CN208927928U - Cement industry self-loopa dry method desulfuration system - Google Patents
Cement industry self-loopa dry method desulfuration system Download PDFInfo
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- CN208927928U CN208927928U CN201820751981.7U CN201820751981U CN208927928U CN 208927928 U CN208927928 U CN 208927928U CN 201820751981 U CN201820751981 U CN 201820751981U CN 208927928 U CN208927928 U CN 208927928U
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 110
- 238000000034 method Methods 0.000 title claims abstract description 61
- 239000004568 cement Substances 0.000 title claims abstract description 53
- 230000023556 desulfurization Effects 0.000 claims abstract description 74
- 239000002994 raw material Substances 0.000 claims abstract description 52
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 49
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 47
- 238000002360 preparation method Methods 0.000 claims abstract description 40
- 239000007789 gas Substances 0.000 claims abstract description 33
- 238000006243 chemical reaction Methods 0.000 claims abstract description 12
- 239000012716 precipitator Substances 0.000 claims description 47
- 239000003546 flue gas Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 13
- 230000033228 biological regulation Effects 0.000 claims description 12
- 238000000227 grinding Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000012546 transfer Methods 0.000 claims description 10
- 239000000428 dust Substances 0.000 claims description 9
- 238000004140 cleaning Methods 0.000 claims description 7
- 239000011214 refractory ceramic Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 235000019504 cigarettes Nutrition 0.000 claims description 2
- 230000029087 digestion Effects 0.000 claims description 2
- 238000012545 processing Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 27
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 15
- 230000008569 process Effects 0.000 abstract description 13
- 239000011593 sulfur Substances 0.000 abstract description 11
- 229910052717 sulfur Inorganic materials 0.000 abstract description 11
- 238000012946 outsourcing Methods 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 abstract description 9
- 238000010276 construction Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 5
- 230000004927 fusion Effects 0.000 abstract description 4
- 238000000605 extraction Methods 0.000 abstract description 3
- 239000003517 fume Substances 0.000 abstract description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 9
- 239000000284 extract Substances 0.000 description 7
- 239000005864 Sulphur Substances 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 5
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 5
- 239000000292 calcium oxide Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 5
- 230000006641 stabilisation Effects 0.000 description 5
- 238000011105 stabilization Methods 0.000 description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 4
- 235000011941 Tilia x europaea Nutrition 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000004571 lime Substances 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- 239000011575 calcium Substances 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- JGIATAMCQXIDNZ-UHFFFAOYSA-N calcium sulfide Chemical compound [Ca]=S JGIATAMCQXIDNZ-UHFFFAOYSA-N 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 235000012054 meals Nutrition 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 150000002898 organic sulfur compounds Chemical class 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 210000000664 rectum Anatomy 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 230000033764 rhythmic process Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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- Treating Waste Gases (AREA)
- Furnace Details (AREA)
Abstract
The utility model proposes a kind of self-loopa dry method desulfuration system, which includes: feeding unit, and feeding unit is connected with the blanking pipe of the one cyclonic cylinder in kiln tail preheater, to obtain hot raw material；Preparation unit, preparation unit are connected with feeding unit, to prepare desulfurizing agent using hot raw material；And desulfurization unit, desulfurization unit are connected with preparation unit and kiln tail preheater respectively, to obtain desulfurizing agent and sulfurous gas respectively and complete desulphurization reaction.Self-loopa dry method desulfuration system disclosed by the utility model gets up the fusion of the main technical process height of sulfur removal technology and manufacture of cement, desulfurizing agent is prepared from the fume extraction raw material of manufacture of cement kiln tail, without outsourcing desulfurizing agent, and flexible operation, construction period are short, and do not influence the normal production of production line, compared under low operating cost stablize, flexibly realize SO2Concentration of emission requirement, and there is preferable economic benefit.
Description
Technical field
The utility model relates to gas sweetening fields, more particularly, to a kind of cement industry self-loopa dry desulfurization system
System.
Background technique
Ending for the end of the year 2016, there are about more than 1770 items (removal part removed for 2016) New Type Dry-process Cement Productions in the whole nation
Line, cement plant high-temperature calcination all divide organic sulfur compound, simple sulfide or the sulfate in cement producting material and fuel
Solution comes out, with oxysulfide (SO2) form be discharged into atmosphere, seriously affected the health of the mankind.In recent years, with country
Attention to environmental protection, SO2Discharge amount gradually decreases, but total amount is still very big.According to GB4915-2013, " cement industry atmosphere is dirty
Contaminate object discharge standard " regulation, cement kiln and kiln mill all-in-one machine exhaust tube in SO2Concentration of emission control is being less than 200mg/m3, weight
The control of point area is being less than 100mg/Nm3, therefore how SO in cost-effective reinforcement flue gas2Removing be enterprise pollution administer
Vital task.Although flue gas desulfurization technique reaches hundreds of, the current most common flue gas desulfurization technique of cement kiln mainly has
Wet Flue Gas Desulfurization Technique, desulfurization by dry method and compound desulfurization technology.Wherein wet desulphurization be most widely used and efficiency compared with
High sulfur removal technology.But wet desulphurization still has a series of problem, such as system complex, takes up a large area, equipment corrosion
Seriously, a large amount of waste liquids are generated to be difficult to handle.The existing land occupation of dry desulfurizing process is less, construction cost is low, free of contamination feature, again
Higher desulfurization degree can be obtained in the case where calcium sulfur ratio is moderate, but its operating cost is high, second decomposition can occur for desulfurization product.
