CN205586806U - Cement kiln flue gas desulfurization simultaneously demercuration system - Google Patents
Cement kiln flue gas desulfurization simultaneously demercuration system Download PDFInfo
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- CN205586806U CN205586806U CN201620438655.1U CN201620438655U CN205586806U CN 205586806 U CN205586806 U CN 205586806U CN 201620438655 U CN201620438655 U CN 201620438655U CN 205586806 U CN205586806 U CN 205586806U
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Abstract
The utility model relates to a cement kiln flue gas desulfurization simultaneously demercuration system, soft manganese ore fines and the mixed slurrying of water, thick liquid pass through the pump and replenish the desulfurizing tower lower part, in the absorption tower, the circulating pump with pyrolusite pulp conveying to desulfurizing tower upper portion after spray set sprays, reaction, formation mnSO4 and hgSO4 take place with SO2 in the cement kiln tail flue gas with hg for mnO2 in the pyrolusite thick liquid, flue gas behind the desulfurization demercuration is through defroster defogging back row play desulfurizing tower, the pyrolusite ore pulp that mnSO4 and hgSO4 were rich in in the reaction completion is through thick liquid pump discharge absorption tower. The fine solution of this method the problem that SO2 and hg exceed standard simultaneously in the flue gas, efficient desulfurization simultaneously and demercuration in same device make flue gas discharge to reach standard, have avoided the pollution to the environment of SO2 and hg. This system operation is simple and convenient, and efficient to SO2 and hg desorption, area is little, and the equipment investment is few.
Description
Technical field
This utility model relates to a kind of cement kiln flue gas process field, particularly a kind of cement kiln cigarette
Gas desulfuration demercuration system simultaneously.
Background technology
GB4915-2013 " cement industry atmosphere pollutants emission standards " specifies, 2015 7
The moon rises on the 1st, existing cement kiln and the grinding integrated SO of kiln2The highest permission concentration of emission is
200mg/Nm3, play newly-built cement kiln and the grinding integrated SO of kiln on March 1st, 20142The highest permission
Concentration of emission is 200mg/Nm3, Hg the highest permission concentration of emission is 0.05mg/Nm3, emphasis ground
The SO in district2Discharge will be determined according to competent administrative department for environmental protection of State Council or people's government at the provincial level
Surely 100mg/Nm is performed3Tightened up standard.
Many clinkers manufacturing enterprise of China SO2Emission reduction tasks is the severeest, annual SO2Blowdown
Expense is up to millions of unit.Therefore, cement kiln SO2Emission control becomes a urgent task.
Mercury emissions, essentially from power plant, cement plant, smeltery, incinerator etc., mainly produces
In the burning of mercurous coal, Ore and junk, cement plant mercury emissions needs to pay close attention to.
For cement kiln SO2Discharge beyond standards, concentration of emission is not more than 1000mg/Nm3Situation,
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..But this
It is the highest all to there is desulfuration efficiency in a little methods, it is impossible to meet the problems such as effluent standard.
The domestic case rarely having enforcement at present of cement kiln demercuration, external flue gas demercuration with activated carbon/
Activated coke is adsorbed as main.Control of cement kiln mercury emissions can use following measures: reduces cement kiln row
Cigarette temperature, but cement kiln end flue gas is widely used in cogeneration and dries raw material, kiln tail cigarette at present
Temperature can not be greatly reduced；Activated carbon/activated coke absorption, the method cost is high, absorption
After activated carbon/activated coke be difficult to secondary utilize；Flue gas coordinated desulfurization mercury removal device is in power plant
Use through maturation, but cement kiln is low compared with power plant's sulphur emissions concentration, it is impossible to realize mercury in flue gas has
Can effect removing, utilize also in conceptual phase on cement kiln.
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 flue gas simultaneously desulfuration demercuration system.This system and method is applied widely, for water
Stall flue gas simultaneous desulfurization demercuration has positive effect.
