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 PDFInfo
- 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
- Authority
- CN
- China
- Prior art keywords
- flue
- temperature
- flue gas
- denitration
- scr
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000004568 cement Substances 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000003546 flue gas Substances 0.000 claims abstract description 120
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 117
- 239000003054 catalyst Substances 0.000 claims abstract description 42
- 239000007789 gas Substances 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- 239000012716 precipitator Substances 0.000 claims abstract description 17
- 239000003638 chemical reducing agent Substances 0.000 claims description 46
- 238000002347 injection Methods 0.000 claims description 25
- 239000007924 injection Substances 0.000 claims description 25
- 239000000779 smoke Substances 0.000 claims description 23
- 230000001105 regulatory effect Effects 0.000 claims description 15
- 239000000428 dust Substances 0.000 claims description 11
- 239000002918 waste heat Substances 0.000 claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- 239000000908 ammonium hydroxide Substances 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 3
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000004202 carbamide Substances 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 239000004744 fabric Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 231100000572 poisoning Toxicity 0.000 abstract description 8
- 230000000607 poisoning effect Effects 0.000 abstract description 8
- 239000003500 flue dust Substances 0.000 abstract description 4
- 230000003247 decreasing effect Effects 0.000 abstract description 3
- 239000004071 soot Substances 0.000 description 7
- 238000007664 blowing Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 239000002956 ash Substances 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 235000019504 cigarettes Nutrition 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 230000003442 weekly effect Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- 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
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- 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
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
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
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.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910320326.5A CN109876662A (en) | 2019-04-19 | 2019-04-19 | SCR denitration system and method for denitration suitable for cement producing line kiln exit gas |
| 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 |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910320326.5A CN109876662A (en) | 2019-04-19 | 2019-04-19 | SCR denitration system and method for denitration suitable for cement producing line kiln exit gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109876662A true CN109876662A (en) | 2019-06-14 |
Family
ID=66937968
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910320326.5A Pending CN109876662A (en) | 2019-04-19 | 2019-04-19 | SCR denitration system and method for denitration suitable for cement producing line kiln exit gas |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN109876662A (en) |
| WO (1) | WO2020211280A1 (en) |
Cited By (4)
| 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 |
| CN112604498A (en) * | 2020-12-31 | 2021-04-06 | 成都达奇环境科技有限公司 | Cement kiln flue gas waste heat utilization and purification system and low-temperature SCR denitration system |
| 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 |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112973415B (en) * | 2021-02-19 | 2022-04-22 | 清华大学 | Cement kiln device and SNCR denitration method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203316011U (en) * | 2013-07-16 | 2013-12-04 | 中国电力工程顾问集团华北电力设计院工程有限公司 | Structure for improving coal-fired boiler tail smoke denitration input rate |
| CN104772014A (en) * | 2015-04-10 | 2015-07-15 | 无锡华光新动力环保科技股份有限公司 | Combined denitration device for flue gas of cement rotary kiln and denitration technology for flue gas |
| CN105169942A (en) * | 2015-09-23 | 2015-12-23 | 广州创能环保科技有限公司 | Glass melter flue gas dust removal, desulfurization and denitrification synergetic treatment system, treatment method and application |