And the drawbacks of obtaining the universally recognized compound desulfurization technology in cement industry field at present, overcoming the first two kind method, it realizes low
Cost, high efficiency, desulfurization rapidly.However, wet desulphurization, dry desulfurization or compound doctor treatment, are both needed to outsourcing desulfurizing agent, increase
The different workshops for adding desulphurization system to need, and corresponding personnel are equipped with, the increase of investment with production and operation cost is caused, after desulfurization
Material can not cycling and reutilization, there are still the discharges of waste material.
With the continuous development of technology, newest new dry process rotary kiln kiln exit gas desulphurization system has started to taste in recent years
The method for using not outsourcing desulfurizing agent, the method are air outlet one rotoclone collectors of increase in dore furnace, utilize kiln tail
The negative pressure of system high temperature blower extracts the dusty gas containing CaO, will be under the material collection containing CaO by rotoclone collector
As the raw material of desulfurizing agent.This method, which overcomes conventional wet desulfurization, dry desulfurization and compound desulfurization, needs outsourcing desulfurizing agent
Defect, but extract~850 DEG C of hot wind in the air outlet of dore furnace and directly affect the thermally equilibrated stabilization of kiln tail process system,
And the heat loss of system is increased, and be the air quantity for being unable to control extraction by kiln tail system high-temperature blower, it also just can not basis
The SO of flue gas2Content and local SO2Emission request, the inventory of desulfurizing agent raw material is extracted in control, therefore its is inefficient and unstable
Fixed, desulfurization effect is only 50% or so.In order not to the excessive original production of influence, the hot blast rate extracted will meet emphasis
Regional SO2Concentration of emission control is being less than 100mg/Nm3It is unapproachable, and also adds kiln tail system high-temperature blower
Load and its power consumption.
Utility model content
In order to solve the above technical problems, the utility model proposes a kind of cement industry self-loopa dry method desulfuration system, it should
Self-loopa dry method desulfuration system includes:
Feeding unit, feeding unit are connected raw to obtain heat with the blanking pipe of the one cyclonic cylinder in kiln tail preheater
Material；
Preparation unit, preparation unit are connected with feeding unit, to prepare desulfurizing agent using hot raw material；
Desulfurization unit, desulfurization unit are connected with preparation unit and kiln tail preheater respectively, with obtain respectively desulfurizing agent and
Sulfurous gas simultaneously completes desulphurization reaction；With
Matter Transfer unit, Matter Transfer unit are connected with desulfurization unit and cement preparation system respectively, so that flue gas is de-
Product after sulphur is used for cement grinding system.
In one embodiment, the one cyclonic cylinder is the afterbody cyclone cylinder in kiln tail preheater.
In one embodiment, feeding unit includes:
One end of feeding pipeline, feeding pipeline is connected with blanking pipe, to obtain hot raw material from blanking pipe, and takes
Trapped line pressure valve is provided on pipe material；
First conveying device, the first conveying device are connected with the other end of feeding pipeline；
First dust-precipitator, the blast pipe of the first dust-precipitator are connected to obtain raw material, and first with the first conveying device
Dust-precipitator has the first dust-precipitator blower；With
Second conveying device, one end of the second conveying device is connected with the first dust-precipitator, the other end and preparation unit phase
Connection,
Preferably, the first conveying device is speed regulation high-temperature spiral conveyer,
Preferably, the first dust-precipitator is refractory ceramics filter bag dust-precipitator, it is preferable that the second conveying device is that metering screw is defeated
Machine is sent, and the inlet of the second conveying device is provided with speed regulation revolution air valve.
In one embodiment, kiln tail preheater is Pyatyi preheater, and the one cyclonic cylinder is level V cyclone cylinder.
In one embodiment, feeding unit further includes air bubble, air bubble be arranged on feeding pipeline and relative to
Trapped line pressure valve is closer to blanking pipe.
In one embodiment, feeding unit further includes air cleaning unit, and air cleaning unit is for connecting first
On the tracheae of conveying device and the first dust-precipitator.
In one embodiment, trapped line pressure valve is gate valve.
In one embodiment, preparation unit includes:
Digester, digester are connected with feeding unit, to obtain raw material and prepare desulfurizing agent；With
Third conveying device, one end of third conveying device is connected with digester, the other end is connected with desulfurization unit,
Desulfurizing agent is delivered to desulfurization unit,
Preferably, third conveying device is helicoidal pump,
Preferably, preparation unit further includes measuring chute, the arrival end of measuring chute is connected with feeding unit, outlet end with disappear
Change device to be connected, and measuring chute includes load sensor and the outlet that measuring chute is arranged in being connected with load sensor
Air valve is turned round in the speed regulation at end, and measuring chute is used to control the weight into the raw material of digester,
Preferably, preparation unit further includes the 4th conveying device, and one end of the 4th conveying device is connected, separately with digester
One end is connected with the feed pipe of kiln tail preheater, it is highly preferred that the expects pipe for connecting the 4th conveying device and digester
It is provided with triple valve, the arrival end of triple valve is connected to digester, two outlet ends are connected respectively to third conveying device and
Four conveying devices,
Preferably, preparation unit further includes water injector, and water injector is connected to spray water into digester with digester.
In one embodiment, desulfurization unit includes:
Desulfurization reactor, desulfurization reactor are connected to obtain desulfurizing agent with preparation unit；With
First rotoclone collector group, the first rotoclone collector group include multiple rotoclone collectors, in multiple rotoclone collectors
The first order cyclone cylinder that is connected in kiln tail preheater of the air intake of each in corresponding one, outlet air end is all connected to
Sulfurous gas in kiln tail preheater is sent into desulfurization reactor, each of multiple rotoclone collectors by desulfurization reactor
Discharge end be connected with the feed pipe of kiln tail preheater,
Preferably, the first rotoclone collector group includes four rotoclone collectors.
In one embodiment, Matter Transfer unit includes:
The air intake of second rotoclone collector group, the second rotoclone collector group is connected with desulfurization unit, to receive from de-
The flue gas of sulphur unit discharge；With
Machine for zipper, one end of machine for zipper is connected with the discharge end of the second rotoclone collector group, the other end and exhaust-gas treatment
System or cement grinding system are connected,
Preferably, the second rotoclone collector group includes two rotoclone collectors, each of two rotoclone collectors
Air intake is connected to desulfurization unit, outlet air end is connected to raw material grinding system, discharge end is connected to machine for zipper.
Cement industry self-loopa dry method desulfuration system disclosed by the utility model is by the main work of sulfur removal technology and manufacture of cement
The fusion of skill process height is got up, and prepares desulfurizing agent from the fume extraction raw material of manufacture of cement kiln tail, is not necessarily to outsourcing desulfurizing agent, is not necessarily to
Increase workshop and producers, and flexible operation, construction period are short, and do not influence the normal production of production line,
Compared under low operating cost stablize, flexibly realize SO2Concentration of emission control is being less than 200mg/Nm3Or it is less than 100mg/Nm3Want
It asks；And the reaction by-product after gas cleaning can be directly used for cement production system, thus have preferable economic benefit.
Detailed description of the invention
Fig. 1 is the schematic diagram according to the self-loopa dry method desulfuration system of an exemplary embodiment of the utility model.
Specific embodiment
Illustrative, non-limiting embodiment of the utility model are described in detail with reference to the accompanying drawings, to practical new according to this
The self-loopa dry method desulfuration system and method for type are described further.
Referring to Fig.1, the one aspect of the utility model proposes a kind of cement industry self-loopa dry method desulfuration system, this is
System includes feeding unit, preparation unit, desulfurization unit and Matter Transfer unit.
Feeding unit is connected with the blanking pipe 21 of the one cyclonic cylinder in kiln tail preheater 2, to obtain containing oxidation
The hot raw material of calcium (CaO).The one cyclonic in kiln tail preheater 2 is arranged in the feeding point of feeding unit by the utility model
The blanking pipe 21 of cylinder, therefore kiln tail system high-temperature blower will not be had an impact, the necessary heat damage of system will not be increased
It loses.In one embodiment, the one cyclonic cylinder is the afterbody cyclone cylinder of kiln tail preheater 2.The afterbody whirlwind
The content of calcium oxide is higher (60% or more) in hot raw material in the blanking pipe 21 of cylinder, therefore under afterbody cyclone cylinder
The available highest desulfurizing agent preparation efficiency of hot raw material is extracted in pipe material 21.Preparation unit is connected with feeding unit, with
Hot raw material are obtained from feeding unit and prepare desulfurizing agent using hot raw material, that is, in preparation unit, calcium oxide and water hybrid reaction
Generate white lime (Ca (OH)2), white lime can be used for completing desulphurization reaction in desulfurization unit.Desulfurization unit and preparation unit
Be connected to obtain desulfurizing agent, while desulfurization unit is connected with kiln tail preheater 2 and obtains kiln tail sulfur-containing smoke gas, desulfurizing agent with contain
The biochemical reaction of sulphur flue gas hybrid concurrency in desulfurization unit generates calcium sulfate (CaSO4), to complete to take off sulfurous gas
Sulphur.