For solving above-mentioned technical problem, this utility model realizes as follows: design one
Planting cement kiln flue gas desulfuration demercuration system simultaneously, including controller, it also includes slurry tank, slurry
Liquid box mixer, slurry feeding pump, absorption tower, demister, spray equipment, absorption tower is stirred
Device, slurry circulating pump and serosity excavationg pump；Continuously stirred slurry tank stirring it is provided with in slurry tank
Device；Slurry tank outlet is connected with slurry feeding pump import, under slurry feeding pump outlet and absorption tower
Portion's import connects；Serum recycle pump intake is received bottom absorption tower, and outlet is connected to spray equipment,
Absorption tower inner upper is located at by spray equipment；It is also equipped with except mist above spray equipment in absorption tower
Device；Absorption tower inner bottom part is additionally provided with continuously stirred absorption tower agitator；Also set bottom absorption tower
There is the serosity excavationg pump discharged for serosity；Middle and lower part, absorption tower is additionally provided with a gas approach.
Further, in order to make pending velocity of flue gas increase, described absorption tower mid diameter becomes
Little.
Design a kind of cement kiln flue gas desulfuration demercuration method simultaneously, step is as follows:
1) by pyrolusite powder and fresh water (FW) slurrying in slurry tank；
2) slurry feeding pump is used to be pumped into the bottom on absorption tower；
3) serosity is transported to the top on absorption tower by slurry circulating pump, sprays through spray equipment
After, carry out chemical reaction, soft manganese with the kiln exit gas entered by gas approach
In ore pulp, MnO2 contacts with SO2 and Hg in the cement kiln end flue gas of rising
Reaction generates MnSO4 and HgSO4；
4) the reacted flue gas demister through top, absorption tower absorbs except discharging after mist
Tower；
5) reacted serosity is discharged bottom absorption tower through serosity excavationg pump.
Further, described pyrolusite powder MnO2Mass fraction is 20%～30%, pyrolusite powder
45 μm tail over≤10%.
Further, the mass concentration of described pyrolusite pulp is 10%～30%, MnO2/SO2Mole
Ratio is 0.5～1.
Further, described kiln tail smoke stack emission flue-gas temperature is 100～200 DEG C；With flue gas
Middle O2Content is 10% benchmark, SO in kiln tail chimney smoke2Content be 1000～
3000mg/Nm3, Hg content≤0.1mg/Nm3。
Good effect of the present utility model: in technical solutions of the utility model, it is provided that a kind of cement
Kiln flue gas simultaneous desulfurization demercuration system, desulfuration demercuration simultaneously, have easy to operate, efficiency is high,
The advantages such as floor space is few, cost of investment is low, are to solve cement kiln SO2 and Hg at present to exceed standard
The effective ways of discharge.
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 radial section structural representation of embodiment of the present utility model.
In figure, 1, slurry tank；2, slurry tank agitator；3, slurry feeding pump；4, absorb
Tower；5, demister；6, spray equipment；7, absorption tower agitator；8, slurry circulating pump；
9, serosity excavationg pump；A, pyrolusite powder；B, fresh water (FW)；C, flue gas；D, clean flue gas；
E, serosity.
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, design a kind of cement kiln flue gas desulfuration demercuration system simultaneously, including controlling
Device, its also include slurry tank 1, slurry tank agitator 2, slurry feeding pump 3, absorption tower 4,
Demister 5, spray equipment 6, absorption tower agitator 7, slurry circulating pump 8 and serosity are discharged
Pump 9；Continuously stirred slurry tank agitator 2 it is provided with in slurry tank 1；Slurry tank 1 outlet with
Slurry feeding pump 3 import connects, and slurry feeding pump 3 outlet is connected with absorption tower 4 lower inlet；
Slurry circulating pump 3 entrance is received bottom absorption tower 4, and outlet is connected to spray equipment 6, spray
Device 6 is located at absorption tower 4 inner upper；It is also equipped with above spray equipment 6 in absorption tower 4
Demister 5；Absorption tower 4 inner bottom part is additionally provided with continuously stirred absorption tower agitator 7；Absorb
The serosity excavationg pump 9 discharged for serosity it is additionally provided with bottom tower 4；Middle and lower part, absorption tower 4 also sets
There is a gas approach.
Further, in order to make pending velocity of flue gas increase, described absorption tower 4 mid diameter
Diminish.
