The air outlet 202 of kiln 2 is connected to the air inlet 301 of two sections of PH of preheating via second pipe L2.Preheat the air outlet 302 of two sections of PH The air inlet 303 of down-draft drying zone DDD is connected to by third pipeline L3；
The air outlet C2b of the cold two sections of C2 of ring is connected to the air inlet 305 of preheated one-section TPH via the 4th pipeline L4.Ring is cold The air outlet C3b of three sections of C3 is connected to the air inlet 307 of blasting drying period UDD via the 5th pipeline L5.
Reduction activator atomising device 4 is equipped in the DDD of down-draft drying zone.Reduction activator atomising device 4 includes a spray Mouth 401.The top inside the DDD of down-draft drying zone is arranged in nozzle 401.
The air inlet C3a of the air inlet C2a and the cold three sections of C3 of ring of the cold two sections of C2 of air inlet C1a, ring of the cold one section of C1 of ring are equal It is connected with blower 9.The air outlet 308 of blasting drying period UDD is connected to chimney 7 by the 9th pipeline L13.
Embodiment 2
As shown in figure 5, repeating embodiment 1, it is the 6th pipeline L6 that only the 4th pipeline L4, which separates a branch,.6th pipeline L6 is connected to the air inlet 303 of down-draft drying zone DDD.
Embodiment 3
As shown in figure 5, repeating embodiment 2, only preheats and be equipped with reduction activator atomising device 4 in two sections of PH.Reduction is lived Agent atomising device 4 includes nozzle 401.The top inside two sections of PH of preheating is arranged in nozzle 401.
Embodiment 4
As shown in fig. 6, repeating embodiment 3, only reduction activator atomising device 4 further includes reducing agent holding vessel 402, helps Agent holding vessel 403, auxiliary agent conveyance conduit L7, water conveyance conduit L8, reduction activator conveyance conduit L9.Auxiliary agent conveyance conduit L7 connects Connect reducing agent holding vessel 402 and auxiliary agent holding vessel 403.Water conveyance conduit L8 is connected to reducing agent holding vessel 402.Reduction activator Conveyance conduit L9 connection reducing agent holding vessel 402 and nozzle 401.Reduction activator conveyance conduit L9 is equipped with flow control valve 404。
Embodiment 5
As shown in fig. 7, repeating embodiment 4, only the production system further includes compressed air storage tank 5, air delivery pipe Road L10.Airflow pipe L10 connection compressed air storage tank 5 and nozzle 401.
Embodiment 6
Embodiment 5 is repeated, multiple nozzles 401 are only equipped in the DDD of down-draft drying zone, multiple nozzles 401 are evenly arranged in On length direction and width direction in the DDD of down-draft drying zone.The section that two sections of PH set 5 along its length is preheated, each In section in the width direction on be uniformly provided with multiple nozzles 401.
Embodiment 7
Embodiment 6 is repeated, temperature-detecting device 601 is only equipped in the DDD of down-draft drying zone.Third pipeline L3 is equipped with the One NOx flow detector 602.Third pipeline L3 is equipped with reduction activator flow detector 603.It is set on 6th pipeline L6 There is the 2nd NOx flow detector 604.Second pipe L2 is equipped with flue gas flow monitoring device 605.Second pipe L2 is equipped with 3rd NOx flow detector 606.
The 7th pipeline connection L11, the air outlet with preheated one-section TPH being connect with the air outlet 304 of down-draft drying zone DDD 8th pipeline L12 of 306 connections is connected to chimney 7 after passing through desulfurization process device and deduster after merging.Third pipeline L3 It is equipped with deduster 8.
