CN109876662A - SCR denitration system and method for denitration suitable for cement producing line kiln exit gas - Google Patents

SCR denitration system and method for denitration suitable for cement producing line kiln exit gas Download PDF

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Publication number
CN109876662A
CN109876662A CN201910320326.5A CN201910320326A CN109876662A CN 109876662 A CN109876662 A CN 109876662A CN 201910320326 A CN201910320326 A CN 201910320326A CN 109876662 A CN109876662 A CN 109876662A
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China
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flue
temperature
flue gas
denitration
scr
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朱廷钰
郭旸旸
朱思佳
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Institute of Process Engineering of CAS
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Institute of Process Engineering of CAS
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Priority to CN201910320326.5A priority Critical patent/CN109876662A/en
Publication of CN109876662A publication Critical patent/CN109876662A/en
Priority to PCT/CN2019/106075 priority patent/WO2020211280A1/en
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D50/00Combinations of methods or devices for separating particles from gases or vapours
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/54Nitrogen compounds
    • B01D53/56Nitrogen oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/90Injecting reactants

Abstract

The present invention relates to the SCR denitration systems and method of denitration that are suitable for cement producing line kiln exit gas, branch flue is added on high-temperature flue, it is adapted flue-gas temperature and catalyst window temperature into SCR reactor by way of drawing temperature adjustment flue gas, and then by NO in SCR denitration reaction devicexEfficiently and economically remove.After SCR denitration reaction device is arranged in kiln tail bag filter simultaneously by the present invention, and hot precipitator is set on branch flue, the flue dust into SCR reactor is greatly decreased, solves catalyst blockage poisoning problem, extends the service life of catalyst.System and method provided by the invention improve the feasibility and economy that SCR denitration technology is applied to manufacture of cement industry, are cement producing line NOxThe raising of discharge standard provides technological guidance, with good economic efficiency and application prospect.

Description

SCR denitration system and method for denitration suitable for cement producing line kiln exit gas
Technical field
The present invention relates to flue gases purification fields, and in particular to the SCR denitration suitable for cement producing line kiln exit gas System and method of denitration.
Background technique
Currently, the NO of China's cement industryxDischarge amount account for national NOx10% or so of total release, comes thermal power generation With the third position after motor vehicle exhaust emission.Currently performed " the cement industry air pollution emission standard " GB4915- in China 2013 require existing and newly-built cement production enterprise NOxDischarge≤400mg/Nm3, key area is adjusted to≤320mg/Nm3.Somely Area even proposes more stringent discharge standard, such as " the cement industry atmosphere that the Hebei province environmental protection Room is issued in April, 2018 Pollutant minimum discharge standard (exposure draft) " in suggest, from the year two thousand twenty January 1, cement production enterprise NOxDischarge is not Greater than 150mg/Nm3;It prints and distributes in the environmental protection Room about development the whole province's non-electrical industry NO in Jiangsu Province in 2017xThe notice of depth emission reduction, it is desirable that NO before cement industry on June 1st, 2019xDischarge is not higher than 100mg/Nm3.Therefore cement industry urgent need is employed new technology, new process To meet increasingly stringent discharge standard.
Industrial smoke denitrating technique mainly selective non-catalytic reduction (SNCR) denitration technology and selective catalytic reduction (SCR) denitration technology, the SNCR technology that cement kiln generallys use at present, NOxRemoval efficiency is 60% or so, it is difficult to meet increasingly Stringent discharge standard.And SCR gas denitrifying technology have reaction condition it is mild, denitration efficiency height (90%) the features such as, be phase To feasible technology.SCR is highly developed in Thermal Power Generation Industry, but the working condition of cement producing line, limits it in water The application of mud industry.Cement kiln end flue gas content of ashes is high, is easy to cause catalyst blockage;CaO content is high in flue dust, with cigarette SO in gas3React the CaSO generated4It is covered on catalyst surface, easily causes SCR catalyst poisoning and deactivation.
For the high dirt of flue gas and the easy poisoning problem of catalyst, CN204543995U discloses a kind of cement kiln end low-temperature flue gas SCR denitration device, denitrification apparatus are arranged in after cement kiln end dust-precipitator, by the purifying smoke after kiln tail dust-precipitator, With reductant supply system supply, the reducing agent injection apparatus being arranged on the preposition flue of low-temperature denitration device is sprayed to flue Interior reducing agent together, enters after the medium temperature denitrification apparatus equipped with catalyst carries out denitration after mixing and is emitted into cement kiln end On flue before exhaust blower entrance, final purification flue gas enters kiln tail smoke stack emission.SCR denitration reaction device is arranged in by the technology After dust-precipitator, solves the problems such as catalyst blockage poisoning.But the flue-gas temperature for entering SCR denitration reaction device is low, though using Low temperature catalyst of the use temperature range at 80-150 DEG C, but at present for the research and development of low temperature catalyst also not at It is ripe, limit the application of this technology.
CN107596917A discloses the SNCR-SCR device and technique of a kind of cement clinker production line kiln exit gas, utilizes The ammonium hydroxide evaporation of (340-360 DEG C) of medium temperature flue gas of kiln tail preheater downstream realization SCR denitration section, with from kiln tail chimney via dilute It is sent into SCR reactor after releasing (90-110 DEG C) of the low-temperature flue gas mixing that blower is introduced into, the flue-gas temperature into SCR reactor is full The requirement of sufficient conventional scr catalyst, can be such that denitration reaction efficiently carries out.But SCR reactor is directly arranged at by the technique After kiln tail preheater, the flue gas into reactor carries a large amount of dust, easily causes SCR catalyst blocking poisoning, contracting Shot-catalyst agent service life.
Summary of the invention
In view of problems of the prior art, the purpose of the present invention is to provide one kind to be suitable for cement producing line kiln tail The SCR denitration system of flue gas and the method for carrying out denitration using the system, can be with the removing cement kiln end flue gas of high-efficiency and economic In NOx, while solving the problems, such as that SCR technology applies the catalyst in cement kiln end flue gas easily to block easy poisoning, extension is urged The shelf life of agent.
To achieve this purpose, the present invention adopts the following technical scheme:
In a first aspect, the present invention provides a kind of SCR denitration system suitable for cement producing line kiln exit gas, the system System includes: kiln tail high-temperature flue 1, main road flue 3, waste heat boiler 4, raw mill 5, bag filter 6, flue gas heat-exchange unit 7, branch Flue 9, hot precipitator 10, high-temperature blower 11, smoke regulating valve 12, reducing agent injection apparatus 13, SCR reactor 14, main wind Machine 15 and chimney 16;
Wherein, the kiln tail high-temperature flue 1 is connect with main road flue 3 and branch flue 9 respectively, on the main road flue 3 Be connected in turn waste heat boiler 4, raw mill 5, bag filter 6,7 cold wind road of flue gas heat-exchange unit, reducing agent injection apparatus 13, SCR reactor 14, main air blower 15,7 hot wind road of flue gas heat-exchange unit and chimney 16;High temperature is connected in turn on the branch flue 9 Deduster 10, high-temperature blower 11 and smoke regulating valve 12, then with the 7 cold wind road of flue gas heat-exchange unit and reducing agent injection apparatus Main road flue 3 between 13 converges.
In order to which the flue-gas temperature for entering reactor to be promoted to the window temperature with catalyst-compatible, the present invention is in kiln tail The kiln tail high-temperature flue of preheater connection is equipped with branch flue, draws flue gas all the way and is used to adjust flue-gas temperature, this road temperature adjustment Flue gas finally imports on the main road pipeline before Benitration reactor.Branch flue is equipped with smoke regulating valve, can be according to required temperature Degree adjusts temperature adjustment flue gas air quantity.
In system provided by the invention, SCR denitration reaction device is arranged in after kiln tail bag filter, while branch flue It is equipped with hot precipitator, the flue dust into SCR reactor can be greatly decreased, solve catalyst blockage poisoning problem, is extended The service life of catalyst.
Flue gas heat-exchange unit is arranged after main road bag filter the present invention, and main road flue gas and branch flue gas mix it Before.Wherein, the cold wind road of the flue gas heat-exchange unit is connect with bag filter, and hot wind road is connect with main air blower, bag filter Treated, and main road flue gas enters the cold wind road of flue gas heat-exchange unit, converges after heating with branch temperature adjustment flue gas;SCR denitration reaction device Treated, and cleaning high-temp flue gas enters the hot wind road of flue gas heat-exchange unit by main air blower, drains into atmosphere by chimney after cooling.
Preferably, the system also includes reducing agent vaporising device 17, the reducing agent vaporising device 17 is sprayed with reducing agent Injection device 13 connects.The reducing agent vaporising device 17 according to what the reducing agent type of selection was adapted therewith can select, The present invention is not specifically limited.
Preferably, the hot precipitator 10 is any one in electric precipitator, bag filter or cyclone dust collectors.
Preferably, the type of the reducing agent injection apparatus 13 is any one in grid type, vortex patern or mixed type.
Preferably, the SCR reactor 14 includes deflector, soot blower and catalyst bed.Wherein, deflector can be with The reducing agent of main road flue gas, branch temperature adjustment flue gas and penetrating is uniformly mixed;Soot blower can select acoustic wave ash ejector or Steam sootblower preferentially selects steam sootblower;Catalyst bed can choose with two for one, with three for one or with five for one Deng can specifically be adjusted according to actual needs.
Preferably, the kiln tail high-temperature flue 1, main road flue 3 and branch flue 9 pass through 2 and of kiln tail high-temperature flue threeway Flue gas mixing tee 8 is attached.
Second aspect, the present invention provides a kind of SCR denitration method suitable for cement producing line kiln exit gas, the sides Method carries out denitration, concrete operations are as follows: kiln exit gas is divided into two after entering kiln tail high-temperature flue 1 using system described in first aspect Road enters main road flue 3 all the way, successively passes through waste heat boiler 4 and raw mill 5, after 6 dedusting of bag filter, into Enter the heat exchange heating of 7 cold wind road of flue gas heat-exchange unit;Another way enters branch flue 9, successively passes through hot precipitator 10, high-temperature blower 11 and smoke regulating valve 12, then converge with the main road flue gas after heating, the flue gas after converging is sprayed through reducing agent injection apparatus 13 After entering reducing agent, denitration is carried out into SCR reactor 14, the purified flue gas of denitration enters flue gas heat-exchange unit 7 through main air blower 15 After the heat exchange cooling of hot wind road, atmosphere is emitted by chimney 16;Wherein, branch flue gas flow is adjusted by smoke regulating valve 12, Control converges catalyst reaction temperatures window in the temperature and SCR reactor 14 of rear flue gas and is adapted.
Preferably, the temperature for converging rear flue gas can be 200-280 DEG C, such as can be 200 DEG C, 210 DEG C, 220 DEG C, 230 DEG C, 240 DEG C, 250 DEG C, 260 DEG C, 270 DEG C or 280 DEG C etc., as space is limited and for concise consideration, the present invention is no longer Exclusive list.
Preferably, temperature of the main road flue gas when converging be 150-200 DEG C, such as can be 150 DEG C, 160 DEG C, 170 DEG C, 180 DEG C, 190 DEG C or 200 DEG C etc., as space is limited and for concise consideration, the present invention no longer exclusive list.
Preferably, temperature of the branch flue gas when converging be 300-380 DEG C, such as can be 300 DEG C, 310 DEG C, 320 DEG C, 330 DEG C, 340 DEG C, 350 DEG C, 360 DEG C, 370 DEG C or 380 DEG C etc., as space is limited and for concise consideration, the present invention No longer exclusive list.
Preferably, the temperature for converging rear flue gas is 200-240 DEG C.It can catalyst window temperature according to actual needs The smoke regulating valve on branch flue is adjusted, the inlet of control temperature adjustment flue gas adjusts the temperature for entering flue gas in SCR reactor, It is allowed to match with the reaction temperature window temperature of catalyst, improves removal efficiency.
Preferably, the present invention can be used at least one of ammonium hydroxide, urea or liquefied ammonia as reducing agent and carry out denitration.
The third aspect, the present invention provides a kind of SCR denitration method suitable for cement producing line kiln exit gas, this method SCR denitration system described in first aspect and SNCR system are combined, the denitration for cement producing line kiln exit gas.
SNCR denitration system has been installed on most domestic cement producing line at present, the present invention can be separately installed, It can be combined with SNCR system existing on production line, share reducing agent preparation facilities.After SNCR denitration, it can mitigate SCR reactor load can suitably reduce the catalyst bed number of plies, improve NOxRemoval efficiency reduces operating cost.
Compared with prior art, the present invention is at least had the advantages that
(1) present invention introduces branch flue in existing denitrating system, draws flue gas all the way and is used to adjust flue gas temperature Degree, and can by control flue gas flow flue-gas temperature is adjusted in real time, ensure that into SCR reactor flue-gas temperature and Catalyst window temperature is adapted, and carries out denitration reaction efficiently.
(2) after SCR denitration reaction device is arranged in kiln tail bag filter by the present invention, and height is set on branch flue The flue dust into SCR reactor is greatly decreased in warm deduster, solves catalyst blockage poisoning problem, extends making for catalyst Use the service life.
(3) present invention improves the feasibility and economy that SCR denitration technology is applied to manufacture of cement industry, is cement Production line NOxThe raising of discharge standard provides technological guidance, with good economic efficiency and application prospect.
Detailed description of the invention
Fig. 1 is the structural representation suitable for cement producing line kiln exit gas SCR denitration system that the embodiment of the present invention 1 provides Figure;
In figure: 1- kiln tail high-temperature flue, 2- kiln tail high-temperature flue threeway, 3- main road flue, 4- waste heat boiler, 5- raw material Mill, 6- bag filter, 7- flue gas heat-exchange unit, 8- flue gas mixing tee, 9- branch flue, 10- hot electrostatic precipitator, 11- high Warm blower, 12- branch smoke regulating valve, 13- reducing agent injection apparatus, 14-SCR reactor, 15- main air blower, 16- chimney, 17- Reducing agent vaporising device.
The present invention is described in more detail below.But following embodiments is only simple example of the invention, not It represents or limitation the scope of the present invention, protection scope of the present invention is subject to claims.
Specific embodiment
To further illustrate the technical scheme of the present invention below with reference to the accompanying drawings and specific embodiments.
In order to better illustrate the present invention, it is easy to understand technical solution of the present invention, of the invention is typical but non-limiting Embodiment is as follows:
Embodiment 1
A kind of SCR denitration system suitable for cement producing line kiln exit gas is present embodiments provided, as shown in Figure 1, institute The system of stating includes: the connection kiln tail high-temperature flue threeway 2 of kiln tail high-temperature flue 1 after kiln tail preheater, by threeway rear pass point For two-way: main road flue 3 and branch flue 9;
Wherein, waste heat boiler 4, raw mill 5, bag filter 6 and flue gas heat-exchange unit 7, cloth are successively arranged on main road flue 3 Bag dust collector 6 is connected with 7 cold wind road of flue gas heat-exchange unit, and reducing agent injection apparatus 13, SCR reactor are equipped with after flue gas heat-exchange unit 7 14 and main air blower 15, main air blower 15 connect with 7 hot wind road of flue gas heat-exchange unit, then connect with chimney 16;
Hot precipitator 10, high-temperature blower 11 and smoke regulating valve 12 are successively arranged on branch flue 9, then with main road cigarette Converged between flue gas heat-exchange unit 7 and reducing agent injection apparatus 13 by flue gas mixing tee 8 in road 3.
The system also includes reducing agent vaporising devices 17, connect with reducing agent injection apparatus 13, are used for reducing agent Gasification enters injection apparatus.
Wherein, the flue gas heat-exchange unit 7 includes cold wind road and hot wind road, carries out heat exchange therebetween, and cold wind road is used It heats up in main road flue gas, hot wind road is for cooling down to purified flue gas.
The hot precipitator 10 can be any one in electric precipitator, bag filter or cyclone dust collectors.
The type of the reducing agent injection apparatus 13 can be any one in grid type, vortex patern or mixed type.
14 internal structure of SCR reactor includes deflector, soot blower, catalyst bed, wherein the soot blowing dress Acoustic wave ash ejector or steam sootblower can be selected by setting, the catalyst bed can choose with two for one, with three for one or With five for one.
Embodiment 2
It is real to carry out denitration on the new dry process rotary kiln production line of a 4500t/d for the device provided using embodiment 1 It tests, this cement producing line has installed SNCR denitration device.The dust content of kiln tail high-temperature flue gas is 60g/Nm3, temperature 380 DEG C, NOxConcentration is 300mg/Nm3, flue gas flow 450000Nm3/h。
Main road flue gas enters main road flue, successively recycles heat by waste heat boiler, and raw mill dries raw material, bag-type dust After device dedusting, into flue gas mixer cold wind road, the temperature of flue gas is 120 DEG C, after exchanging heat, flue gas at cold wind way outlet at this time Temperature is 180 DEG C.Temperature adjustment flue gas enters branch flue, through high temperature electric precipitation, after high-temperature blower, reaches temperature when flue gas point Degree is 360 DEG C.Selecting reaction temperature is 220 DEG C of catalyst, using the flow of smoke regulating valve control temperature adjustment flue gas, by main road After the ratio of exhaust gas volumn and temperature adjustment exhaust gas volumn is adjusted to 3.5:1, it can match with catalyst reaction window temperature.After converging Flue gas is after reducing agent injection apparatus sprays into reducing agent, into carrying out denitration in SCR reactor, the smoke temperature change after denitration Less, enter flue gas heat-exchange unit hot wind road through main air blower, flue-gas temperature is 120 DEG C after heat exchange, through smoke stack emission to atmosphere.
It is 20% ammonium hydroxide that reducing agent, which selects concentration, in the present embodiment, and reducing agent injection apparatus uses grid type, catalyst Bed use with three for one arrangement, catalyst cross-sectional aperture be 0.5cm, using rake steam sootblowers, frequency of soot blowing For weekly, after denitration, NO in the flue gas of dischargexConcentration be 32.5mg/Nm3
Embodiment 3
It is real to carry out denitration on the new dry process rotary kiln production line of a 3200t/d for the device provided using embodiment 1 It tests.The dust content of kiln tail high-temperature flue gas is 40g/Nm3, temperature is 360 DEG C, NOxConcentration is 420mg/Nm3, flue gas flow is 420000Nm3/h。
Main road flue gas enters main road flue, successively recycles heat by waste heat boiler, and raw mill dries raw material, bag-type dust After device dedusting, into flue gas mixer cold wind road, the temperature of flue gas is 110 DEG C, after exchanging heat, flue gas at cold wind way outlet at this time Temperature is 160 DEG C.Temperature adjustment flue gas enters branch flue, through high temperature electric precipitation, after high-temperature blower, reaches temperature when flue gas point Degree is 340 DEG C.Selecting reaction temperature is 200 DEG C of catalyst, using the flow of smoke regulating valve control temperature adjustment flue gas, by main road After the ratio of exhaust gas volumn and temperature adjustment exhaust gas volumn is adjusted to 3.5:1, it can match with catalyst reaction window temperature.After converging Flue gas is after reducing agent injection apparatus sprays into reducing agent, into carrying out denitration in SCR reactor, the smoke temperature change after denitration Less, enter flue gas heat-exchange unit hot wind road through main air blower, flue-gas temperature is 115 DEG C after heat exchange, through smoke stack emission to atmosphere.