By above description it is recognised that the utility model proposes cement industry self-loopa dry method desulfuration system can be with water
The main technical process height fusion of mud production, is extracted hot raw material from cement factory kiln tail preheater 2 and is made using hot raw material de-
Sulphur agent, therefore outsourcing desulfurizing agent is not necessarily in sulfur removal technology, the effect for reducing production cost may be implemented；In addition, pre- from kiln tail
The blanking pipe 21 of one cyclonic cylinder in hot device 2 extracts raw material, can directly extract flue gas to avoid from the air outlet of dore furnace 1
And the thermally equilibrated stability of kiln tail process system is influenced, and then the problem of the heat loss of increase system；Reaction after flue gas desulfurization
Byproduct can be directly used for cement production system, have preferable economic benefit.Therefore, cement industry disclosed by the utility model
Self-loopa dry method desulfuration system is truly realized in the case where not affecting the normal production, and is not necessarily to outsourcing desulfurizing agent, without increasing
Workshop and producers, and flexible operation, construction period are short, do not influence the normal production of production line, guarantee in lower fortune
It is realized under the premise of row cost and stablizes, flexibly controls SO2Concentration of emission purpose.
In one embodiment, feeding unit includes sequentially connected feeding pipeline 31, the first conveying device 33, first receipts
Dirt device 34, the first dust-precipitator blower 35 and the second conveying device 36.
Feeding pipeline 31 is connect with the blanking pipe 21 of the afterbody cyclone cylinder in kiln tail preheater 2, the first conveying dress
Set 33 and obtain hot raw material from kiln tail by the way of mechanical, with generated in the first dust-precipitator blower 35 negative pressure under the action of will be hot
Raw material suck the first dust-precipitator 34.Meanwhile trapped line pressure valve 32 is provided on feeding pipeline 31, with control take hot raw material process and
Speed.Since the temperature of kiln tail feeder pipe is higher (850 DEG C or more), feeding pipeline 31 is made of heat-resisting material.?
In one embodiment, trapped line pressure valve 32 is gate valve.Gate valve is the valve that a kind of flashboard and valve seat are in close contact sealing always, valve
Body latus rectum un-grooved, therefore medium will not card resistance blocking；Due to gate valve have full-bore flow characteristics, so can quickly,
Pass through hot raw material without blocking；Meanwhile because gate valve 32 have good leakproofness, it is possible to avoid raw material leak and
Cause environmental pollution.In one embodiment, kiln tail preheater 2 is Pyatyi preheater, and afterbody cyclone cylinder is level V rotation
Air duct.
First conveying device 33 is connected with the other end of feeding pipeline 31, is used for raw material conveyor to the first dust-precipitator 34
Blast pipe.Since the raw material temperature extracted from blanking pipe 21 is higher (850 DEG C or more), the one of the utility model
In a embodiment, the first conveying device 33 is speed regulation high-temperature spiral conveyer.Its existing normal spiral conveyer utilizes motor band
Dynamic spiral revolution, passage material have the function of current stabilization, speed regulation to realize the function of conveying, the simple, cross section with structure
Product is small, good airproof performance, easy to operate, maintenance is easy, is convenient for the advantages that enclosed conveying.
The blast pipe of first dust-precipitator 34 is connected with the first conveying device 33, is conveyed with receiving by the first conveying device 33
Hot raw material.First dust-precipitator 34 has the first dust-precipitator blower 35, and in the course of work, the first dust-precipitator blower 35 can be in life
Certain negative pressure is generated in material conveying tube road, under the action of negative pressure, the feeder pipe of the afterbody cyclone cylinder in kiln tail preheater 2
Hot raw material in road 21 are entered by the first conveying device 33 in the blast pipe of first dust-precipitator 34.On the other hand, it is received by first
Dirt device blower 35 makes the gas of the first dust-precipitator 34 sucking environment temperature, is dropped by the mixing of the gas and hot raw material of environment temperature
The temperature of low raw material, for example, being cooled to about 250 DEG C.In this way, meeting the needs for preparing desulfurizing agent, and to the first dust-precipitator
34 follow-up equipment plays a protective role.Since the raw material temperature extracted from the blanking pipe 21 of preheater is higher, at this
In one embodiment of utility model, the filtrate of the first dust-precipitator 34 uses refractory ceramics filtrate, to reduce caused by high temperature
Equipment loss guarantees the normal work of feeding unit.
One end of second conveying device 36 is connected with the first dust-precipitator 34, the other end is connected with preparation unit, will
Raw material conveyor to preparation unit after cooling down in the first dust-precipitator 34 carries out desulfurizing agent preparation section.In the second conveying device 36
Feeding inlet be also equipped with speed regulation revolution air valve (not shown), for lock wind guarantee the second conveying device 36 metering conveying
Stabilization.Second conveying device 36 is the high-temperature spiral conveyer with function of measuring, is also possible to have metering conveying material
Other conveying devices of function.In one embodiment, feeding unit further includes air cleaning unit 37.Air cleaning unit 37
Tracheae for connecting the first conveying device 33 and the first dust-precipitator 34 is set, it is negative in the first dust-precipitator blower 35 to ensure
Pressure, the air into the environment temperature of system are free from foreign meter.
In one embodiment, feeding unit further includes air bubble 38.Air bubble 38 is arranged on feeding pipeline 31, it can
To spray compressed gas with the speed more than one Mach, compressed gas pours tracheae, overcomes material static friction, makes to block
Tracheae circulates again.
The reclaiming process of feeding unit disclosed by the utility model is as follows: starting the first dust-precipitator blower 35 and first gathers dust
Device 34 opens gate valve 32, to generate negative pressure in the air inlet pipeline of the first dust-precipitator 34 of feeding unit；In suction function
Under, start the first conveying device 33, by the way of mechanical, the hot raw material in blanking pipe 21 enter feeding pipeline 31 and pass through
First conveying device 33 enters the blast pipe of the first dust-precipitator 34；It is sucked in first dust-precipitator 34 by the first dust-precipitator blower 35
Environmental gas, environmental gas mix to drop in 34 blast pipe of the first dust-precipitator and in the first dust-precipitator 34 with the hot raw material of powdery
The temperature (for example, being reduced to 250 DEG C or so) of low-heat raw material；After the cooling of the first dust-precipitator 34, raw material pass through the second conveying
Device 36 enters preparation unit.As shown in the above description, feeding unit disclosed by the utility model from kiln tail preheater 2 most
21 feeding of blanking pipe of rear stage cyclone cylinder extracts oxidation preferably from 21 feeding of blanking pipe of afterbody cyclone cylinder
The highest raw material of calcium content, and will not influence the thermally equilibrated stability of kiln tail process system, and then increase the heat loss of system
The problem of；The temperature that raw material are reduced by the first dust-precipitator blower 35 and the first dust-precipitator 34 and its blast pipe, can be to subsequent
Processing equipment play the role of protection, while using ceramic filter material in the inside of the first dust-precipitator 34, make the first dust-precipitator 34
It has the performance of high temperature resistance, to prolong the service life.
With continued reference to Fig. 1, in one embodiment of the utility model, preparation unit includes digester 42 and third conveying
Device 43.
Digester 42 is connected with the second conveying device 36 in feeding unit, to obtain raw material from feeding unit.Disappear
Changing device 42 has mixing, digestion, conveying, dust-collecting function, the raw material obtained from feeding unit can be uniformly mixed with water
Desulfurizing agent.In this way, desulfurizing agent is prepared using digester 42 by extracting hot raw material from the blanking pipe 21 of kiln tail preheater,
It is not necessarily to outsourcing desulfurizing agent in sulfur removal technology, the purpose for reducing production cost may be implemented, and the scheme being prepared in situ also has
Advantage with short production cycle and flexible.One end of third conveying device 43 is connected with digester 42, the other end and desulfurization unit
It is connected, desulfurizing agent is delivered to desulfurization unit.In one embodiment, third conveying device 43 is screw delivery pump.But
It is it will be apparent to a skilled person that third conveying device 43 can be and commonly used in the art have Gaseous materials conveying
Any conveying device of function.
In one embodiment, preparation unit further includes measuring chute 41.In the arrival end and feeding unit of measuring chute 41
Second conveying device 36 is connected, outlet end is connected with digester 42, and measuring chute 41 include load sensor (in figure not
Show) and measuring chute 41 outlet end speed regulation revolution air valve (not shown).Load sensor can detecte metering
The weight of the raw material in storehouse 41, speed regulation revolution air valve can control the discharge quantity of measuring chute 41, to control into digester 42
Raw material total amount, meet the production requirement of desulfurizing agent to guarantee suitable raw material amount, and whole rhythm of production can be cooperated
Control the stabilization of the preparation speed of desulfurizing agent.In this way, by the way that measuring chute 41 is arranged in the upstream of digester 42, it is ensured that preparation
Desulfurizing agent quality and improve the preparation efficiency of desulfurizing agent.
In one embodiment, preparation unit further includes the 4th conveying device 44.One end of 4th conveying device 44 with disappear
Device 42 is connected, the other end is connected with the apparatus for feeding (not shown) of kiln tail preheater 2 for change, thus by the desulfurization of preparation
Agent is fed directly to kiln tail preheater 2 to react with the sulfurous gas in kiln tail preheater 2, that is, is acutely disturbed with flue gas
Contact completes more deep desulphurization reaction, that is to say the desulfurization by dry method in traditional handicraft.In this way, using two kinds simultaneously
Sulfur method, it is ensured that 85% or more desulfurization, by key area SO2Concentration of emission is controlled in 100mg/Nm3Environmental protection below is wanted
It asks.Preferably, it is provided with triple valve 46 on the tracheae for connecting the 4th conveying device 44 and digester 42, triple valve 46
Arrival end is connected to 42, two outlet ends of digester and is connected respectively to third conveying device 43 and the 4th conveying device 44, with root
The amount for entering third transmission device 43 and the desulfurizing agent into the 4th transmission device 44 is adjusted according to specific concentration of emission, reaches pre-
Fixed desulfurization effect.
In one embodiment, preparation unit further includes water injector 45.Water injector 45 is connected with digester 42, institute
The water of ejection, which sufficiently reacts in digester 42 with raw material, generates desulfurizing agent.
With continued reference to Fig. 1, desulfurization unit includes desulfurization reactor 51 and the first rotoclone collector group 52.
Desulfurization reactor 51 is connected with the third conveying device 43 in preparation unit to obtain desulfurizing agent.First whirlwind is received
Dirt device group 52 includes multiple rotoclone collectors, and the air intake of each of multiple rotoclone collectors is connected to kiln tail preheater 2
In first order preheater windspout barrel in corresponding one, outlet air end be connected to desulfurization reactor 51, by kiln tail preheater 2
In sulfurous gas be sent into desulfurization reactor 51.In this way, increasing in the outlet end of the first order cyclone cylinder of original pre-heating system
Add the first rotoclone collector group 52, the dust content of the sulfur contained high temoperature gas of first order cyclone cylinder out can be reduced to about 15g/
Nm3, the collection again to raw meal powder is realized, to greatly reduce the consumption of desulfurizing agent, increase desulfuration byproduct purity and reduce
Desulfurization by-product total amount.Purified sulfur-containing smoke gas enters desulfurization reactor 51.Desulfurization reactor 51 is with optimization fluid point
The efficient low-resistance reactor of cloth special construction, sulfur-containing smoke gas can carry out in desulfurization reactor 51 with desulfurizing agent greater than 5 seconds
Sufficiently reaction is to generate calcium sulfate (CaSO2).Reduce the efficient de- of gas flow rates, increase desulfurizing agent and gas reaction speed
Reaction of Salmon-Saxl process can effectively remove SO2, guarantee the SO in discharge gas2Concentration reaches national environmental standard requirement.In a reality
It applies in example, the first rotoclone collector group 52 includes four rotoclone collectors, and each of four rotoclone collectors respectively correspond
Corresponding one in first order cyclone cylinder in kiln tail preheater 2, to gather dust high temperature sulfurous gas, it is de- to reduce feeding
The dust content of sulfurous gas in reaction of Salmon-Saxl device 51.
Referring to Fig.1, the utility model proposes self-loopa dry method desulfuration system in Matter Transfer unit include second rotation
Wind dust-precipitator group 61 and machine for zipper 62.
The air intake of second rotoclone collector group 61 is connected with the subsequent air hose of desulfurization reactor 51 in desulfurization unit, with
Flue gas after receiving desulfurization, outlet air end are connected to raw grinding system 8.One end of machine for zipper 62 is connected to the second cyclone dust collection
Discharge end, the other end of device group 61 are connected to the conveying equipment of exhaust treatment system 7, will pass through the second rotoclone collector group 61
Gas after gathering dust is sent into raw grinding system 8, and the desulfuration byproduct accepted is sent into the defeated of exhaust treatment system 7 by machine for zipper 62
Send equipment.The flue gas discharged from desulfurization reactor 51 gathering dust by the second rotoclone collector group 61, it is ensured that enters life
The gas of feed powder grinding system 8 is practically free of calcium sulfate and white lime.In addition, the material collected by the second rotoclone collector group 61
It can be sent by the conveying equipment of machine for zipper 62 and exhaust treatment system 7 to an individual storage cavern, and according to cement grinding process
It needs, is added in cement grinding system (not shown) as adjustable solidification agent, the Matter Transfer for forming cement factory is utilized, do not produced
Raw waste, the self-loopa desulphurization system for meeting national requirements for environmental protection；It simultaneously can also be by machine for zipper 62 and exhaust treatment system 7
Conveying equipment is sent into kiln elevator, into kiln tail preheater system 2, with common dry technique and smoke reaction, the row of reduction
Put SO in flue gas2Content, it is ensured that reach best desulfurization effect.
In one embodiment, the second rotoclone collector group 61 includes two rotoclone collectors, in two rotoclone collectors
The air intake of each the subsequent air hose of desulfurization reactor 51, the discharge end that are connected in desulfurization unit be connected to machine for zipper
62.It will be understood by those skilled in the art that the not limited to of the second rotoclone collector group 61 is in two, and can root
It adjusts according to specific operating condition needs.
By above description it is recognised that the utility model proposes self-loopa dry method desulfuration system can be with manufacture of cement
Main technical process height fusion, outsourcing desulfurizing agent is not necessarily in sulfur removal technology, realizes the effect for reducing production cost；In addition, from
The blanking pipe 21 of afterbody cyclone cylinder in kiln tail preheater 2 extracts raw material, can be to avoid straight from the air outlet of dore furnace 1
The problem of connecing and extract flue gas and influence the thermally equilibrated stability of kiln tail process system, and then increasing the heat loss of system；In kiln tail
Increase the first rotoclone collector group 52, the cigarette that can be lowered into desulfurization reactor 51 at the first order cyclone cylinder of preheater 2
The dust content of gas, to reduce the dosage of desulfurizing agent；Increase by the second rotoclone collector group 61, Ke Yibao in Matter Transfer unit
The gas that card enters raw grinding system 8 is practically free of calcium sulfate and white lime.Self-loopa dry method disclosed by the utility model is de-
Sulphur system is truly realized in the case where not affecting the normal production, be not necessarily to outsourcing desulfurizing agent, woth no need to increase workshop and
Producers, and flexible operation, construction period are short, do not influence the normal production of production line, are guaranteeing compared with low operating cost situation
Lower stabilization flexibly controls SO2Concentration of emission.
Although having been combined specific exemplary embodiment to be illustrated the utility model it should be appreciated that this
Utility model is not limited to disclosed embodiment, and being intended to covering includes in appended claims and its equivalents
Various modifications and equivalent structure in spirit and scope.
Claims (20)
1. a kind of cement industry self-loopa dry method desulfuration system, which is characterized in that the cement industry self-loopa dry desulfurization system
System includes:
Feeding unit, the feeding unit are connected raw to obtain heat with the blanking pipe of the one cyclonic cylinder in kiln tail preheater
Material；
Preparation unit, the preparation unit are connected with the feeding unit, to prepare desulfurizing agent using hot raw material；
Desulfurization unit, the desulfurization unit are connected with the preparation unit and the kiln tail preheater respectively, to obtain respectively
Desulfurizing agent and sulfurous gas simultaneously complete desulphurization reaction；With
Matter Transfer unit, the Matter Transfer unit is connected with the desulfurization unit and cement preparation system respectively, so that cigarette
Product after desulfurization is used for cement grinding system.
2. cement industry self-loopa dry method desulfuration system according to claim 1, which is characterized in that the one cyclonic cylinder
For the afterbody cyclone cylinder in the kiln tail preheater.
3. cement industry self-loopa dry method desulfuration system according to claim 1, which is characterized in that the feeding unit packet
It includes:
One end of feeding pipeline, the feeding pipeline is connected with the blanking pipe, raw to obtain heat from the blanking pipe
Material, and trapped line pressure valve is provided on the feeding pipeline；
First conveying device, first conveying device are connected with the other end of the feeding pipeline；
First dust-precipitator, the blast pipe of first dust-precipitator are connected with first conveying device to obtain raw material, and
First dust-precipitator has the first dust-precipitator blower；With
Second conveying device, one end of second conveying device is connected with first dust-precipitator, the other end and the system
Standby unit is connected.
4. cement industry self-loopa dry method desulfuration system according to claim 3, which is characterized in that the first conveying dress
It is set to speed regulation high-temperature spiral conveyer.
5. cement industry self-loopa dry method desulfuration system according to claim 3, which is characterized in that first dust-precipitator
For refractory ceramics filter bag dust-precipitator.
6. cement industry self-loopa dry method desulfuration system according to claim 3, which is characterized in that the second conveying dress
It is set to metering screw conveyer, and the inlet of second conveying device is provided with speed regulation revolution air valve.
7. cement industry self-loopa dry method desulfuration system according to claim 3, which is characterized in that the kiln tail preheater
For Pyatyi preheater, the one cyclonic cylinder is level V cyclone cylinder.
8. cement industry self-loopa dry method desulfuration system according to claim 3, which is characterized in that the feeding unit is also
Including air bubble, the air bubble is arranged on the feeding pipeline and relative to the trapped line pressure valve closer to the feeder pipe
Road.
9. cement industry self-loopa dry method desulfuration system according to claim 3, which is characterized in that the feeding unit is also
Including air cleaning unit, the air cleaning unit is for connecting first conveying device and first dust-precipitator
On tracheae.
10. cement industry self-loopa dry method desulfuration system according to claim 3, which is characterized in that the trapped line pressure valve is
Gate valve.
11. cement industry self-loopa dry method desulfuration system according to claim 1, which is characterized in that the preparation unit
Include:
Digester, the digester are connected with the feeding unit, to obtain raw material and prepare desulfurizing agent；With
Third conveying device, one end of the third conveying device is connected with the digester, the other end and the desulfurization list
Member is connected, and desulfurizing agent is delivered to the desulfurization unit.
12. cement industry self-loopa dry method desulfuration system according to claim 11, which is characterized in that the third conveying
Device is helicoidal pump.
13. cement industry self-loopa dry method desulfuration system according to claim 11, which is characterized in that the preparation unit
It further include measuring chute, the arrival end of the measuring chute is connected with the feeding unit, outlet end is connected with the digester,
And the measuring chute include load sensor and be connected with the load sensor be arranged in the measuring chute go out
Air valve is turned round in the speed regulation at mouth end, and the measuring chute is used to control the weight into the raw material of the digester.
14. cement industry self-loopa dry method desulfuration system according to claim 11, which is characterized in that the preparation unit
It further include the 4th conveying device, one end of the 4th conveying device is connected with the digester, the other end and the kiln tail
The feed pipe of preheater is connected.
15. cement industry self-loopa dry method desulfuration system according to claim 14, which is characterized in that described for connecting
It is provided with triple valve in 4th conveying device and the expects pipe of the digester, the arrival end of the triple valve is connected to the digestion
Device, two outlet ends are connected respectively to the third conveying device and the 4th conveying device.
16. cement industry self-loopa dry method desulfuration system according to claim 11, which is characterized in that the preparation unit
It further include water injector, the water injector is connected to spray water into the digester with the digester.
17. cement industry self-loopa dry method desulfuration system according to claim 1, which is characterized in that the desulfurization unit
Include:
Desulfurization reactor, the desulfurization reactor are connected with the preparation unit to obtain desulfurizing agent；With
First rotoclone collector group, the first rotoclone collector group include multiple rotoclone collectors, the multiple cyclone dust collection
The air intake of each of device is connected to corresponding one, outlet air end in the first order cyclone cylinder in the kiln tail preheater
It is all connected to the desulfurization reactor, the sulfurous gas in the kiln tail preheater is sent into the desulfurization reactor, it is described
The discharge end of each of multiple rotoclone collectors is connected with the feed pipe of the kiln tail preheater.
18. cement industry self-loopa dry method desulfuration system according to claim 17, which is characterized in that first whirlwind
Dust-precipitator group includes four rotoclone collectors.
19. cement industry self-loopa dry method desulfuration system according to claim 1, which is characterized in that the Matter Transfer
Unit includes:
The air intake of second rotoclone collector group, the second rotoclone collector group is connected with the desulfurization unit, to receive
The flue gas being discharged from the desulfurization unit；With
Machine for zipper, one end of the machine for zipper is connected with the discharge end of the second rotoclone collector group, the other end and exhaust gas
Processing system or cement grinding system are connected.
20. cement industry self-loopa dry method desulfuration system according to claim 19, which is characterized in that second whirlwind
Dust-precipitator group includes two rotoclone collectors, and the air intake of each of described two rotoclone collectors is connected to the desulfurization
Unit, outlet air end are connected to raw material grinding system, discharge end is connected to the machine for zipper.
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| CN201820751981.7U CN208927928U (en) | 2018-05-21 | 2018-05-21 | Cement industry self-loopa dry method desulfuration system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109772144A (en) * | 2018-05-21 | 2019-05-21 | 莱歇研磨机械制造(上海)有限公司 | Cement industry self-loopa dry method desulfuration system and method |
| CN110052152A (en) * | 2019-06-06 | 2019-07-26 | 天津水泥工业设计研究院有限公司 | One kind being based on cement clinker production line calcium circulation desulfurization system and sulfur removal technology |
| CN112426872A (en) * | 2020-11-30 | 2021-03-02 | 天津中材工程研究中心有限公司 | Method for improving purity of desulfurizer for limestone-gypsum wet desulphurization |
-
2018
- 2018-05-21 CN CN201820751981.7U patent/CN208927928U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109772144A (en) * | 2018-05-21 | 2019-05-21 | 莱歇研磨机械制造(上海)有限公司 | Cement industry self-loopa dry method desulfuration system and method |
| CN110052152A (en) * | 2019-06-06 | 2019-07-26 | 天津水泥工业设计研究院有限公司 | One kind being based on cement clinker production line calcium circulation desulfurization system and sulfur removal technology |
| CN110052152B (en) * | 2019-06-06 | 2024-01-05 | 天津水泥工业设计研究院有限公司 | Calcium circulation desulfurization system and desulfurization process based on cement clinker production line |
| CN112426872A (en) * | 2020-11-30 | 2021-03-02 | 天津中材工程研究中心有限公司 | Method for improving purity of desulfurizer for limestone-gypsum wet desulphurization |
| CN112426872B (en) * | 2020-11-30 | 2022-08-09 | 天津中材工程研究中心有限公司 | Method for improving purity of desulfurizer for limestone-gypsum wet desulphurization |
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