Embodiment 8
As shown in Figure 1, a kind of low NO of grate-kiln pelletizingxProduction technology, the production technology the following steps are included:
1) green-ball is on drying grate 1 successively by blasting drying period UDD, down-draft drying zone DDD, preheated one-section TPH and pre- Two sections of PH of heat are heated, subsequently into successively cold by ring cold one section of C1, ring by roasting, then on ring cold machine C in rotary kiln 2 Two sections of C2 and the cold three sections of C3 of ring are cooled down, and acid pellet is obtained；
2) cooling wind temperature after the cold one section of C1 of ring increases, and then the wind by the cold one section of C1 discharge of ring is delivered to rotary kiln Pellet roasting is participated in 2, the hot wind discharged from rotary kiln 2 is delivered to two sections of PH of preheating of drying grate 1；The hot wind is in two sections of preheating It is delivered to down-draft drying zone DDD after carrying out heat exchange with green-ball in PH, then the exhaust outlet discharge of down-draft drying zone DDD；
3) it is increased by the cooling wind temperature of the cold two sections of C2 of ring, the wind of the cold two sections of C2 discharge of ring is delivered to drying grate 1 Preheated one-section TPH, and heat exchange is carried out with green-ball in preheated one-section TPH, green-ball is preheated, then from the row of preheated one-section TPH Air port discharge；
4) it is increased by the cooling wind temperature of the cold three sections of C3 of ring, the wind of the cold three sections of C3 discharge of ring is delivered to drying grate 1 Blasting drying period UDD, and heat exchange is carried out with green-ball in blasting drying period UDD, then from the exhaust outlet of blasting drying period UDD Discharge；
In the DDD of down-draft drying zone, position above green-ball sprays into reduction activator, reduction activator with from revolution Kiln 2 enters NO contained in the hot wind in the DDD of down-draft drying zonexSCR denitration is realized in reaction.
Reduction activator includes reducing agent and auxiliary agent, and reducing agent is ammonia, and auxiliary agent is saturation NaCl solution.It is dry in exhausting While spraying into reduction activator in the section DDD and/or cold two sections of C2 of ring, compressed air is sprayed into.It is dilute that water is added in reduction activator Down-draft drying zone DDD is sprayed into after releasing again.
This technique sprays into reduction activator in the DDD of down-draft drying zone, inputs the flue gas in the DDD of down-draft drying zone with the section Green-ball on drying grate is reaction bedding, carries out SCR with reduction activator and reacts, removes the nitrogen oxides of flue gas.By this hair After bright process, from the flue gas that down-draft drying zone DDD is discharged, NOxContent is 89mg/Nm3。
Embodiment 9
As shown in Fig. 2, a kind of low NO of grate-kiln pelletizingxProduction technology, the production technology the following steps are included:
1) green-ball is on drying grate 1 successively by blasting drying period UDD, down-draft drying zone DDD, preheated one-section TPH and pre- Two sections of PH of heat are heated, subsequently into successively cold by ring cold one section of C1, ring by roasting, then on ring cold machine C in rotary kiln 2 Two sections of C2 and the cold three sections of C3 of ring are cooled down, and acid pellet is obtained；
2) cooling wind temperature after the cold one section of C1 of ring increases, and then the wind by the cold one section of C1 discharge of ring is delivered to rotary kiln Pellet roasting is participated in 2, the hot wind discharged from rotary kiln 2 is delivered to two sections of PH of preheating of drying grate 1；The hot wind is in two sections of preheating It is delivered to down-draft drying zone DDD after carrying out heat exchange with green-ball in PH, then the exhaust outlet discharge of down-draft drying zone DDD；
3) it is increased by the cooling wind temperature of the cold two sections of C2 of ring, the wind of the cold two sections of C2 discharge of ring is delivered to drying grate 1 Preheated one-section TPH and down-draft drying zone DDD, and in preheated one-section TPH with green-ball carry out heat exchange, preheat green-ball, then from The exhaust outlet of preheated one-section TPH is discharged；
4) it is increased by the cooling wind temperature of the cold three sections of C3 of ring, the wind of the cold three sections of C3 discharge of ring is delivered to drying grate 1 Blasting drying period UDD, and heat exchange is carried out with green-ball in blasting drying period UDD, then from the exhaust outlet of blasting drying period UDD Discharge；
In the DDD of down-draft drying zone, position above green-ball sprays into reduction activator, reduction activator with from revolution Kiln 2 enters NO contained in the hot wind in the DDD of down-draft drying zonexSCR denitration is realized in reaction.The wind tune of the cold two sections of C2 discharge of ring In the range of temperature in section down-draft drying zone DDD is 250-500 DEG C.