| CN209848678U (en) * | 2019-04-19 | 2019-12-27 | 中国科学院过程工程研究所 | SCR denitration system suitable for cement manufacture line kiln tail flue gas |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203663706U (en) * | 2013-12-25 | 2014-06-25 | 北京建筑材料科学研究总院有限公司 | Low-temperature selective catalytic reduction denitration system of heating cement kiln |
| CN104174287B (en) * | 2014-08-06 | 2016-09-07 | 北京京诚泽宇能源环保工程技术有限公司 | Partial flue gas denitration system and method for sintering machine |
| CN109876662A (en) * | 2019-04-19 | 2019-06-14 | 中国科学院过程工程研究所 | SCR denitration system and method for denitration suitable for cement producing line kiln exit gas |
-
2019
- 2019-04-19 CN CN201910320326.5A patent/CN109876662A/en active Pending
- 2019-09-17 WO PCT/CN2019/106075 patent/WO2020211280A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203316011U (en) * | 2013-07-16 | 2013-12-04 | 中国电力工程顾问集团华北电力设计院工程有限公司 | Structure for improving coal-fired boiler tail smoke denitration input rate |
| CN104772014A (en) * | 2015-04-10 | 2015-07-15 | 无锡华光新动力环保科技股份有限公司 | Combined denitration device for flue gas of cement rotary kiln and denitration technology for flue gas |
| CN105169942A (en) * | 2015-09-23 | 2015-12-23 | 广州创能环保科技有限公司 | Glass melter flue gas dust removal, desulfurization and denitrification synergetic treatment system, treatment method and application |
| CN209848678U (en) * | 2019-04-19 | 2019-12-27 | 中国科学院过程工程研究所 | SCR denitration system suitable for cement manufacture line kiln tail flue gas |
Cited By (4)
| 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 |
| CN112604498A (en) * | 2020-12-31 | 2021-04-06 | 成都达奇环境科技有限公司 | Cement kiln flue gas waste heat utilization and purification system and low-temperature SCR denitration system |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2020211280A1 (en) | 2020-10-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109876662A (en) | SCR denitration system and method for denitration suitable for cement producing line kiln exit gas | |
| CN204555717U (en) | Warm flue gas SCR denitration device in a kind of cement kiln end | |
| CN207591613U (en) | A kind of regenerated SCR system of low-temperature SCR catalyst | |
| CN104162352B (en) | A kind of glass furnace fume dedusting, denitration, desulfurization integrated handling process | |
| CN101898086A (en) | Power-generation and denitrification integrated device by residual heat of glass furnace and method thereof | |
| CN210814723U (en) | High-temperature dust removal, desulfurization and denitrification device for cement kiln | |
| CN110075681B (en) | Dry desulfurization and denitrification device and method suitable for cement kiln flue gas | |
| CN210699488U (en) | Full-green clean production process equipment for glass kiln | |
| CN108554144A (en) | A kind of SCR denitration system suitable for the high-alkali flue gas of the high dirt of cement kiln tail | |
| CN111495143A (en) | SCR denitration system and method suitable for hazardous waste incinerator | |
| CN208660780U (en) | A kind of SCR denitration system suitable for the high-alkali flue gas of the high dirt of cement kiln tail | |
| CN110180386A (en) | A kind of flue gas spiral diffusion denitrification apparatus and method of denitration | |
| CN112169589A (en) | Ultralow-temperature flue gas SCR denitration system and technology | |
| CN103691315B (en) | A kind of heated type cement kiln low-temperature selective catalytic reduction denitration system | |
| CN103104927A (en) | Smoke denitration method of carbon monoxide (CO) heat recovery boiler of fluid catalytic cracking (FCC) device | |
| CN109731472B (en) | Energy-saving boiler flue gas purification system and method | |
| CN113731113B (en) | System for reducing blockage of ammonium bisulfate of air preheater of coal-fired power plant | |
| CN206253015U (en) | Low temperature is from heat exchange type SCR denitration reaction tower | |
| CN113209823A (en) | Low-temperature SCR denitration device and process for waste gas from nonferrous metal Kaldo furnace smelting | |
| CN111804138A (en) | Biomass boiler flue gas denitration system and application process thereof | |
| CN109351181B (en) | Integrated wide-temperature SCR flue gas denitration method and system | |
| CN209848678U (en) | SCR denitration system suitable for cement manufacture line kiln tail flue gas | |
| CN204543995U (en) | A kind of cement kiln end low-temperature smoke air SCR denitrification apparatus | |
| CN203663706U (en) | Low-temperature selective catalytic reduction denitration system of heating cement kiln | |
| CN217220939U (en) | SCR denitration system of steel mill sintering machine flue gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |