CN109966812A - A kind of cement kiln end denitrating flue gas and system, the process of waste heat recycling - Google Patents
A kind of cement kiln end denitrating flue gas and system, the process of waste heat recycling Download PDFInfo
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- 239000004568 cement Substances 0.000 title claims abstract description 63
- 239000003546 flue gas Substances 0.000 title claims abstract description 59
- 239000002918 waste heat Substances 0.000 title claims abstract description 58
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 22
- 238000004064 recycling Methods 0.000 title claims description 20
- 230000008569 process Effects 0.000 title abstract description 19
- 239000000428 dust Substances 0.000 claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 239000007789 gas Substances 0.000 claims abstract description 20
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 21
- 230000003750 conditioning effect Effects 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 239000000908 ammonium hydroxide Substances 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 6
- 229910000765 intermetallic Inorganic materials 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 5
- 230000001939 inductive effect Effects 0.000 claims 1
- 239000000463 material Substances 0.000 claims 1
- 239000003344 environmental pollutant Substances 0.000 abstract description 7
- 231100000719 pollutant Toxicity 0.000 abstract description 7
- 238000011160 research Methods 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000004140 cleaning Methods 0.000 abstract description 2
- 239000003054 catalyst Substances 0.000 description 22
- 238000004519 manufacturing process Methods 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- 230000009471 action Effects 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 231100000572 poisoning Toxicity 0.000 description 3
- 230000000607 poisoning effect Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- ZFSFDELZPURLKD-UHFFFAOYSA-N azanium;hydroxide;hydrate Chemical compound N.O.O ZFSFDELZPURLKD-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910052784 alkaline earth metal Inorganic materials 0.000 description 1
- 150000001342 alkaline earth metals Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 238000011020 pilot scale process Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
-
- 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
- B01D53/74—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
- B01D53/8628—Processes characterised by a specific catalyst
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chimneys And Flues (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses system, processes that a kind of cement kiln end denitrating flue gas and waste heat recycle, including preheater, waste heat boiler, high air-heater, high-temperature bag dust remover, SCR denitration reaction device, raw mill, kiln tail deduster, air-introduced machine, heat exchanger and chimney, the exhanst gas outlet of cement rotary kiln kiln tail is connected to by pipeline with the entrance of preheater lower part, and the outlet at the top of preheater is connected to by pipeline with the entrance at the top of waste heat boiler；The outlet of waste heat boiler lower part is connected to by pipeline with high-temperature bag dust remover entrance, and high-temperature bag dust remover outlet is connected to by pipeline with the entrance of SCR denitration reaction device, and the outlet of SCR denitration reaction device bottom is connected to by pipeline with the entrance of raw mill；The outlet of raw mill is connected to by pipeline with the entrance of kiln tail deduster.The present invention provides effective collaborative research of ultralow temperature UTILIZATION OF VESIDUAL HEAT IN and pollutant minimum discharge.Energy low energy consumption, the efficient content for reducing NOx in cement kiln flue gas, the final cleaning discharge for realizing flue gas.
Description
Technical field
The present invention relates to atmosphere pollution Treatment process field, especially a kind of cement kiln end denitrating flue gas and waste heat recycling
System, process.
Background technique
Cement industry NOxTotal emission volumn occupies industrial discharge second, is only second to power industry, real in electric power, steel
In the case where the low transformation of Shih-chao, realize that the minimum discharge of cement industry pollutant is trend of the times.Country is to cement industry pollutant
Discharge standard it is also increasingly stringent.
Low nitrogen burning, fractional combustion and the SNCR technology emission reduction efficiency that cement industry has been applied are difficult to meet increasingly stringent
Therefore standard requirements promote the nitrogen oxides control technology of cement industry imperative.
It is the only way that cement industry realizes minimum discharge using SCR denitration technology, although SCR technology is in coal-fired flue-gas
Use comparative maturity, but there are very big difference in cement production process feature and flue gas operating condition and power plant, can not directly indiscriminately imitate
Power plant's SCR technology, it is therefore desirable to be suitable for the SCR denitration skill of cement kiln flue gas characteristic in conjunction with manufacture of cement and flue gas condition research and development
Art.
SCR denitration technology has application in external manufacture of cement at present, but real case is few, such as Germany in 2000
The cement plant Solnhofen arranges that SCR, denitration efficiency reach 80% using high dirt, the problem is that: first, runing time is short,
It is easy to appear antigravity system blocking；Second, catalyst needs to frequently replace, and system deactivates frequently, has seriously run equipment company
Reforwarding turns；Third, operating cost are uncontrollable.
Summary of the invention
The object of the present invention is to provide system, processes that a kind of cement kiln end denitrating flue gas and waste heat recycle, to solve
Certainly cement kiln flue gas overall process nitrogen oxides minimum discharge control process is complicated at this stage, denitration efficiency is low, energy consumption is big and
Waste heat can not utilize, catalyst easily blocks the technical problems such as duct.
To achieve the above object, the present invention adopts the following technical scheme: the present invention provides a kind of cement kiln end denitrating flue gas
And the system of waste heat recycling, including preheater, waste heat boiler, high air-heater, high-temperature bag dust remover, SCR denitration reaction device, raw material
The exhanst gas outlet of mill, kiln tail deduster, air-introduced machine, heat exchanger and chimney, cement rotary kiln kiln tail passes through under pipeline and preheater
The entrance in portion is connected to, and the outlet at the top of preheater is connected to by pipeline with the entrance at the top of waste heat boiler；
The outlet of waste heat boiler lower part is connected to by pipeline with high-temperature bag dust remover entrance, and high-temperature bag dust remover outlet passes through pipeline
It is connected to the entrance of SCR denitration reaction device, the outlet of SCR denitration reaction device bottom is connected to by pipeline with the entrance of raw mill；
The outlet of raw mill is connected to by pipeline with the entrance of kiln tail deduster, and the outlet of kiln tail deduster passes through pipeline and heat exchange
Device connection, the gas after heat exchanger cools down are discharged by pipeline from chimney.
Further, the amount of nitrogen oxides in SCR denitration reaction device exit is lower than 50mg/Nm3。
Further, the side on the pipeline between waste heat boiler and high-temperature bag dust remover, close to high-temperature bag dust remover entrance
It is provided with high air-heater.
Further, air-introduced machine is provided on the pipeline between kiln tail deduster and heat exchanger.
Further, ammonium hydroxide water supplement port is provided at the top of SCR denitration reaction device.(ammonium hydroxide water supplement port is by having ammonium hydroxide system by oneself
It provides)
It further, further include bypath system；Pipeline connection between bypath system one end and preheater and waste heat boiler, bypass system
The pipeline connection united between the other end and waste heat boiler and high-temperature bag dust remover.(bypath system can be the branch in original system
Road is also possible to branch roads system of meeting an urgent need)
It further, further include conditioning Tower；The entrance of conditioning Tower passes through the pipeline between branch pipe and SCR denitration reaction device and raw mill
The outlet of connection, conditioning Tower passes through the pipeline connection between branch pipe and raw mill and kiln tail deduster.
Further, water inlet and water outlet are provided on heat exchanger；Water outlet is connected to by pipeline with waste heat boiler bottom.
Further, high-temperature bag dust remover is intermetallic compound flexible membrane high temperature high precision deduster；Treated dust
Not higher than 30mg/Nm3。
Further, baffle door is provided at the entrance and exit of high-temperature bag dust remover and kiln tail deduster.
Further, baffle door is provided at the entrance and exit of raw mill.
Further, baffle door is provided at the entrance and exit of SCR denitration reaction device.
Another aspect of the present invention provides the process of the system of above-mentioned cement kiln end denitrating flue gas and waste heat recycling, specifically
Steps are as follows:
Step 1, the exhanst gas outlet through cement rotary kiln kiln tail enter preheater by pipeline；
Step 2 provides suction by high air-heater, and flue gas enters in waste heat boiler from preheater outlet；
Step 3, flue gas reduce dust concentration in high-temperature bag dust remover before entering SCR denitration reaction device；
Step 4 enters raw mill, conditioning Tower by the gas that SCR denitration reaction device is handled；
Step 5 is sent into heat exchanger after secondary filter, carries out heat exchange, and the gas after cooling is discharged by chimney.