This technique sprays into reduction activator in the DDD of down-draft drying zone, inputs the flue gas in the DDD of down-draft drying zone with the section Green-ball on drying grate is reaction bedding, meanwhile, the part wind of the cold two sections of C2 discharge of ring is delivered to down-draft drying zone DDD, really The temperature in the DDD of down-draft drying zone is protected in the range of 250-500 DEG C, for the temperature of optimum SCR reaction；Nitrogen oxygen in flue gas Compound carries out SCR with reduction activator and reacts, and removes the nitrogen oxides of flue gas.After process of the invention, from exhausting In the flue gas of dryer section DDD discharge, NOxContent is 66mg/Nm3。
Embodiment 10
Embodiment 9 is repeated, is only being preheated in two sections of PH, the position above green-ball sprays into reduction activator.Reduction Activator and NO contained in the hot wind entered in two sections of PH of preheatingxSNCR denitration is realized in reaction.In two sections of PH of control preheating In the range of temperature is 800-1100 DEG C.Down-draft drying zone DDD and ring cold two are sprayed into again after water dilution is added in reduction activator In section C2.It is within the scope of 300-450 DEG C that the wind of the cold two sections of C2 discharge of ring, which adjusts the temperature in the DDD of down-draft drying zone,.
This technique, down-draft drying zone DDD is interior to carry out out of stock processing at a temperature of optimum SCR reaction, preheats two sections of PH The out of stock processing of interior progress SNCR, preheat two sections escape reduction activator with flue gas enter together in the DDD of down-draft drying zone after It is continuous to utilize.After process of the invention, from the flue gas that down-draft drying zone DDD is discharged, NOxContent is 41mg/Nm3。
Embodiment 11
Embodiment 10 is repeated, is only preheating in two sections of PH, is being equipped with reduction activator atomising device.Reduction activator atomization Device includes multiple nozzles.It preheats a length of 10m of two sections of PH, width 4m, be highly 3m, the exhaust gas volumn of two sections of PH of input preheating is 162000m3/ h will preheat two sections of PH and set 4 sections along its length.Each section is equipped with nozzle.Set nozzle away from Height distance from mineral aggregate charge level in drying grate 1 is h.Detect the NOx flow in the unit time in two sections of PH of input preheating 300mg/m3, calculating processing flow is Q1Be reduction activator needed for NOx theoretical amount 434L/h, reduction activator With NOxThe reaction time of reaction is 0.8s, passes through calculating: distinguished and admirable horizontal velocity V in two sections of PH drying grates of preheating1For 3.75m/ s；Preheat vertical speed V distinguished and admirable in two sections of PH drying grates2For 1.125m/s；Preheat two sections of PH drying grate setting section number n It is 4；Each siding-to-siding block length d for preheating the setting of two sections of PH drying grates is 2.5m；The height of mineral aggregate charge level in nozzle distance drying grate Degree distance h is 0.75m；
The straying quatity for controlling reduction activator in each section, in the unit time, the 1st section reduction activator is sprayed into Measure U1For 27.13L/h；2nd section reduction activator straying quatity U2For 25.43L/h；3rd section reduction activator straying quatity U3For 23.84L/h；4th section reduction activator straying quatity U4For 22.35L/h.
This technique is close by the straying quatity of reduction activator and the selection of each position in two sections of PH of rationally control preheating The amount that the nozzle of rotary kiln position sprays into is larger, and the amount that the nozzle far from rotary kiln position sprays into is smaller.The each spray of rational deployment The straying quatity of mouth, makes full use of reduction activator, improves the denitration efficiency of SNCR.After process of the invention, from pumping In the flue gas of wind dryer section DDD discharge, NOxContent is 35mg/Nm3。
Embodiment 12
Embodiment 11 is repeated, only in the DDD of down-draft drying zone, the straying quatity of reduction activator is U, detects the unit time NOx flow 180mg/m in interior input down-draft drying zone DDD3, reduction activator needed for calculating processing flow NOx Theoretical amount 260L/h, it is 10L/ that detection, which escapes into the reduction activation agent flux in the DDD of down-draft drying zone from two sections of PH of preheating, H, the then straying quatity of the reduction activator sprayed into the unit time in the DDD of down-draft drying zone are 250L/h.
This technique makes full use of reduction activation by the straying quatity of reduction activator in rationally control down-draft drying zone DDD Agent avoids the escape of reducing agent, causes to waste, while improving the denitration efficiency of SNCR.
Embodiment 13
Embodiment 12 is repeated, only reducing agent is urea, and auxiliary agent is ammonium metavanadate.

Claims (12)

1. a kind of low NO of grate-kiln pelletizingxProduction technology, the production technology the following steps are included:
1) green-ball successively passes through blasting drying period (UDD), down-draft drying zone (DDD), preheated one-section (TPH) on drying grate (1) And two sections of preheating (PH) is heated, subsequently into successively cold by ring by roasting, then on ring cold machine (C) in rotary kiln (2) One section (C1), ring cold two sections (C2) and ring cold three sections (C3) are cooled down, and acid pellet is obtained；
2) cooling wind temperature after ring cold one section (C1) increases, and then the wind by cold one section (C1) discharge of ring is delivered to rotary kiln (2) pellet roasting is participated in, the hot wind discharged from rotary kiln (2) is delivered to two sections of preheating (PH) of drying grate (1)；The hot wind exists It is delivered to down-draft drying zone (DDD) after carrying out heat exchange with green-ball in two sections of preheating (PH), then the row of down-draft drying zone (DDD) Air port discharge；
3) it is increased by the cooling wind temperature of ring cold two sections (C2), the wind of cold two sections (C2) discharge of ring is delivered to drying grate (1) Preheated one-section (TPH), and carry out heat exchange with green-ball in the preheated one-section (TPH), green-ball preheated, then from preheated one-section (TPH) exhaust outlet discharge；
4) it is increased by the cooling wind temperature of ring cold three sections (C3), the wind of cold three sections (C3) discharge of ring is delivered to drying grate (1) Blasting drying period (UDD), and heat exchange is carried out with green-ball in the blasting drying period (UDD), then from blasting drying period (UDD) Exhaust outlet discharge；
It is characterized by: the position above green-ball sprays into reduction activator, reduction activation in down-draft drying zone (DDD) Agent and NO contained in the hot wind entered in down-draft drying zone (DDD) from rotary kiln (2)xSCR denitration is realized in reaction.
2. production technology according to claim 1, it is characterised in that: the wind of cold two sections (C2) discharge of ring is delivered to chain and is combed The wind of the preheated one-section (TPH) and down-draft drying zone (DDD) of machine (1), cold two sections (C2) discharge of ring adjusts down-draft drying zone (DDD) Interior temperature is 250-500 DEG C, preferably 300-450 DEG C, more preferably 350-420 DEG C；And/or
In preheating two sections (PH), the position above green-ball sprays into reduction activator, reduction activator and enters preheating two NO contained in hot wind in section (PH)xSNCR denitration is realized in reaction；Preferably, the temperature in two sections of preheating (PH) is 800-1100 DEG C, preferably 850-1050 DEG C, more preferably 900-1000 DEG C.
3. production technology according to claim 2, it is characterised in that: in two sections of preheating (PH), be equipped with reduction activator Atomising device, reduction activator atomising device include multiple nozzles；It preheats a length of a of two sections (PH), width b, be highly c, it is defeated The exhaust gas volumn for entering preheating two sections (PH) is S, and two sections of preheating (PH) is set n section along its length；Each section is all provided with There is nozzle, sets the height distance of the interior mineral aggregate charge level of nozzle distance drying grate (1) as h, input preheats two in the detection unit time NOx flow Q in section (PH)1, calculating processing flow is Q1Be reduction activator needed for NOx theoretical amount U0, reduction Activator and NOxThe reaction time of reaction is t, passes through following calculating:
Preheat horizontal velocity V distinguished and admirable in two sections of (PH) drying grates1Are as follows:
Preheat vertical speed V distinguished and admirable in two sections of (PH) drying grates2Are as follows:
Section number n is arranged in two sections of (PH) drying grates of preheating are as follows:
Preheat each siding-to-siding block length d of two sections of (PH) drying grates setting are as follows:
The height distance h of mineral aggregate charge level in nozzle distance drying grate are as follows:
The straying quatity for controlling reduction activator in each section, in the unit time,
1st section reduction activator straying quatity U1Are as follows:
2nd section reduction activator straying quatity U2Are as follows:
……
N-th of section reduction activator straying quatity UnAre as follows:
4. production technology according to claim 2 or 3, it is characterised in that: in down-draft drying zone (DDD), reduction activation The straying quatity of agent is U, the NOx flow Q in the detection unit time in input down-draft drying zone (DDD)2, calculate and handle the flow The theoretical amount U of reduction activator needed for NOx0', detection escapes into down-draft drying zone (DDD) from preheating two sections (PH) Reduction activation agent flux be U ', then the straying quatity of the reduction activator sprayed into down-draft drying zone (DDD) the interior unit time is U =U0’-U’。
5. production technology according to claim 4, it is characterised in that: in the SNCR denitration reaction in two sections of preheating (PH), U0 =k1*Q1；Wherein, k1To calculate gained coefficient according to the ammonia nitrogen ratio (NSR) of the interior SNCR denitration reaction of two sections of preheating (PH)；And/or
In SCR denitration reaction in down-draft drying zone (DDD), U0'=k2*Q2；Wherein, k2For according in down-draft drying zone (DDD) The ammonia nitrogen ratio (NSR) of SCR denitration reaction calculates gained coefficient；And/or
Reduction activator and NOxThe reaction time t of reaction is more than or equal to 0.5 second, preferably 0.6-2 seconds, more preferably 0.7-1.5 Second, more preferably 0.8-1.2 seconds.
6. production technology according to any one of claims 1-5, it is characterised in that: the reduction activator includes reduction Agent and auxiliary agent；Preferably, reducing agent is one of ammonia, ammonium hydroxide, urea or a variety of, auxiliary agent NaCl, contains vanadium solution, is situated between One of hole/micropore nanophase materials are a variety of；And/or
While spraying into reduction activator in down-draft drying zone (DDD) and/or ring cold two sections (C2), compressed air is sprayed into；Make It is sprayed into down-draft drying zone (DDD) and/or ring cold two sections (C2) again after water dilution is added to be preferred, in reduction activator.
7. a kind of low NO of grate-kiln pelletizingxProduction system or for production technology described in any one of claim 1-6 Pelletizing production system, which includes: drying grate (1), rotary kiln (2), ring cold machine (C)；Wherein: being moved towards according to technique, institute It states drying grate (1) and is disposed with two sections of blasting drying period (UDD), down-draft drying zone (DDD), preheated one-section (TPH) and preheating (PH), ring cold machine (C) cold three sections (C3), the tail of rotary kiln (2) that is disposed with ring cold one section (C1), ring cold two sections (C2) and ring Two sections of preheating (PH) rings that ring cold machine (C) is connected with the other end of end connection drying grate (1) are cold one section (C1)；
Wherein: the air outlet (C1b) of ring cold one section (C1) is connected to the air inlet of rotary kiln (2) via first pipe (L1) (201), the air outlet (202) of rotary kiln (2) is connected to the air inlet (301) of preheating two sections (PH) via second pipe (L2), The air outlet (302) of preheating two sections (PH) is connected to the air inlet (303) of down-draft drying zone (DDD) by third pipeline (L3)；
The air outlet (C2b) of ring cold two sections (C2) is connected to the air inlet of preheated one-section (TPH) via the 4th pipeline (L4) (305)；The air outlet (C3b) of ring cold three sections (C3) is connected to the air inlet of blasting drying period (UDD) via the 5th pipeline (L5) (307)；
It is characterized by: reduction activator atomising device (4) are equipped in down-draft drying zone (DDD), reduction activator atomising device It (4) include nozzle (401), nozzle (401) the setting top internal at down-draft drying zone (DDD).
8. production system according to claim 7, it is characterised in that: it is the 6th pipe that the 4th pipeline (L4), which separates a branch, Road (L6), the 6th pipeline (L6) are connected to the air inlet (303) of down-draft drying zone (DDD)；And/or
Reduction activator atomising device (4) are equipped in two sections of preheating (PH), reduction activator atomising device (4) includes nozzle (401), nozzle (401) the setting top internal in two sections of preheating (PH).
9. production system according to claim 7 or 8, it is characterised in that: reduction activator atomising device (4) further includes Former agent holding vessel (402), auxiliary agent holding vessel (403), auxiliary agent conveyance conduit (L7), water conveyance conduit (L8), reduction activator are defeated Send pipeline (L9)；Auxiliary agent conveyance conduit (L7) connects reducing agent holding vessel (402) and auxiliary agent holding vessel (403), water conveyance conduit (L8) it is connected to reducing agent holding vessel (402), reduction activator conveyance conduit (L9) connects reducing agent holding vessel (402) and nozzle (401)；Preferably, reduction activator conveyance conduit (L9) is equipped with flow control valve (404)；And/or
The production system further includes compressed air storage tank (5), airflow pipe (L10), airflow pipe (L10) connection Compressed air storage tank (5) and nozzle (401).
10. the production system according to any one of claim 7-9, it is characterised in that: be equipped in down-draft drying zone (DDD) One or more nozzles (401)；Preferably, multiple nozzles (401) are equipped in down-draft drying zone (DDD), multiple nozzles (401) It is evenly arranged on the length direction and width direction in down-draft drying zone (DDD)；And/or
Two sections of preheating (PH) sets n section along its length, and one or more nozzles (401) are equipped in each section；Make To be preferred, in each section in the width direction on be uniformly provided with multiple nozzles (401).
11. the production system according to any one of claim 7-10, it is characterised in that: set in down-draft drying zone (DDD) Have temperature-detecting device (601), third pipeline (L3) is equipped with the first NOx flow detector (602), on third pipeline (L3) Equipped with reduction activator flow detector (603), the 6th pipeline (L6) is equipped with the 2nd NOx flow detector (604)； And/or
Second pipe (L2) is equipped with flue gas flow monitoring device (605), and second pipe (L2) is equipped with the 3rd NOx flow detection Device (606).
12. production system according to any one of claims 7-11, it is characterised in that: with down-draft drying zone (DDD) The 7th pipeline connection (L11) of air outlet (304) connection, the 8th pipeline being connect with the air outlet (306) of preheated one-section (TPH) (L12) by being connected to chimney (7) after desulfurization process device and/or deduster after merging, preferably, third pipeline (L3) It is equipped with deduster (8)；And/or
The air inlet (C2a) of air inlet (C1a), the ring cold two sections (C2) of ring cold one section (C1) and the air inlet of ring cold three sections (C3) (C3a) it is connected with blower (9)；The air outlet (308) of blasting drying period (UDD) is connected to chimney by the 9th pipeline (L13) (7)。
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