CN205340559U - System for online kiln tail flue gas is from desulfurization - Google Patents
System for online kiln tail flue gas is from desulfurization Download PDFInfo
- Publication number
- CN205340559U CN205340559U CN201620080435.6U CN201620080435U CN205340559U CN 205340559 U CN205340559 U CN 205340559U CN 201620080435 U CN201620080435 U CN 201620080435U CN 205340559 U CN205340559 U CN 205340559U
- Authority
- CN
- China
- Prior art keywords
- reactor
- desulfurization
- kiln
- discharge end
- online
- 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)
Abstract
The utility model discloses a system for online kiln tail flue gas is from desulfurization, 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 the metering device who is used for measuring raw material powder quantity who divides that material pipe raw material powder discharge end connects, with the metering device discharge end is connected have spraying system be used for make the raw material powder generate ca (OH's) 2 reation kettle, with what the reation kettle discharge end was connected is used for the dispersion devices in the exhaust piping of sending into heat transfer pipeline and/or kiln tail after 2 dispersions of ca (OH), and be used for realizing the conveying system that the material carried, the utility model discloses send the raw material powder into reation kettle, the reaction of caO and water generates ca (OH) 2 in the raw material, and in carrying the exhaust piping that gets into heat transfer pipeline and kiln tail once more, the SO2 in ca (OH) 2 and the flue gas reacts and reaches the desulfurization purpose, the utility model discloses desulfurization efficiency can reach more than 60%, 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, particularly to a kind of online kiln exit gas from the system of desulfurization.
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 a kind of online kiln exit gas from the system of desulfurization, has reduced investment, feature easy to operate, that discharge without additional waste.
To achieve these goals, the technical solution adopted in the utility model is:
A kind of online kiln exit gas from the system of desulfurization, 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；
The metering device 7 for measuring raw meal powder consumption being connected with described sub-feed tube 1 raw meal powder discharge end；
Be connected with described metering device 7 discharge end with spray system be used for make raw meal powder generate Ca (OH)2Reactor 11；
What be connected with described reactor 11 discharge end is used for Ca (OH)2The dispersal device 12 in the exhaust piping of heat exchange pipeline and/or kiln tail is sent into after dispersion；
And, for realizing the induction system of material conveying.
It is provided with surge bunker 5 between described metering device 7 and sub-feed tube 1, the export pipeline of surge bunker 5 arranges push-pull valve 6, 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.
It is provided with chiller 3 between described surge bunker 5 and sub-feed tube 1, the export pipeline of chiller 3 arranges flap valve 4, going out the raw meal powder of sub-feed tube to be introduced into chiller 3 and cool down, enter back into surge bunker 5 and 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, then reactor 11 is fluidization reactor, induction system includes the feeding boots 8 connecing metering device 7 discharge end, feeding boots 8 are arranged on pneumatic transport equipment 9, pneumatic transport equipment 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, another terminates reactor 11, and it is ultimately connected to heat exchange pipeline and/or the exhaust piping of kiln tail, its power resources are in the negative pressure of entrance point, dispersal device 12 is arranged on the export pipeline end-position of reactor 11；According to machinery mode of movement, then reactor 11 is stirring-type reactor, and induction system includes the mechanical conveying equipment 9 connecing reactor 11 discharge end, and machinery conveying equipment 9 is by Ca (OH)2Deliver to dispersal device 12.
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.
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 60%, 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 online kiln exit gas that this utility model relies on is from the method for desulfurization, 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: deliver in reactor after being measured by raw meal powder, in still, water spray reacts with CaO simultaneously, generates Ca (OH)2；
3rd step: by Ca (OH)2Send in the exhaust piping of heat exchange pipeline and/or kiln tail after fully dispersed, Ca (OH)2With the SO in flue gas2React, reach desulfurization purpose.
Wherein, according to pneumatic conveying mode, its power resources are in self negative pressure of kiln tail preheater system, and reactor is fluidization reactor；According to machinery mode of movement, its conveying equipment is machinery conveying equipment, such as elevator；Reactor is stirring-type reactor, and raw meal powder is first cooled to less than 300 DEG C in chiller and measures, and the power resources of chiller are in self negative pressure of kiln tail preheater system.