Further, in step 5, the temperature of gas is 70-80 DEG C after cooling.
The beneficial effects of the present invention are embodied in:
1, system, the process of a kind of cement kiln end denitrating flue gas and waste heat recycling provided by the invention provide high temperature and remove
The Coupling Research and application mode of dirt device and SCR denitration process system.Ultralow temperature UTILIZATION OF VESIDUAL HEAT IN has been carried out simultaneously and pollutant is super
Effective collaborative research of low emission.NO in energy low energy consumption, efficient reduction cement kiln flue gasxContent, finally realize flue gas
Cleaning discharge.
2, usually working as the alkali metal contents such as calcium oxide in cement kiln end flue gas is more than 80%, much higher than station boiler 5-10%'s
Level, the poisoning of Yi Yinqi catalyst reduce the activity of catalyst.A kind of cement kiln end denitrating flue gas provided by the invention and remaining
System, the process of recuperation of heat, it is careful to have done to the influence high-alkali, that high calcium is to SCR catalyst in cement production process
Research.
3, high-temperature bag dust remover and kiln tail deduster are first set behind the outlet of kiln tail high-temperature blower, the dust in flue gas is dense
Degree reduces, and enters SCR reactor later, the reducing agent of injection is under the action of low temperature catalyst by low temperature, the flue gas item of low dirt
Denitration reaction is completed under part, and amount of nitrogen oxides is finally down to 50mg/Nm3Below.Waste heat is realized by waste-heat recovery device
It utilizes.Complete solid waste, dangerous waste cooperative disposal generate pernicious gas to SCR catalyst influence research.
It overcomes traditional fiber bag filter and is easy to produce " burning bag phenomenon " in high-temperature flue gas environment, for cement
The Gas Parameters of kiln, using " intermetallic compound flexible membrane high temperature high precision deduster ", it can be achieved that dust is not higher than 30mg/
Nm3Minimum discharge.
4, for the research and application of cement furnace high activity low-temperature SCR catalyst.Due to the SO in flue gas2Concentration pole
Low, so having used middle temperature catalyst, catalytic temperature is 200-300 DEG C.High temperature after the reaction temperature and waste heat boiler of catalyst
Fan outlet flue-gas temperature (220-280 DEG C) can be matched preferably, dust concentration 50-80g/Nm3.In use, effective anti-
Only the case where catalyst blockage, no need to increase the volumes of script catalyst, and catalyst life is longer, later period renewal cost
It is low.
The present invention be directed to cement industry typical production process flue gas pollutant discharge characteristics, in conjunction with source process and end
Cement kiln flue gas overall process nitrogen oxides minimum discharge control technology is researched and developed in control, is provided for improvement atmosphere quality important
Technical support.With preferable popularizing action.
Other features and advantages of the present invention will be illustrated in the following description, and partly becomes from specification
It is clear that understand through the implementation of the invention.The main object of the present invention and further advantage can be by the description
Specifically noted scheme is achieved and obtained.
Detailed description of the invention
The present invention will be further described in detail with reference to the accompanying drawing.
Fig. 1 is the system structure diagram of a kind of cement kiln end denitrating flue gas of the present invention and waste heat recycling.
Appended drawing reference: 1- preheater, 2- waste heat boiler, 3- high-temperature blower, 4- high-temperature bag dust remover, 5- SCR denitration reaction
Device, 6- raw mill, 7- kiln tail deduster, 8- air-introduced machine, 9- heat exchanger, 10- chimney, 11- ammonium hydroxide fill into mouth, 12- conditioning Tower,
13- cement rotary kiln, 14- have ammonium hydroxide system, 15- bypath system, 16- baffle door by oneself.
Specific embodiment
Carry out the technical solution that the present invention will be described in detail by the following examples, embodiment below is only exemplary,
It is only capable of for explanation and illustration technical solution of the present invention, and the limitation to technical solution of the present invention cannot be construed to.
As shown in Figure 1, being directed to cement industry typical production process and flue gas pollutant discharge characteristics, subtract in conjunction with source process
Row and end Collaborative Control, the present invention provides the system of a kind of cement kiln end denitrating flue gas and waste heat recycling, to realize nitrogen oxygen
Compound minimum discharge.
Specifically, include preheater 1, waste heat boiler 2, high air-heater 3, high-temperature bag dust remover 4, SCR denitration reaction device 5,
The flue gas of raw mill 6, kiln tail deduster 7, air-introduced machine 8, heat exchanger 9, conditioning Tower 12 and chimney 10,13 kiln tail of cement rotary kiln goes out
Mouthful be connected to the entrance of 1 lower part of preheater by pipeline, cement kiln end heat boiler outlet smoke temperature generally at 220 DEG C -300 DEG C,
Fully meet the reaction temperature of low temperature catalyst.Therefore SCR denitration reaction device 5 is arranged in the exit of waste heat boiler 2.The present invention
Preferably overcome following problem in the prior art: first, since preheater windspout barrel outlet temperature is about 350-400 DEG C,
Dust concentration 80-100g/Nm3It is higher, while being the case where preventing catalyst blockage and selecting using macroporous catalyst.Second,
The volume of the catalyst used further increases, and easily causes catalyst poisoning containing alkali metal such as CaO in flue gas.Third, catalysis
The reduction of agent activity is too fast, the service life is short, and renewal cost is high.
The aperture low temperature catalyst of bigger serface is used in treatment process.Since dust content is high in cement kiln end flue gas
Up to 80~100g/Nm3, and there are a large amount of alkaline-earth metal CaO, there is the risk of blocking catalyst, easily accelerates the abrasion of catalyst
And poisoning.In denitration reactor inlet, intermetallic compound flexible membrane high temperature high precision deduster is set；Treated dust is not
Higher than 30mg/Nm3, effectively the dust concentration in flue gas is reduced, then carries out denitration reaction again.
The outlet at 1 top of preheater is connected to by pipeline with the entrance at 2 top of waste heat boiler.2 lower part of waste heat boiler goes out
Mouth is connected to by pipeline with 4 entrance of high-temperature bag dust remover, on the pipeline between waste heat boiler 2 and high-temperature bag dust remover 4, close to high
The side of warm 4 entrance of bag dust collector is additionally provided with high air-heater 3.The outlet of high-temperature bag dust remover 4 passes through pipeline and SCR denitration reaction
The entrance of device 5 is connected to, and the outlet of 5 bottom of SCR denitration reaction device is connected to by pipeline with the entrance of raw mill 6；SCR denitration reaction
The top of device 5 is provided with ammonium hydroxide and fills into mouth 11.(ammonium hydroxide fills into mouth 11 and is provided by own ammonium hydroxide system 14).
The outlet of raw mill 6 is connected to by pipeline with the entrance of kiln tail deduster 7, and the outlet of kiln tail deduster 7 passes through pipe
Road is connected to heat exchanger 9.
Existing chimney emission temperature is about -120 DEG C, SO in flue gas2、SO3Isoconcentration is extremely low, and there is no asking for dew point corrosion
Topic, therefore increase heat exchanger 9 and carry out waste heat recycling.It is provided with water inlet and water outlet on heat exchanger 9, heat exchanger 9 is by flue gas
Temperature is reduced to 70-80 DEG C；Water outlet is connected to by pipeline with 2 bottom of waste heat boiler, and it is remaining for improving to recycle this partial heat
The feed temperature of heat boiler 2, while by improving total power generation, realizing ultralow temperature to 2 heating surface local flow improvement of waste heat boiler
UTILIZATION OF VESIDUAL HEAT IN also can provide hot water, be used as other heating or other systems.Finally, the gas after the cooling of heat exchanger 9 passes through pipe
Road is discharged from chimney 10.
