CN205340557U - System for utilize SO2 in online desorption kiln tail flue gas of raw material powder - Google Patents
System for utilize SO2 in online desorption kiln tail flue gas of raw material powder Download PDFInfo
- Publication number
- CN205340557U CN205340557U CN201620080646.XU CN201620080646U CN205340557U CN 205340557 U CN205340557 U CN 205340557U CN 201620080646 U CN201620080646 U CN 201620080646U CN 205340557 U CN205340557 U CN 205340557U
- Authority
- CN
- China
- Prior art keywords
- raw meal
- meal powder
- kiln
- kiln tail
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Furnace Details (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a system for utilize SO2 in online desorption kiln tail flue gas of raw material powder, include: it is effective in the branch material pipe of telling the raw material powder that contains a large amount of caO that water receiving stall tail preheats in advance a decomposition system whirlwind section of thick bamboo or reactor unloading, with divide the material to manage being used for the dispersion devices in the exhaust piping of sending into heat transfer pipeline and/or kiln tail after the dispersion of raw material powder of ejection of compact connection, and for realize the conveying system of material transport, the utility model discloses to come from cement and preheat in advance the raw material powder that a decomposition system whirlwind section of thick bamboo or reactor unloading pipe contain a large amount of caO and send into buffer stock bin, a measuring equipment measurement quantitative material through it under, feeding conveying system is through the transport to in getting into the exhaust piping of heat exchange tube way and kiln tail by dispersion devices after finally fully being disperseed, the SO2 in caO and the flue gas reacts, reaches the desulfurization purpose, the utility model discloses desulfurization efficiency can reach more than 50%, and the flow is simple and convenient, and control is simple, invests in for a short time, and operating power consumption is little and do not produce extra discarded object.
Description
Technical field
This utility model belongs to technical field of cement production, utilizes raw meal powder to remove SO in kiln exit gas online particularly to one2System.
Background technology
Acid rain, greenhouse effect and depletion of the ozone layer are the three overall situation problems that the mankind currently face, and wherein acid rain is the problem that must be first solved.What China's acid rain was formed is primarily due to a large amount of SO2Discharge, cement industry is as SO2Discharge rich and influential family, it is imperative for limiting its discharge, and Environmental Protection in China department discharged in " cement industry atmosphere pollutants emission standards " (GB4915-2013) put into effect for SO for cement industry in 20132Discharge just propose more strict emission index, cement kiln and kiln tail bootstrap system generally area SO2Concentration of emission requires to control at 200mg/m3Within, key area controls at 100mg/m3Within.
Cement industry sulphur emissions has the feature of himself, and its sulfur source has two, raw material sulfur-bearing and fuel sulfur-bearing, and comparatively speaking in raw material, sulfur is more easy to for modern cement industry and is carried over, contaminated environment.The contained sulfur that reason is in that in raw material limestone mainly exists with pyritous form, and its maximum oxidation rate corresponding temperature is approximately about 500 DEG C, and cement slurry is not formed and can adsorb SO in a large number at this temperature2CaO, the SO therefore formed2, the overwhelming majority is carried over system.From the practical operation situation of a plurality of cement clinker production line in 1500 existing for current China, the SO that this kind of situation causes2Discharge, can reach 1300mg/Nm3。
The traditional handicraft being relatively suitable for cement kiln end flue gas desulfurization at present is mainly wet desulfurization of flue gas by limestone-gypsum method method.The method technology maturation, reliable, equipment and technology are easy to obtain；Desulfurizing agent limestone is easy to get, low price；Side-product-Gypsum Fibrosum has certain market at present；To SO in flue gas2Concentration change, desulphurization system can keep higher desulfuration efficiency and system stability.But its floor space is relatively big, desulfurizing tower equipment investment is slightly higher；Desulfurizing tower circulating load is big, and power consumption is higher；System has the tendency that fouling, blocking occur；Gypsum purity must just have outlet more than 94%.
Summary of the invention
In order to overcome the shortcoming of above-mentioned prior art, the purpose of this utility model is in that to provide one to utilize raw meal powder to remove SO in kiln exit gas online2System, have reduced investment, easy to operate, without additional waste discharge feature.
To achieve these goals, the technical solution adopted in the utility model is:
One utilizes raw meal powder to remove SO in kiln exit gas online2System, including:
Connect cement kiln end precalcining system cyclone cylinder or reactor tremie pipe for separating the sub-feed tube 1 of the raw meal powder containing a large amount of CaO；
What be connected with the discharging of described sub-feed tube 1 is used for the dispersal device 11 in the exhaust piping sending into heat exchange pipeline and/or kiln tail after raw meal powder dispersion；
And, for realizing the induction system of material conveying.
This utility model system may also include that
The surge bunker 5 being connected with described sub-feed tube 1 raw meal powder discharging；
The metering device 7 being connected with described surge bunker 5 discharge end；
Wherein,
Arranging push-pull valve 6 on the export pipeline of surge bunker 5, the raw meal powder entrance surge bunker 5 going out sub-feed tube 1 is kept in, and described surge bunker 5 uses as feed bin, and it is steel plate or the concrete storehouse with refractory lining and Insulation；
The discharging of metering device 7 enters dispersal device 11 by induction system.
This utility model system may also include that
The chiller 3 for raw meal powder is lowered the temperature being connected with described sub-feed tube 1 discharge end, the export pipeline of chiller 3 arranges flap valve 4, go out the raw meal powder of sub-feed tube to be introduced into chiller 3 and cool down, entering back into surge bunker 5 to keep in, the power resources of described chiller 3 are in self negative pressure of kiln tail preheater system.
Described induction system adopts pneumatic conveying mode or machinery mode of movement, according to pneumatic conveying mode, induction system includes the feeding boots 8 connecing metering device 7 discharge end, feeding boots 8 are arranged on Pneumatic conveying pipeline 9, Pneumatic conveying pipeline 9 entrance point is connected with air and is arranged to the cold blast sliding valve 10 that the air quantity entered in pipeline is adjusted, the exhaust piping of another termination heat exchange pipeline and/or kiln tail, its power resources are in the negative pressure of entrance point, and dispersal device 11 is arranged on the port of export position of Pneumatic conveying pipeline 9；According to machinery mode of movement, induction system includes the mechanical conveying equipment 9 connecing metering device 7 discharge end, and raw meal powder is delivered to dispersal device 11 by machinery conveying equipment 9.
Described kiln tail precalcining system cyclone cylinder or reactor tremie pipe are that the tremie pipe of the most subordinate of precalcining system or reactor tremie pipe or other can obtain the tremie pipe containing a large amount of CaO (CaO has unsalted surface, and reactivity is high) raw meal powder；Described heat exchange pipeline is cement kiln end preheater heat exchange pipeline at different levels, and described exhaust piping is the cement kiln end preheater whole section of exhaust piping to kiln tail dust-precipitator.
If this utility model adopts pneumatic conveying mode, chiller 3 can be not provided with.
Compared with prior art, the beneficial effects of the utility model are:
1) technical process is simple, and reduced investment, floor space is little.
2) operation energy consumption is low.
3) easy and simple to handle.
4) to affect normal production cycles short for transformation process.
5) additional waste is not discharged.
To sum up, this utility model desulfuration efficiency can reach more than 50%, simple flow, controls simple, invests little, and operation energy consumption is little and does not produce additional waste.
Accompanying drawing explanation
Fig. 1 is flue gas desulfurization process block diagram of the present utility model.
Fig. 2 is flue gas desulphurization system form one structural representation of the present utility model.
Fig. 3 is flue gas desulphurization system form two structural representation of the present utility model.
Fig. 4 is flue gas desulphurization system form three structural representation of the present utility model.
Detailed description of the invention
Embodiment of the present utility model is described in detail below in conjunction with drawings and Examples.
As it is shown in figure 1, the raw meal powder that utilizes that this utility model relies on removes SO in kiln exit gas online2Technique, comprise the steps:
The first step: separate the raw meal powder containing a large amount of CaO by sub-feed tube from cement kiln end precalcining system cyclone cylinder or reactor tremie pipe；
Second step: by the exhaust piping sending into heat exchange pipeline and/or kiln tail after fully dispersed for raw meal powder, CaO and the SO in flue gas2React, reach desulfurization purpose.