Design a kind of cement kiln flue gas desulfuration demercuration method simultaneously, step is as follows:
1) by pyrolusite powder and fresh water (FW) slurrying in slurry tank 1；
2) slurry feeding pump 3 is used to be pumped into the bottom on absorption tower；
3) serosity is transported to the top on absorption tower 4 by slurry circulating pump 8, through spray equipment
After 6 sprays, carry out chemical reaction with the kiln exit gas entered by gas approach,
MnO in pyrolusite pulp2With the SO in the cement kiln end flue gas risen2Contact with Hg
Reaction generates MnSO4And HgSO4；
4) discharge after the reacted flue gas demister 5 through top, absorption tower 4 is except mist and inhale
Receive tower 4；
5) reacted serosity is discharged bottom absorption tower through serosity excavationg pump.
Further, described pyrolusite powder MnO2Mass fraction is 20%～30%, pyrolusite powder
45 μm tail over≤10%.
Further, the mass concentration of described pyrolusite pulp is 10%～30%, MnO2/SO2Mole
Ratio is 0.5～1.
Further, described kiln tail smoke stack emission flue-gas temperature is 100～200 DEG C；With flue gas
Middle O2Content is 10% benchmark, SO in kiln tail chimney smoke2Content be 1000～
3000mg/Nm3, Hg content≤0.1mg/Nm3。
Operation principle of the present utility model: utilize SO2With the reproducibility of Hg, utilize MnO2Oxygen
The property changed, employing pyrolusite is absorbent, and reaction generates MnSO4And HgSO4.Reaction mechanism is:
SO2+H2O=H2SO3
H2SO3+MnO2=MnSO4+H2O
SO2+H2O+1/2O2=H2SO4
Hg+MnO2+2H2SO4=HgSO4+MnSO4+2H2O
Embodiment: certain cement production enterprise kiln exit gas chimney SO2Content is
1500～2500mg/Nm3, mean concentration is 2000mg/Nm3；Hg content is 0.05～0.1mg/Nm3,
Mean concentration is 0.075mg/Nm3.After pyrolusite powder and fresh water (FW) are sufficiently mixed, quality is dense
Degree is that 10%～30% pyrolusite pulp is transported to bottom, absorption tower, MnO2/SO2Mol ratio is 0.5～1；
Then serosity is transported to the top on absorption tower by slurry circulating pump, after spray equipment is sprayed,
MnO in pyrolusite pulp2With the SO in the cement kiln end flue gas risen2Generate with Hg haptoreaction
MnSO4And HgSO4；The reacted flue gas demister through desulfurizing tower top is inhaled except discharging after mist
Receive tower；Reacted serosity is discharged bottom absorption tower through serosity pump.After desulfuration demercuration completes,
The SO in kiln exit gas is detected at chimney2Concentration is 89mg/Nm3, clearance reaches 95.6%；
Hg concentration is 0.006mg/Nm3, clearance reaches 92%.Chimney breast SO2Dense with Hg discharge
Degree all reaches the up-to-date discharge standard of cement industry.
MnO in described pyrolusite powder2Mass fraction is 20%～30%, pyrolusite powder 45 μm
Tail over≤10%.
Kiln tail chimney smoke temperature is 100～200 DEG C.
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 (2)
1. a cement kiln flue gas desulfuration demercuration system simultaneously, including controller, its feature
Be: its also include slurry tank (1), slurry tank agitator (2), slurry feeding pump (3),
Absorption tower (4), demister (5), spray equipment (6), absorption tower agitator (7),
Slurry circulating pump (8) and serosity excavationg pump (9)；It is provided with continuously stirred in slurry tank (1)
Slurry tank agitator (2)；Slurry tank (1) outlet is with slurry feeding pump (3) import even
Connecing, slurry feeding pump (3) outlet is connected with absorption tower (4) lower inlet；Serum recycle
Pump (3) entrance receives bottom, absorption tower (4), and outlet is connected to spray equipment (6), spray
Shower device (6) is located at absorption tower (4) inner upper；Absorption tower (4) interior spray equipment (6)
Top is also equipped with demister (5)；Absorption tower (4) inner bottom part is additionally provided with continuously stirred
Absorption tower agitator (7)；Bottom, absorption tower (4) is additionally provided with the serosity discharged for serosity
Excavationg pump (9)；Absorption tower (4) middle and lower part is additionally provided with a gas approach.
2. cement kiln flue gas as claimed in claim 1 desulfuration demercuration system simultaneously, it is special
Levy and be: described absorption tower (4) mid diameter diminishes.
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| CN201620438655.1U CN205586806U (en) | 2016-05-12 | 2016-05-12 | Cement kiln flue gas desulfurization simultaneously demercuration system |
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| CN201620438655.1U CN205586806U (en) | 2016-05-12 | 2016-05-12 | Cement kiln flue gas desulfurization simultaneously demercuration system |
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| CN205586806U true CN205586806U (en) | 2016-09-21 |
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Cited By (8)
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| CN106512698A (en) * | 2016-12-21 | 2017-03-22 | 贵州大学 | Flue gas desulfurization and demercuration method for coal-fired power plant |
| CN106512699A (en) * | 2016-12-21 | 2017-03-22 | 贵州大学 | Method for removing sulfur and mercury in flue gas by using ethylenediamine |
| CN106582210A (en) * | 2016-12-22 | 2017-04-26 | 贵州大学 | Method for preparing coal-fired flue gas sulfur and mercury remover from tartaric acid serving as raw material |
| CN106582244A (en) * | 2016-12-21 | 2017-04-26 | 贵州大学 | Method for removing sulfur and mercury in mercury-containing and sulfur-containing smoke with wet process |
| CN106582251A (en) * | 2016-12-21 | 2017-04-26 | 贵州大学 | Method for preparing flue gas desulfurization and mercury removal agent through raw material of lithium manganese titanate |
| CN106731648A (en) * | 2016-12-22 | 2017-05-31 | 贵州大学 | A kind of modification of chitosan prepares sulfur and mercury removing agent and preparation method thereof for raw material |
| CN106731548A (en) * | 2016-12-21 | 2017-05-31 | 贵州大学 | One kind is with La2O2CO3For raw material prepares flue gas desulfurizing and hydrargyrum-removing agent and preparation method thereof |
| CN107362675A (en) * | 2016-05-12 | 2017-11-21 | 南京凯盛国际工程有限公司 | Cement kiln flue gas while desulfuration demercuration system and method |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107362675A (en) * | 2016-05-12 | 2017-11-21 | 南京凯盛国际工程有限公司 | Cement kiln flue gas while desulfuration demercuration system and method |
| CN106731548A (en) * | 2016-12-21 | 2017-05-31 | 贵州大学 | One kind is with La2O2CO3For raw material prepares flue gas desulfurizing and hydrargyrum-removing agent and preparation method thereof |
| CN106582244A (en) * | 2016-12-21 | 2017-04-26 | 贵州大学 | Method for removing sulfur and mercury in mercury-containing and sulfur-containing smoke with wet process |
| CN106582251A (en) * | 2016-12-21 | 2017-04-26 | 贵州大学 | Method for preparing flue gas desulfurization and mercury removal agent through raw material of lithium manganese titanate |
| CN106512698A (en) * | 2016-12-21 | 2017-03-22 | 贵州大学 | Flue gas desulfurization and demercuration method for coal-fired power plant |
| CN106512699A (en) * | 2016-12-21 | 2017-03-22 | 贵州大学 | Method for removing sulfur and mercury in flue gas by using ethylenediamine |
| CN106582251B (en) * | 2016-12-21 | 2019-05-14 | 贵州大学 | A kind of manganese titanate lithium raw material prepares flue gas desulfurizing and hydrargyrum-removing agent method |
| CN106512698B (en) * | 2016-12-21 | 2019-06-04 | 贵州大学 | A kind of coal fired thermal power plant flue gas desulfurizing and hydrargyrum-removing method |
| CN106512699B (en) * | 2016-12-21 | 2019-06-04 | 贵州大学 | A kind of ethylenediamine is used for flue gas desulfurizing and hydrargyrum-removing processing method |
| CN106582244B (en) * | 2016-12-21 | 2019-07-09 | 贵州大学 | A kind of wet process removes mercurous, sulphur and mercury in sulfur-containing smoke gas method |
| CN106582210A (en) * | 2016-12-22 | 2017-04-26 | 贵州大学 | Method for preparing coal-fired flue gas sulfur and mercury remover from tartaric acid serving as raw material |
| CN106731648A (en) * | 2016-12-22 | 2017-05-31 | 贵州大学 | A kind of modification of chitosan prepares sulfur and mercury removing agent and preparation method thereof for raw material |
| CN106582210B (en) * | 2016-12-22 | 2019-08-02 | 贵州大学 | A kind of tartaric acid is that raw material prepares coal-fired flue gas desulfurization demercuration agent method |
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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 |