Air-introduced machine 8 is arranged on the pipeline between kiln tail deduster 7 and heat exchanger 9.The entrance of conditioning Tower 12 passes through branch pipe
The outlet of pipeline connection between SCR denitration reaction device 5 and raw mill 6, conditioning Tower 12 passes through branch pipe and raw mill 6 and kiln tail
Pipeline connection between deduster 7.
High-temperature bag dust remover 4, kiln tail deduster 7, raw mill 6 and SCR denitration reaction device 5 entrance and exit at be all provided with
It is equipped with baffle door 16.
Above system further includes bypath system 15；Pipeline between 15 one end of bypath system and preheater 1 and waste heat boiler 2 connects
It is logical, the pipeline connection between 15 other end of bypath system and waste heat boiler 2 and deduster.
The process of above-mentioned cement kiln end denitrating flue gas and the system of waste heat recycling, the specific steps are as follows:
Step 1, the exhanst gas outlet through 13 kiln tail of cement rotary kiln enter preheater 1 by pipeline；
Step 2 provides suction by high air-heater 3, and flue gas enters in waste heat boiler 2 from the outlet of preheater 1；
Step 3, flue gas reduce dust concentration in high-temperature bag dust remover 4 before entering SCR denitration reaction device 5；
Step 4 enters raw mill 6, conditioning Tower 12 by the gas that SCR denitration reaction device 5 is handled；
Step 5 is sent into heat exchanger 9 after secondary filter, carries out heat exchange, and the gas after cooling passes through 10 row of chimney
Out.The temperature of gas is 70-80 DEG C after cooling.
System, the process recycled using cement kiln end denitrating flue gas provided by the invention and waste heat is carried out:
First, experimental study:
In conjunction with cement production process and flue gas condition, Beijing company #1 cement dangerous waste cooperative disposal production line is relied on
(2000t/d) builds treatment quantity 10000Nm3The cement low temperature SCR denitration experimental rig of/h, subtracts flue gas NOx of cement kiln
Capable test is discharged into, research SCR denitration technology provides data branch in the feasibility of cement industry for designing and implementing for demonstration project
Support.
Second, engineering mimoir:
Rely on pilot-scale experiment, to Beijing company #1 cement dangerous waste cooperative disposal production line (2000t/d) install additional SCR denitration and
Dust-extraction unit realizes minimum discharge (NOx < 50mg/Nm of cement kiln flue gas pollutant3, dust < 30mg/Nm3).
In conclusion the system, the process that are recycled using cement kiln end denitrating flue gas provided by the invention and waste heat, it can
With realize under the action of low temperature catalyst by low temperature, low dirt flue gas condition under complete denitration reaction, finally by nitrogen oxides
Content is down to 50mg/Nm3Below.And it overcomes traditional fiber bag filter to be easy to produce in high-temperature flue gas environment
" burning bag phenomenon " is realized for the Gas Parameters of cement kiln using " intermetallic compound flexible membrane high temperature high precision deduster "
Dust is not higher than 30mg/Nm3Minimum discharge.
The foregoing is merely the preferable specific embodiments of the present invention, but scope of protection of the present invention is not limited thereto,
The change or replacement that anyone skilled in the art is expected in the technical scope disclosed by the present invention should all be contained
Lid is within protection scope of the present invention.
Claims (10)
1. a kind of cement kiln end denitrating flue gas and the system of waste heat recycling, it is characterised in that: including preheater (1), waste heat boiler
(2), high air-heater (3), high-temperature bag dust remover (4), SCR denitration reaction device (5), raw mill (6), kiln tail deduster (7), air inducing
The exhanst gas outlet of machine (8), heat exchanger (9) and chimney (10), cement rotary kiln (13) kiln tail passes through pipeline and preheater (1) lower part
Entrance connection, the outlet at the top of preheater (1) is connected to by pipeline with the entrance at the top of waste heat boiler (2)；
The outlet of waste heat boiler (2) lower part is connected to by pipeline with high-temperature bag dust remover (4) entrance, and high-temperature bag dust remover (4) goes out
Mouth is connected to by pipeline with the entrance of SCR denitration reaction device (5), and the outlet of SCR denitration reaction device (5) bottom passes through pipeline and life
The entrance connection of material mill (6)；
The outlet of raw mill (6) is connected to by pipeline with the entrance of kiln tail deduster (7), and the outlet of kiln tail deduster (7) passes through
Pipeline is connected to heat exchanger (9), and the gas after heat exchanger (9) cooling is discharged by pipeline from chimney (10).
2. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that SCR denitration is anti-
Answer the amount of nitrogen oxides in device (5) exit lower than 50mg/Nm3。
3. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that waste heat boiler
(2) high air-heater is provided on the pipeline between high-temperature bag dust remover (4), close to the side of high-temperature bag dust remover (4) entrance
(3).
4. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that kiln tail deduster
(7) air-introduced machine (8) are provided on the pipeline between heat exchanger (9).
5. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that SCR denitration is anti-
It answers and is provided with ammonium hydroxide at the top of device (5) and fills into mouth (11).
6. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that further include bypass
System (15)；Pipeline connection between bypath system (15) one end and preheater (1) and waste heat boiler (2), bypath system (15)
Pipeline connection between the other end and waste heat boiler (2) and high-temperature bag dust remover (4).
7. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that further include humidification
Tower (12)；The entrance of conditioning Tower (12) is increased by the pipeline connection between branch pipe and SCR denitration reaction device (5) and raw mill (6)
The outlet of wet tower (12) passes through the pipeline connection between branch pipe and raw mill (6) and kiln tail deduster (7).
8. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that heat exchanger (9)
On be provided with water inlet and water outlet；Water outlet is connected to by pipeline with waste heat boiler (2) bottom.
9. cement kiln end denitrating flue gas as described in claim 1 and the system of waste heat recycling, which is characterized in that temperature bag dedusting
Device (4) is intermetallic compound flexible membrane high temperature high precision deduster；Treated, and dust is not higher than 30mg/Nm3。
10. the technique side of the system of cement kiln end denitrating flue gas and waste heat recycling as described in any one of claim 1-9
Method, which is characterized in that specific step is as follows:
Step 1, the exhanst gas outlet through cement rotary kiln (13) kiln tail enter preheater (1) by pipeline；
Step 2 provides suction by high air-heater (3), and flue gas enters in waste heat boiler (2) from preheater (1) outlet；
Step 3, flue gas reduce dust concentration before entering SCR denitration reaction device (5) in high-temperature bag dust remover (4)；
Step 4 enters raw mill (6), conditioning Tower (12) by the gas that SCR denitration reaction device (5) are handled；
Step 5 is sent into heat exchanger (9) after secondary filter, carries out heat exchange, and the gas after cooling passes through chimney
(10) it is discharged.
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| CN110314543A (en) * | 2019-08-02 | 2019-10-11 | 陕西大秦环境科技有限公司 | Dirt arrangement SCR denitration device and technique in a kind of cement kiln |
| CN110893379A (en) * | 2019-12-27 | 2020-03-20 | 浙江德创环保科技股份有限公司 | Cement kiln tail high temperature dust removal deNOx systems |
| CN111879132A (en) * | 2020-08-03 | 2020-11-03 | 黄震 | Device and method for denitration of cement kiln flue gas |
| CN111895377A (en) * | 2020-08-03 | 2020-11-06 | 黄震 | Efficient-circulation device and method for cement kiln denitration |
| CN112138477A (en) * | 2020-08-18 | 2020-12-29 | 华电电力科学研究院有限公司 | Filter bag service life optimization management method for bag type dust collector |
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| CN115307154A (en) * | 2022-06-29 | 2022-11-08 | 成都易态科技有限公司 | Method and device for purifying waste incineration flue gas |
| CN115301014A (en) * | 2022-06-30 | 2022-11-08 | 成都易态科技有限公司 | Cement raw meal grinds high temperature flue gas purification device and cement production system |
| CN115671910A (en) * | 2022-06-30 | 2023-02-03 | 成都易态科技有限公司 | High-temperature flue gas purification device of cement burning clinker cooling machine and cement production system |
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Application publication date: 20190705 |