Described raw meal powder is according to pneumatic conveying mode, and its power resources are in self negative pressure of kiln tail preheater system；According to machinery mode of movement, its conveying equipment is machinery conveying equipment.
Wherein, before the dispersing, can first measuring, the amount of the raw meal powder of metering is by SO in the flue gas of discharge pre-heating system2Concentration is determined, it is ensured that calcium to sulphur mole ratio is 1:1～10:1.
And before measuring, can first cool down again, raw meal powder is cooled to less than 300 DEG C to be measured again, and cooling power resources are in self negative pressure of kiln tail preheater system.
If raw meal powder is according to pneumatic conveying mode, its power resources are in self negative pressure of kiln tail preheater system；According to machinery mode of movement, its conveying equipment is machinery conveying equipment.
This utility model provides corresponding system simultaneously, including following three kinds of forms.
As in figure 2 it is shown, one of be the form of this utility model system:
The concrete position that obtains of desulfurizing agent is cement kiln end precalcining system cyclone cylinder or reactor tremie pipe.Separate material mounted thereon resistant to elevated temperatures push-pull valve 2 herein by sub-feed tube 1, cut off entering desulphurization system material if desired.
The desulfurizing agent separated enters surge bunker 5, surge bunker 5 inwall sets fire-resistant pouring material, and surge bunker 5 divides into resistant to elevated temperatures push-pull valve 6, and resistant to elevated temperatures metering device 7 divided into by push-pull valve 6, carrying out the accurate metering of desulfurizing agent, the desulfurizing agent after metering feeds in air conveying feeding boots 8.
Feeding boots 8 are arranged on Pneumatic conveying pipeline 9, and pipe head is connected with air, and the other end accesses on heat exchanger tube or exhaust piping, and its power resources are in the negative pressure of entrance point.Pipe head arranges cold blast sliding valve 10, and the air quantity entered in conveyance conduit is adjusted.
The final whereabouts of desulfurizing agent is decided by the link position of Pneumatic conveying pipeline 9.The link position of Pneumatic conveying pipeline 9, is decided by system SO2Content and produce position, fully dispersed by the dispersal device 11 being arranged on entrance before desulfurizing agent feeding system.
The desulfurizing agent material of feeding precalcining system, and the SO in flue gas2React and reach desulfurization purpose.
System arranges PLC and regulates system, controls to adjust material, the size of air quantity.Its control flow is that the size of feeding system feeding capacity is by SO in flue gas2The size of concentration is adjusted, and air quantity passes through inventory size adjustment.
As it is shown on figure 3, be the two of the form of this utility model system:
The concrete position that obtains of desulfurizing agent is cement kiln end precalcining system cyclone cylinder or reactor tremie pipe.Separate material mounted thereon resistant to elevated temperatures push-pull valve 2 herein by sub-feed tube 1, cut off entering desulphurization system material if desired.
The desulfurizing agent separated enters chiller 3, after cooling, temperature of charge is down to less than 300 DEG C, after cooling, desulfurizing agent enters surge bunker 5 by flap valve 4, surge bunker 5 inwall sets fire-resistant pouring material, and surge bunker divides into push-pull valve 6, and metering device 7 divided into by push-pull valve 6, carrying out the accurate metering of desulfurizing agent, the desulfurizing agent after metering feeds in air conveying feeding boots 8.
Feeding boots 8 are arranged on Pneumatic conveying pipeline 9, and pipe head is connected with air, and the other end accesses on heat exchanger tube or exhaust piping, and its power resources are in the negative pressure of arrival end.Pipe head arranges cold blast sliding valve 10, and the air quantity entered in conveyance conduit is adjusted.
The final whereabouts of desulfurizing agent is decided by the link position of Pneumatic conveying pipeline 9.The link position of Pneumatic conveying pipeline 9, is decided by system SO2Content and produce position, fully dispersed by the dispersal device 11 being arranged on entrance before desulfurizing agent feeding system.
The desulfurizing agent material of feeding precalcining system, and the SO in flue gas2React and reach desulfurization purpose.
System arranges PLC and regulates system, controls to adjust material, the size of air quantity.Its control flow is that the size of feeding system feeding capacity is by SO in flue gas2The size of concentration is adjusted, and air quantity passes through inventory size adjustment.
As shown in Figure 4, for the three of the form of this utility model system:
The concrete position that obtains of desulfurizing agent is cement kiln end precalcining system cyclone cylinder or reactor tremie pipe.Separate material mounted thereon resistant to elevated temperatures push-pull valve 2 herein by sub-feed tube 1, cut off entering desulphurization system material if desired.
The desulfurizing agent separated enters chiller 3, after cooling, temperature of charge is down to less than 300 DEG C, after cooling, desulfurizing agent enters surge bunker 5 by flap valve 4, surge bunker 5 inwall sets fire-resistant pouring material, and surge bunker divides into push-pull valve 6, and metering device 7 divided into by push-pull valve 6, carry out the accurate metering of desulfurizing agent, the desulfurizing agent feeding conveying equipment 12 after metering.
Feeding dispersal device 11 after conveying equipment 12 is carried, after fully dispersed, feeding heat exchanger tube and kiln tail wind converging tube carry out desulfurization process.
The desulfurizing agent material of feeding system, and the SO in flue gas2React and reach desulfurization purpose.
System arranges PLC and regulates system, controls to adjust material, the size of air quantity.Its control flow is that the size of feeding system feeding capacity is by SO in flue gas2The size of concentration is adjusted, and air quantity passes through inventory size adjustment.
Claims (5)
1. one kind utilizes raw meal powder to remove SO in kiln exit gas online2System, it is characterised in that including:
Connect cement kiln end precalcining system cyclone cylinder or reactor tremie pipe for separating the sub-feed tube (1) of the raw meal powder containing a large amount of CaO；
What be connected with described sub-feed tube (1) discharging is used for the dispersal device (11) in the exhaust piping sending into heat exchange pipeline and/or kiln tail after raw meal powder dispersion；
And, for realizing the induction system of material conveying.
2. one utilizes raw meal powder to remove SO in kiln exit gas online according to claim 12System, it is characterised in that also include:
The surge bunker (5) being connected with described sub-feed tube (1) raw meal powder discharging；
The metering device (7) being connected with described surge bunker (5) discharge end；
Wherein,
The export pipeline of surge bunker (5) arranges push-pull valve (6), raw meal powder entrance surge bunker (5) going out sub-feed tube is kept in, described surge bunker (5) uses as feed bin, and it is steel plate or the concrete storehouse with refractory lining and Insulation；
The discharging of metering device (7) enters dispersal device (11) by induction system.
3. one utilizes raw meal powder to remove SO in kiln exit gas online according to claim 22System, it is characterized in that, also include: the chiller (3) for raw meal powder is lowered the temperature being connected with described sub-feed tube (1) raw meal powder discharge end, the export pipeline of chiller (3) arranges flap valve (4), go out the raw meal powder of sub-feed tube to be introduced into chiller (3) and cool down, entering back into surge bunker (5) to keep in, the power resources of described chiller (3) are in self negative pressure of kiln tail preheater system.
4. one utilizes raw meal powder to remove SO in kiln exit gas online according to claim 12System, it is characterized in that, described induction system adopts pneumatic conveying mode or machinery mode of movement, according to pneumatic conveying mode, induction system includes the feeding boots (8) connecing metering device (7) discharge end, feeding boots (8) are arranged on Pneumatic conveying pipeline (9), Pneumatic conveying pipeline (9) entrance point is connected with air and is arranged to the cold blast sliding valve (10) that the air quantity entered in pipeline is adjusted, the exhaust piping of another termination heat exchange pipeline and/or kiln tail, its power resources are in the negative pressure of entrance point, dispersal device (11) is arranged on the port of export position of Pneumatic conveying pipeline (9)；According to machinery mode of movement, induction system includes the mechanical conveying equipment (9) connecing metering device (7) discharge end, and raw meal powder is delivered to dispersal device (11) by machinery conveying equipment (9).
5. one utilizes raw meal powder to remove SO in kiln exit gas online according to claim 12System, it is characterised in that described kiln tail precalcining system cyclone cylinder or reactor tremie pipe are tremie pipe or the reactor tremie pipe of the most subordinate of precalcining system；Described heat exchange pipeline is cement kiln end preheater heat exchange pipeline at different levels, and described exhaust piping is the cement kiln end preheater whole section of exhaust piping to kiln tail dust-precipitator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620080646.XU CN205340557U (en) | 2016-01-27 | 2016-01-27 | System for utilize SO2 in online desorption kiln tail flue gas of raw material powder |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620080646.XU CN205340557U (en) | 2016-01-27 | 2016-01-27 | System for utilize SO2 in online desorption kiln tail flue gas of raw material powder |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205340557U true CN205340557U (en) | 2016-06-29 |
Family
ID=56184380
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620080646.XU Active CN205340557U (en) | 2016-01-27 | 2016-01-27 | System for utilize SO2 in online desorption kiln tail flue gas of raw material powder |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205340557U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105771616A (en) * | 2016-01-27 | 2016-07-20 | 西安建筑科技大学 | Method and system for on-line removal of SO2 in kiln tail flue gas by using raw material powder |
| CN114870613A (en) * | 2022-04-08 | 2022-08-09 | 福建中翼节能科技有限公司 | Novel cement kiln flue gas environmental protection desulfurization device |
-
2016
- 2016-01-27 CN CN201620080646.XU patent/CN205340557U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105771616A (en) * | 2016-01-27 | 2016-07-20 | 西安建筑科技大学 | Method and system for on-line removal of SO2 in kiln tail flue gas by using raw material powder |
| CN114870613A (en) * | 2022-04-08 | 2022-08-09 | 福建中翼节能科技有限公司 | Novel cement kiln flue gas environmental protection desulfurization device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103771734B (en) | A kind of mass-producing calcination processing utilizes the method for electrolytic manganese residues | |
| CN105771616A (en) | Method and system for on-line removal of SO2 in kiln tail flue gas by using raw material powder | |
| CN102502524B (en) | Method for producing sulfur dioxide from calcium sulfate and sulfur | |
| CN109776002B (en) | Suspension calcination activation system and method suitable for clay mine tailings | |
| CN102380903A (en) | Large-scale production process for paper surface gypsum boards with annual yield scale being 50 million square meters | |
| CN205340557U (en) | System for utilize SO2 in online desorption kiln tail flue gas of raw material powder | |
| CN105536506A (en) | Online kiln exit gas self-desulfuration method and system | |
| CN101955166B (en) | Method for decomposing semi-hydrated phosphogypsum | |
| CN207619279U (en) | A kind of system carrying out desulfurization using digestive fever raw material | |
| CN101306803A (en) | Process for producing sulfate acid from gypsum | |
| CN205340559U (en) | System for online kiln tail flue gas is from desulfurization | |
| CN109896760A (en) | A kind of device and technique using cement kiln end lime burning | |
| CN110052153B (en) | Desulfurizing agent preparation unit based on cement clinker production line calcium cycle | |
| CN204224467U (en) | Limestone kiln and system for producing calcium carbide | |
| CN103241717B (en) | Drying and calcining process and device for coproduction of sulfuric acid and cement from gypsum | |
| CN105152141B (en) | A kind of gypsum relieving haperacidity thermal technology and device | |
| CN110052158A (en) | One kind recycling dry method desulfuration system based on cement clinker production line calcium | |
| CN110052151B (en) | Calcium-cycle semi-dry desulfurization system based on cement clinker production line | |
| CN110052152A (en) | One kind being based on cement clinker production line calcium circulation desulfurization system and sulfur removal technology | |
| CN205023854U (en) | Gypsum relieving haperacidity thermal technology device | |
| CN105541141A (en) | A device and a method for preparing cement from dry and wet calcium carbide slag | |
| CN210625308U (en) | Independent pulverized coal conveying system and cement kiln using same | |
| CN113149487B (en) | Gypsum calcining device and calcining system | |
| CN201288148Y (en) | Novel multifuel combustion kiln | |
| CN209275655U (en) | In-furnace calcium spraying air-transport system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |