CN205760546U - Cement kiln desulphurization system - Google Patents
Cement kiln desulphurization system Download PDFInfo
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- CN205760546U CN205760546U CN201620437161.1U CN201620437161U CN205760546U CN 205760546 U CN205760546 U CN 205760546U CN 201620437161 U CN201620437161 U CN 201620437161U CN 205760546 U CN205760546 U CN 205760546U
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- dore furnace
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Abstract
This utility model relates to a kind of desulphurization system, the cement kiln desulphurization system of a kind of cement kiln；Ammonia is sprayed onto in preheater, ammonia and the SO of generation in preheater2Reaction generates (NH4)2SO4；The ammonium sulfate generated after boiler of power generation by waste heat, enters bag filter with flue gas；Bag filter dust collects ash silo, and the flue gas after desulfurization enters chimney；By in ash silo rich in (NH4)2SO4Ash be delivered to the middle and upper part of dore furnace；The ammonium sulfate that sweetening process generates is generated stable sulfate in dore furnace, enters rotary kiln, finally discharge rotary kiln with grog.The method small investment, efficiency is high, does not produce secondary pollution, can effectively solve cement plant chimney smoke SO2Content≤1000mg/Nm3Discharge beyond standards problem.
Description
Technical field
This utility model relates to a kind of desulphurization system, and the cement kiln of a kind of cement kiln takes off
Sulfur system.
Background technology
Major tasks suggestion about environmental conservation issued by the State Council, particularly points out for water
Industries SO such as mud, petrochemical industry, Coal Chemical Industry2Improvement with NOX should be stricter.GB4915-2013
" cement industry atmosphere pollutants emission standards " specifies, on July 1st, 2015 rises, existing
Cement kiln and the grinding integrated SO of kiln2The highest permission concentration of emission is 200mg/Nm3,2014 3
The moon plays newly-built cement kiln and the grinding integrated SO of kiln on the 1st2The highest permission concentration of emission is
200mg/Nm3, key area will be according to competent administrative department for environmental protection of State Council or provincial people
People's government decided performs 1000mg/Nm3Tightened up standard.
Many clinkers manufacturing enterprise of China SO2Emission reduction tasks is the severeest, annual SO2Row
Dirty expense is up to millions of unit.Therefore, cement kiln SO2Emission control becomes a urgent task.
For cement kiln SO2Discharge beyond standards, concentration of emission is not more than the situation of 1000mg/Nm3,
In order to reduce investment, occur in that following several minimizing SO2Draining technology: change raw material, humidification
Tower water spray desulfurization technology, cyclone cylinder method desulfurization technology, add slaked lime desulfurizing technology etc..
Replacing raw material refers to: changes the raw materials such as the high limestone of sulfur content, reduces into kiln raw material
Sulfur content, reduces SO from source2Generation discharge, but height universal for sulfur content of raw material
Area, the method has limitation.
Conditioning Tower water-jet technology refers to: cement kiln end flue gas enters the most afterwards from cyclone cylinder preheater
Waste heat boiler, enters back into conditioning Tower from waste heat boiler flue gas out and carries out desulfurization of spraying water, the party
Although method small investment, technique is simple, but removal efficiency is the highest, removal efficiency about 20%.
Cyclone cylinder method desulfurization technology refers to: be extracted into through pipeline from decomposition furnace outlet extraction partial fume
One external cyclone separator, the high activity CaO of collection receives the outlet of two grades of cyclone cylinders
(six grades of preheaters receive third level cyclone cylinder above), active calcium oxide and SO2Haptoreaction,
Absorb SO2The sulfate or the sulphite that are formed return to kiln system, whole mistake with raw material or kiln ash
Process control Ca/S is 10～12.Sweetening process will not produce solid waste, will not be to environment
Produce secondary pollution.But this technology desulfuration efficiency about 30%.Cement kiln SO2Discharge is more than 300
Mg/Nm3, then can not meet cement kiln discharge standard requirement.
Add slaked lime desulfurizing technology to refer to: most going up outer adding calcium hydroxide between two stage cyclone cylinder,
Calcium sulfur ratio is generally 3～5, and desulfuration efficiency is not more than 40%.Add slaked lime and carry out desulfuration efficiency not
Height, can not meet industrially desulfurized requirement.
Utility model content
Technical problem to be solved in the utility model be to provide a kind of easy and simple to handle, run efficiently
Cement kiln desulphurization system.This system and method range is wide, for SO in flue gas2Discharge
The concentration cement kiln desulfurization less than 1000mg/Nm3 has positive effect.
For solving above-mentioned technical problem, this utility model realizes as follows: design one
Kind of cement kiln desulphurization system, its by kiln tail preheater, waste heat boiler, bag filter, chimney,
Dust-precipitator ash silo, kiln tail dore furnace and rotary kiln composition；Kiln tail preheater is constituted with waste heat boiler
Exhaust gases passes connects；Waste heat boiler with by flue gas and desulfurization product (NH4)2SO4The pocket type separated is received
Dirt device constitutes exhaust gases passes and connects；Bag filter constitutes fume emission with chimney and is connected；Pocket type
Dust-precipitator constitutes desulfurization product (NH with dust-precipitator ash silo4)2SO4Gather dust connection；Dust-precipitator ash silo with
Kiln tail dore furnace constitutes sulfate and generates connection；It is defeated that kiln tail dore furnace and rotary kiln constitute sulfate
Enter to connect.
A kind of cement kiln sulfur method of design, its step is as follows:
1) ammonia is sprayed into kiln tail preheater, ammonia and the SO herein generated2Reaction generates
(NH4)2SO4；
2) ammonium sulfate generated enters bag filter with flue gas through waste heat boiler；
3) bag filter dust collects dust-precipitator ash silo, and the flue gas after desulfurization enters cigarette
Chimney；
4) by dust-precipitator ash silo rich in (NH4)2SO4Ash be delivered in kiln tail dore furnace
Top；The ammonium sulfate that sweetening process generates is generated surely in kiln tail dore furnace
Fixed sulfate；
5) sulfate is entered rotary kiln by kiln tail dore furnace, finally discharges rotary kiln with grog
7。
Further, in order to make troilite sulfur in raw material be oxidized to SO in a large number2Discharge,
It is 400～600 DEG C that described ammonia sprays into preheater eject position temperature range.
Further, the mass concentration of described ammonia is 10%～30%, and ammonia generates with preheater
Sulfur dioxide mol ratio be 2.1～2.3.
Further, described chimney smoke SO2Content is with O in flue gas2Content is 10% benchmark meter
Calculation≤1000mg/Nm3。
Good effect of the present utility model: in technical solutions of the utility model, utilizes ammonia to carry out
Cement kiln SO2Removing can effectively solve cement kiln chimney smoke SO2Content is less than
The discharge beyond standards problem of 1000mg/Nm3；And technique is simple, transform at original system,
Cost of investment is low, and desulfurization product is utilized effectively, and will not produce secondary pollution, has good
Economic benefit and environmental benefit.
Accompanying drawing explanation
In order to be illustrated more clearly that this utility model embodiment or technical scheme of the prior art,
The accompanying drawing used required in embodiment or description of the prior art will be briefly described below,
It should be evident that the accompanying drawing in describing below is only embodiments more of the present utility model, right
From the point of view of those of ordinary skill in the art, do not pay creation laborious on the premise of, it is also possible to
Other accompanying drawing is obtained according to these accompanying drawings.
Fig. 1 is the structural representation of embodiment of the present utility model.
In figure, 1, kiln tail preheater；2, waste heat boiler；3, bag filter；4, chimney；
5, dust-precipitator ash silo；6, kiln tail dore furnace；7, rotary kiln.
Detailed description of the invention
In order to make the purpose of this utility model, technical scheme and advantage clearer, below
In conjunction with detailed description of the invention and accompanying drawing, this utility model is described in further details.Here,
Exemplary embodiment of the present utility model and explanation thereof are used for explaining this utility model, but not
As to restriction of the present utility model.
As it is shown in figure 1, a kind of cement kiln desulphurization system of design, it is by kiln tail preheater 1, remaining
Heat boiler 2, bag filter 3, chimney 4, dust-precipitator ash silo 5, kiln tail dore furnace 6 and return
Rotary kiln 7 forms；Kiln tail preheater 1 constitutes exhaust gases passes with waste heat boiler 2 and is connected；Waste heat pot
Stove 2 with by flue gas and desulfurization product (NH4)2SO4The bag filter 3 separated constitutes exhaust gases passes
Connect；Bag filter 3 constitutes fume emission with chimney and is connected；Bag filter 3 with gather dust
Device ash silo 5 constitutes desulfurization product (NH4)2SO4Gather dust connection；Dust-precipitator ash silo 5 is decomposed with kiln tail
Stove 6 constitutes sulfate and generates connection；Kiln tail dore furnace 6 and rotary kiln 7 constitute sulfate input
Connect.
A kind of cement kiln sulfur method of design, its step is as follows:
1) ammonia is sprayed into kiln tail preheater 1, ammonia and the SO herein generated2Reaction generates
(NH4)2SO4；
2) ammonium sulfate generated enters bag filter 3 with flue gas through waste heat boiler 2；
3) bag filter 3 dust collects dust-precipitator ash silo 5, and the flue gas after desulfurization enters
Enter chimney 4；
4) by interior for dust-precipitator ash silo 5 rich in (NH4)2SO4Ash be delivered to kiln tail dore furnace 6
Middle and upper part；Ammonium sulfate sweetening process generated is in kiln tail dore furnace 6
Generate stable sulfate；
5) sulfate is entered rotary kiln 7 by kiln tail dore furnace 6, finally discharges back with grog
Rotary kiln 7.