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 transport equipment 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.
Native system adopts diluted phase transport, enter feeding boots 8 material, it is brought in reactor 11 through air conveying, reactor 11 is fluidization reactor, it is provided above atomizer at reactor 11, after required water is atomized shower nozzle atomization quoted from the plant area network of rivers, with the material countercurrent reaction of diluted phase transport, CaO meets water and generates Ca (OH) in the process2。
The material generated continues rising with the wind and reenters pneumatic transport equipment 9, and the final whereabouts of material is decided by the link position of pneumatic transport equipment 9.And the link position of pneumatic transport equipment 9, it is decided by system SO2Content and produce position, fully dispersed by the dispersal device 12 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.
Native system adopts diluted phase transport, enter feeding boots 8 material, it is brought in reactor 11 through air conveying, reactor 11 is fluidization reactor, it is provided above atomizer at reactor 11, after required water is atomized shower nozzle atomization quoted from the plant area network of rivers, with the material countercurrent reaction of diluted phase transport, CaO meets water and generates Ca (OH) in the process2。
The material generated continues rising with the wind and reenters pneumatic transport equipment 9, and the final whereabouts of material is decided by the link position of pneumatic transport equipment 9.And the link position of pneumatic transport equipment 9, it is decided by system SO2Content and produce position, fully dispersed by the dispersal device 12 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, and after cooling, desulfurizing agent enters surge bunker 5 by flap valve 4, and surge bunker 5 inwall sets fire-resistant pouring material, surge bunker divides into push-pull valve 6, metering device 7 divided into by push-pull valve 6, carries out the accurate metering of desulfurizing agent, in the desulfurizing agent feeding reactor 11 after metering, reactor 11 is succinct stirring-type reactor, and in still, desulfurizing agent and shower water reaction generate Ca (OH)2。
Feeding dispersal device 12 after conveying equipment 9 is carried, after fully dispersed, feeding heat exchanger tube and kiln tail wind converging tube carry out desulfurization process.Conveying equipment 9 is the machinery conveying equipments such as elevator.
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. an online kiln exit gas is from the system of desulfurization, 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；
The metering device (7) for measuring raw meal powder consumption being connected with described sub-feed tube (1) raw meal powder discharge end；
Be connected with described metering device (7) discharge end with spray system be used for make raw meal powder generate Ca (OH)2Reactor (11)；
What be connected with described reactor (11) discharge end is used for Ca (OH)2The dispersal device (12) in the exhaust piping of heat exchange pipeline and/or kiln tail is sent into after dispersion；
And, for realizing the induction system of material conveying.
2. according to claim 1 a kind of online kiln exit gas from the system of desulfurization, it is characterized in that, surge bunker (5) it is provided with between described metering device and sub-feed tube, the export pipeline of surge bunker (5) arranges push-pull valve one (6), raw meal powder entrance surge bunker (5) going out sub-feed tube (1) 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.
3. according to claim 2 a kind of online kiln exit gas from the system of desulfurization, it is characterized in that, chiller (3) it is provided with between described surge bunker (5) and sub-feed tube (1), the export pipeline of chiller (3) arranges flap valve (4), go out the raw meal powder of sub-feed tube (1) 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. according to claim 1 a kind of online kiln exit gas from the system of desulfurization, it is characterized in that, described induction system adopts pneumatic conveying mode or machinery mode of movement, according to pneumatic conveying mode, then reactor (11) is fluidization reactor, induction system includes the feeding boots (8) connecing metering device (7) discharge end, feeding boots (8) are arranged on pneumatic transport equipment (9), pneumatic transport equipment (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, another termination reactor (11), and it is ultimately connected to heat exchange pipeline and/or the exhaust piping of kiln tail, its power resources are in the negative pressure of entrance point, dispersal device (12) is arranged on the export pipeline end-position of reactor (11)；According to machinery mode of movement, then reactor (11) is stirring-type reactor, induction system includes the mechanical conveying equipment (9) connecing reactor (11) discharge end, and machinery conveying equipment (9) is by Ca (OH)2Deliver to dispersal device (12).