Reducing agent selects urea in the present embodiment, and reducing agent injection apparatus uses grid type, and catalyst bed is used with three Standby one arrangement, catalyst cross-sectional aperture are 1.0cm, and using rake steam sootblowers, frequency of soot blowing is biweekly.It is de- After nitre, NO in the flue gas of dischargexConcentration be 38.2mg/Nm3
Embodiment 4
It is real to carry out denitration on the new dry process rotary kiln production line of a 2000t/d for the device provided using embodiment 1 It tests.The dust content of kiln tail high-temperature flue gas is 18g/Nm3, temperature is 340 DEG C, NOxConcentration is 190mg/Nm3, flue gas flow is 28000Nm3/h。
Main road flue gas enters main road flue, successively recycles heat by waste heat boiler, and raw mill dries raw material, bag-type dust After device dedusting, into flue gas mixer cold wind road, the temperature of flue gas is 110 DEG C, after exchanging heat, flue gas at cold wind way outlet at this time Temperature is 150 DEG C.Temperature adjustment flue gas enters branch flue, through high temperature electric precipitation, after high-temperature blower, reaches temperature when flue gas point Degree is 320 DEG C.Selecting reaction temperature is 200 DEG C of catalyst, using the flow of smoke regulating valve control temperature adjustment flue gas, by main road After the ratio of exhaust gas volumn and temperature adjustment exhaust gas volumn is adjusted to 2.4:1, it can match with catalyst reaction window temperature.After converging Flue gas is after reducing agent injection apparatus sprays into reducing agent, into carrying out denitration in SCR reactor, the smoke temperature change after denitration Less, enter flue gas heat-exchange unit hot wind road through main air blower, flue-gas temperature is 110 DEG C after heat exchange, through smoke stack emission to atmosphere.
Reducing agent selects liquefied ammonia in the present embodiment, and reducing agent injection apparatus uses grid type, and catalyst bed is used with two Standby one arrangement, catalyst cross-sectional aperture are 1.5cm, and using rake steam sootblowers, frequency of soot blowing is biweekly.It is de- After nitre, NO in the flue gas of dischargexConcentration be 22.6mg/Nm3
The Applicant declares that the present invention is explained by the above embodiments detailed construction feature of the invention, but the present invention is simultaneously It is not limited to above-mentioned detailed construction feature, that is, does not mean that the present invention must rely on above-mentioned detailed construction feature and could implement.Institute Belong to those skilled in the art it will be clearly understood that any improvement in the present invention, to the equivalence replacement of component selected by the present invention And increase, selection of concrete mode of accessory etc., all of which fall within the scope of protection and disclosure of the present invention.

Claims (10)

1. a kind of SCR denitration system suitable for cement producing line kiln exit gas, which is characterized in that the system comprises: kiln tail High-temperature flue (1), main road flue (3), waste heat boiler (4), raw mill (5), bag filter (6), flue gas heat-exchange unit (7), branch Road flue (9), hot precipitator (10), high-temperature blower (11), smoke regulating valve (12), reducing agent injection apparatus (13), SCR are anti- Answer device (14), main air blower (15) and chimney (16);
Wherein, the kiln tail high-temperature flue (1) connect with main road flue (3) and branch flue (9) respectively, the main road flue (3) waste heat boiler (4), raw mill (5), bag filter (6), flue gas heat-exchange unit (7) cold wind road, reducing agent are connected in turn Injection apparatus (13), SCR reactor (14), main air blower (15), flue gas heat-exchange unit (7) hot wind road and chimney (16);The branch Be connected with hot precipitator (10), high-temperature blower (11) and smoke regulating valve (12) on flue (9) in turn, then with the flue gas Main road flue (3) between heat exchanger (7) cold wind road and reducing agent injection apparatus (13) converges.
2. the system as claimed in claim 1, which is characterized in that described the system also includes reducing agent vaporising device (17) Reducing agent vaporising device (17) is connect with reducing agent injection apparatus (13).
3. system as claimed in claim 1 or 2, which is characterized in that the hot precipitator (10) is electric precipitator, cloth bag removes Any one in dirt device or cyclone dust collectors.
4. system as described in any one of claims 1-3, which is characterized in that the type of the reducing agent injection apparatus (13) is Any one in grid type, vortex patern or mixed type.
5. system according to any one of claims 1-4, which is characterized in that the SCR reactor (14) includes deflector, blows Apparatus for ash and catalyst bed.
6. system as described in any one in claim 1-5, which is characterized in that the kiln tail high-temperature flue (1), main road flue (3) it is attached with branch flue (9) by kiln tail high-temperature flue threeway (2) and flue gas mixing tee (8).
7. a kind of SCR denitration method suitable for cement producing line kiln exit gas, which is characterized in that the method is wanted using right The described in any item systems of 1-6 are asked to carry out denitration, concrete operations are as follows: kiln exit gas is divided into two after entering kiln tail high-temperature flue (1) Road enters main road flue (3) all the way, successively passes through waste heat boiler (4) and raw mill (5), removes by bag filter (6) After dirt, exchanges heat and heat up into flue gas heat-exchange unit (7) cold wind road;Another way enters branch flue (9), successively passes through hot precipitator (10), high-temperature blower (11) and smoke regulating valve (12), then converge with the main road flue gas after heating, and the flue gas after converging is through also After former agent injection apparatus (13) sprays into reducing agent, denitration is carried out into SCR reactor (14), the purified flue gas of denitration is through main wind After machine (15) enters the heat exchange cooling of flue gas heat-exchange unit (7) hot wind road, atmosphere is emitted by chimney (16);Wherein, pass through flue gas Regulating valve (12) adjusts branch flue gas flow, and control converges catalyst reaction temperature in the temperature and SCR reactor (14) of rear flue gas Window is spent to be adapted.
8. the method for claim 7, which is characterized in that 200-280 DEG C of the temperature for converging rear flue gas, preferably 200-240℃;
Preferably, temperature of the main road flue gas when converging is 150-200 DEG C, and temperature of the branch flue gas when converging is 300- 380℃。
9. method as claimed in claim 7 or 8, which is characterized in that the reducing agent be ammonium hydroxide, urea or liquefied ammonia at least It is a kind of.
10. a kind of SCR denitration method suitable for cement producing line kiln exit gas, which is characterized in that claim 1-6 is any SCR denitration system and SNCR system described in are combined, the denitration for cement producing line kiln exit gas.
CN201910320326.5A 2019-04-19 2019-04-19 SCR denitration system and method for denitration suitable for cement producing line kiln exit gas Pending CN109876662A (en)

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PCT/CN2019/106075 WO2020211280A1 (en) 2019-04-19 2019-09-17 Scr denitrification system and denitrification method used for cement production line kiln tail gas

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020211280A1 (en) * 2019-04-19 2020-10-22 中国科学院过程工程研究所 Scr denitrification system and denitrification method used for cement production line kiln tail gas
CN111879132A (en) * 2020-08-03 2020-11-03 黄震 Device and method for denitration of cement kiln flue gas
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CN113578045A (en) * 2021-08-18 2021-11-02 中航超能(北京)科技有限公司 Dust removal and denitration treatment process for cement kiln tail flue gas

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