Further, in order to make troilite sulfur in raw material be oxidized to SO in a large number2Discharge,
It is 400～600 DEG C that described ammonia sprays into preheater eject position temperature range.
Further, the mass concentration of described ammonia is 10%～30%, and ammonia generates with preheater
Sulfur dioxide mol ratio be 2.1～2.3.
Further, described chimney smoke SO2Content is with O in flue gas2Content is 10% benchmark meter
Calculation≤1000mg/Nm3。
Embodiment:
Certain cement production enterprise kiln tail chimney smoke SO2Content is 600～800mg/Nm3, the denseest
Degree is 700mg/Nm3.Being that 20%～30% ammonia sprays into preheater by mass concentration, ammonia is with pre-
The sulfur dioxide mol ratio that hot device generates is 2.1～2.3, ammonia and the SO herein generated2Reaction
Generate (NH4)2SO4；The ammonium sulfate generated enters bag filter with flue gas；Bag filter ash
Dirt collects ash silo, and the flue gas after desulfurization enters chimney；Desulfurization detects kiln after completing at chimney
SO in exit gas2Concentration is 91mg/Nm3, clearance reaches 87%, chimney breast SO2Dense
Degree reaches the up-to-date discharge standard of cement industry.By in ash silo rich in (NH4)2SO4Ash be delivered to point
Solve the middle and upper part of stove；The ammonium sulfate that sweetening process generates is generated stable sulphuric acid in dore furnace
Salt, enters rotary kiln, finally discharges rotary kiln with grog.
Cement kiln discharge uses the SO in ammonia removing flue gas2, there is efficiency high, cost of investment
The advantage such as low, the desulfurization product (NH of generation4)2Sulfur in SO4 is effectively fixed in grog,
Do not cause secondary pollution, be to solve cement kiln SO at present2The effective ways of discharge beyond standards.
Embodiment described above is only to be described preferred implementation of the present utility model,
Not spirit and scope of the present utility model are defined, are designing without departing from this utility model
Under concept thereof, in this area, the technical solution of the utility model is made by ordinary skill technical staff
The various modification gone out and improvement, all should fall into protection domain of the present utility model, this utility model
The technology contents being claimed the most all is recorded in detail in the claims.
Claims (1)
1. a cement kiln desulphurization system, it is characterised in that: its by kiln tail preheater (1),
Waste heat boiler (2), bag filter (3), chimney (4), dust-precipitator ash silo (5),
Kiln tail dore furnace (6) and rotary kiln (7) composition；Kiln tail preheater (1) and waste heat boiler
(2) constitute exhaust gases passes to connect；Waste heat boiler (2) with by flue gas and desulfurization product (NH4)2SO4
The bag filter (3) separated constitutes exhaust gases passes and connects；Bag filter (3) and cigarette
Chimney constitutes fume emission and connects；Bag filter (3) and dust-precipitator ash silo (5) constitute de-
Sulfur product (NH4)2SO4Gather dust connection；Dust-precipitator ash silo (5) and kiln tail dore furnace (6) structure
Become sulfate to generate to connect；It is defeated that kiln tail dore furnace (6) and rotary kiln (7) constitute sulfate
Enter to connect.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620437161.1U CN205760546U (en) | 2016-05-12 | 2016-05-12 | Cement kiln desulphurization system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620437161.1U CN205760546U (en) | 2016-05-12 | 2016-05-12 | Cement kiln desulphurization system |
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| Publication Number | Publication Date |
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| CN205760546U true CN205760546U (en) | 2016-12-07 |
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ID=57410056
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| CN201620437161.1U Active CN205760546U (en) | 2016-05-12 | 2016-05-12 | Cement kiln desulphurization system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107362668A (en) * | 2016-05-12 | 2017-11-21 | 南京凯盛国际工程有限公司 | Cement kiln desulphurization system and sulfur method |
| WO2020164259A1 (en) * | 2019-02-11 | 2020-08-20 | 江苏中圣园科技股份有限公司 | Rotary lime kiln preheater with efficient flue gas desulfurization |
-
2016
- 2016-05-12 CN CN201620437161.1U patent/CN205760546U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107362668A (en) * | 2016-05-12 | 2017-11-21 | 南京凯盛国际工程有限公司 | Cement kiln desulphurization system and sulfur method |
| WO2020164259A1 (en) * | 2019-02-11 | 2020-08-20 | 江苏中圣园科技股份有限公司 | Rotary lime kiln preheater with efficient flue gas desulfurization |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 303 Hanzhongmen street, Gulou District, Nanjing City, Jiangsu Province Patentee after: Zhongcai International Intelligent Technology Co.,Ltd. Address before: 303 Hanzhongmen street, Gulou District, Nanjing City, Jiangsu Province Patentee before: NANJING KISEN INTERNATIONAL ENGINEERING Co.,Ltd. |
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| CP01 | Change in the name or title of a patent holder |