5. according to claim 1 a kind of online kiln exit gas from the system of desulfurization, 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620080435.6U CN205340559U (en) | 2016-01-27 | 2016-01-27 | System for online kiln tail flue gas is from desulfurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620080435.6U CN205340559U (en) | 2016-01-27 | 2016-01-27 | System for online kiln tail flue gas is from desulfurization |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205340559U true CN205340559U (en) | 2016-06-29 |
Family
ID=56184343
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620080435.6U Active CN205340559U (en) | 2016-01-27 | 2016-01-27 | System for online kiln tail flue gas is from desulfurization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205340559U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105536506A (en) * | 2016-01-27 | 2016-05-04 | 西安建筑科技大学 | Online kiln exit gas self-desulfuration method and system |
| CN114225881A (en) * | 2021-12-14 | 2022-03-25 | 河南汇金智能装备有限公司 | Gas flow reaction kettle in pipeline and desulfurizing device using same |
-
2016
- 2016-01-27 CN CN201620080435.6U patent/CN205340559U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105536506A (en) * | 2016-01-27 | 2016-05-04 | 西安建筑科技大学 | Online kiln exit gas self-desulfuration method and system |
| CN114225881A (en) * | 2021-12-14 | 2022-03-25 | 河南汇金智能装备有限公司 | Gas flow reaction kettle in pipeline and desulfurizing device using same |
| CN114225881B (en) * | 2021-12-14 | 2023-11-10 | 河南汇金智能装备有限公司 | Air flow reaction kettle in pipeline and desulfurizing device using air flow reaction kettle |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101343047B (en) | Improved preparation technique for preparing sulphuric acid and cement with gypsum | |
| CN102502524B (en) | Method for producing sulfur dioxide from calcium sulfate and sulfur | |
| CN204768245U (en) | Flue gas desulfurizing apparatus | |
| CN105536506A (en) | Online kiln exit gas self-desulfuration method and system | |
| CN104587826A (en) | Novel dry-process cement kiln tail flue gas desulfurization system and desulfurization process thereof | |
| CN105771616A (en) | Method and system for on-line removal of SO2 in kiln tail flue gas by using raw material powder | |
| CN109776002B (en) | Suspension calcination activation system and method suitable for clay mine tailings | |
| CN207567121U (en) | A kind of system that desulfurated plaster recycling is carried out using power plant exhaust waste heat | |
| CN205340559U (en) | System for online kiln tail flue gas is from desulfurization | |
| CN207619279U (en) | A kind of system carrying out desulfurization using digestive fever raw material | |
| CN205340557U (en) | System for utilize SO2 in online desorption kiln tail flue gas of raw material powder | |
| CN110052153B (en) | Desulfurizing agent preparation unit based on cement clinker production line calcium cycle | |
| CN110282889B (en) | Cement self-desulfurization device and method | |
| 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 | |
| CN204522733U (en) | A kind of new dry process rotary kiln kiln exit gas desulphurization system | |
| CN110052151B (en) | Calcium-cycle semi-dry desulfurization system based on cement clinker production line | |
| CN106215678B (en) | Cement kiln semi-dry desulfurization system | |
| CN110052152A (en) | One kind being based on cement clinker production line calcium circulation desulfurization system and sulfur removal technology | |
| CN208145761U (en) | A kind of in-furnace calcium spraying dry method desulfuration system | |
| CN208282640U (en) | Exhaust gas processing device | |
| CN105541141A (en) | A device and a method for preparing cement from dry and wet calcium carbide slag | |
| CN205023854U (en) | Gypsum relieving haperacidity thermal technology device | |
| CN211514068U (en) | High-efficient desulfurization system of hot raw material of cement kiln flue gas | |
| CN205087919U (en) | Ardealite, sour coproduction basicity fertilizer production system of potassic feldspar sulfur production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |