CN102913917A - Technology for incinerating volatile organic gases and circulating fluidized bed incinerator utilizing technology - Google Patents
Technology for incinerating volatile organic gases and circulating fluidized bed incinerator utilizing technology Download PDFInfo
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- CN102913917A CN102913917A CN2012104549396A CN201210454939A CN102913917A CN 102913917 A CN102913917 A CN 102913917A CN 2012104549396 A CN2012104549396 A CN 2012104549396A CN 201210454939 A CN201210454939 A CN 201210454939A CN 102913917 A CN102913917 A CN 102913917A
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Abstract
The invention discloses a circulating fluidized bed incinerator of volatile organic gases, based on small aluminum oxidized hollow spheres as bed materials. The invention also provides a technology for incinerating the volatile organic gases by utilizing the circulating fluidized bed incinerator of the volatile organic gases. In the technology, the volatile organic gases enter a hearth from a gas inlet, and are burnt together with auxiliary fuel materials under the effects of the bed materials and a fluidized fan. The circulating fluidized bed incinerator of the volatile organic gases adopts small aluminum oxidized hollow spheres as the bed materials, the critical fluidized air speed of the circulating fluidized bed is lowered, thus the fluidized air quantity is lowered, and the circulating fluidized bed incinerator of the volatile organic gases has an energy-saving effect; and the volatile organic gases are incinerated at the high-temperature condition of 850-950 DEG C, and can achieve the combustion efficiency higher than 99.99%, and the aim of clean incineration and treatment is realized.
Description
Technical field
The present invention relates to a kind of circulating fluidized bed incinerator, relate in particular to a kind of circulating fluidized bed incinerator and burning process thereof that burns volatile organic waste gas that clean.
Background technology
Organic exhaust gas is the common pollutant of the industry dischargings such as petrochemical industry, light industry, plastics, printing, coating, often contain hydrocarbon compound, oxygen-containing organic compound, nitrogenous, sulphur, halogen and organic phosphorus compound etc. in the organic exhaust gas, such as VOCs such as benzene, toluene, styrene, polycyclic aromatic hydrocarbon (VOCs) etc.
Volatile organic waste gas is one of Air Pollutants, and is harmful, and the common symptom that causes is fatigue and weak, dizziness headache, n and V, nervous asthma, blood change etc., and the materials such as aldehyde, amine are foul smelling also.Volatile organic waste gas can also cause photochemical fog, causes secondary pollution.In 25 kinds of gases in the listed toxic gas emission inventory (TRI) of American National Environmental Protection Department (EPA), 18 kinds is organic matter.VOC (VOCs) odorant such as benzene, toluene, styrene, polycyclic aromatic hydrocarbon that mostly contains low concentration in the organic exhaust gas.These worsen people's living environment, but also can work the mischief to health and ecological environment with the gaseous contaminant meeting severe jamming resident's of peculiar smell (smelly or fragrant) daily life.
Along with developing rapidly of Chinese national economy, particularly chemical industry and manufacturing development, the discharge capacity of industrial VOCs constantly increases, and has become at present the one of the main reasons of China key cities (group) and local atmospheric combined pollution.Aspect waste gas pollution control and treatment, after the dedusting that continues, desulphurization and denitration and the Motor Vehicle Emission Control, the pollution control problem of industrial volatile organic waste gas has become the of paramount importance direction of present control air pollution in China.
At present a lot of for the processing method of VOCs, mainly can be divided into heat treating process, Physical, biological degradation method etc.Wherein general with the heat treating process application, it is very wide to the accommodation of VOCs kind and concentration.These class methods mainly are divided into firing method and Production by Catalytic Combustion Process.Ordinary combustion method system is simple, but energy consumption is very large, and the heat accumulating type oxidation is burned and improved the large shortcoming of energy consumption, but still has the higher problem of NOX discharging; The Production by Catalytic Combustion Process development in recent years is very fast, but the catalyst price is higher, requires can not contain the composition that causes catalyst poisoning in the waste gas, and as a kind of low-temperature burning technology, it still is the bottleneck that the restriction catalysis technique is applied that the generation of its dioxin suppresses.
Circulating fluidized bed technique is a kind of clean burning technology, its running temperature is generally at 850～950 ℃, because material concentration is high, gas-solid mixing is strong, and efficiency of combustion is high, pollutant emission is low, be a kind of cleaning incineration technology, adopt CFBC based process VOC, its advantage is not need preliminary treatment, adaptable to gas componant, treatment effeciency is high.Therefore, exploitation has broad application prospects for the circulating fluidized bed incinerator of volatile organic waste gas.
The concentration of VOC is often lower, and that its concentration range is low is 10～1000ppm, and what concentration was high also is no more than 2～3%.Therefore, when adopting high-temperature combustion method to process VOC, VOC is lower to the requirement of combustion air volume.Choosing with 0.528 power of the density of material of the operating air velocity of recirculating fluidized bed is directly proportional, and traditional recirculating fluidized bed selects quartz sand, cinder to expect as bed, and the bulk density of these material is larger, is generally 1100～1300kg/m
3Therefore, cause its critical fluidising air velocity higher, it is higher also to cause moving air quantity, exceeds the required combustion-supporting air quantity of actual after-flame VOC far away, correspondingly the power requirement to fluidized air blower is also high, in addition, these combustion airs are heated to 850 ℃, have also wasted a large amount of energy, cause cost of disposal high, limited its range of application.Therefore, reduce the density of inert bed material, can effectively reduce operating cost.
Summary of the invention
Low for the VOC concentration that produces in the industrial production, require low to burning air capacity, and bed material density is high in the existing circulating fluidized bed incinerator, required fluidising air velocity is large and then cause the large contradiction of air quantity, the invention provides a kind of low circulating fluidized bed incinerator of fluidising air velocity that VOC burns that is suitable for.
A kind of circulating fluidized bed incinerator of VOC comprises:
Burner hearth;
Be positioned at the air compartment of described burner hearth bottom;
Be arranged at the gas access at described burner hearth middle part;
With the separator that described roof of the furnace is communicated with, this separator has top exit and outlet at bottom;
The back-end ductwork that is communicated with described top exit;
Be used for connecting the refeed line of described outlet at bottom and burner hearth;
Be separated with air distribution plate between described burner hearth bottom and the air compartment;
Described air compartment is circumscribed with fluidized air blower by pipeline;
The bottom of described burner hearth is equipped with the bed material, and described bed material is the hollow bead of aluminium oxide.
VOC and assistant coal are sent in the burner hearth respectively to burn, the fluidized wind that fluidized air blower is produced by boasting enters air compartment, then enter burner hearth by air distribution plate, bed material fluidisation is got up, tiny bed material particle is raised suctions, is entrained into and falls into refeed line by centrifugal force, gravity in the separator and send into burner hearth by flue gas, has consisted of the bed material and has circulated.
The circulation of bed material has improved the granule density of combustion space, become a larger heat storage, fully contact with VOC with the air in the burner hearth, mass transfer, carry out heat exchange, make whole furnace cavity temperature evenly, be stabilized in 850～950 ℃, so that the burning of VOC is more abundant.
The fluidisation of bed material directly affects the efficiency of combustion of burner hearth fuel.And fluid mapper process is closely related with bed material and fluidising air velocity, and the density of bed material particle is less, and is lower to the requirement of fluidized wind.Because the operating temperature in the burner hearth is in 850～950 ℃ of scopes in the circulating fluidized bed incinerator, the bed material that therefore adds must have resistant to elevated temperatures performance simultaneously.As preferably, expect to be the hollow bead of aluminium oxide for described; Aluminium oxide has higher fusing point, can bear the high temperature about 2000 ℃, and aluminium oxide is made hollow bead, greatly reduces the density of aluminium oxide, so that corresponding critical fluidising air velocity greatly reduces, has reduced the power requirement to fluidized air blower.
As preferably, the bulk density of the hollow bead of described aluminium oxide is 600～900kg/m
3
Except the bulk density of bed material particle, other physical characteristic parameters such as solid particle size, sphericity and the particle size distribution etc. of bed material are determining also whether recirculating fluidized bed can efficient, trouble-free operation.
Bed material particle diameter is excessive, normal primary air flow can't blow afloat the bed material, large particle diameter bed material a large amount of after the long-time running will be deposited on a material layer lower part, affect the fluidisation of the whole bed bed of material, making becomes dead bed in the burner hearth, and bed temperature may appear, a bed end finger shows unusually, the incinerator parameter can't be kept, can form coking when serious, as can not in time reversing, be easy to cause that final fluidisation is undesired is forced to blowing out; Bed material particle diameter is meticulous, will cause separator to reduce, and can't form Matter Transfer, reduces the bed material concentration of combustion space.Therefore, as preferably, the particle diameter of the hollow bead of described aluminium oxide is 1～5mm.
The present invention also provides the technique of utilizing described recirculating fluidized bed VOC incinerator to burn VOC, and described VOC enters burner hearth from the gas access, jointly burns with auxiliary fuel under the effect of bed material and fluidized air blower.
As preferably, the temperature range in the described burner hearth is 850～950 ℃.
After VOC is admitted to burner hearth, because adopting the hollow bead of aluminium oxide expects as bed, required fluidising air velocity is lower, so VOC can reach about 3s the burning time in burner hearth, discharges through entering back-end ductwork by separator behind the clean burning of about 3s.Recirculating fluidized bed can conveniently be realized maximizing, and the treating capacity of described VOC can adapt to 100～10000m
3The burning disposal requirement of/h.
Compared with prior art, the present invention has following beneficial effect:
The present invention adopts recirculating fluidized bed to come the burning disposal VOC, can make VOC lower time of staying of burning condition of 850～950 ℃ in recirculating fluidized bed guarantee its firing efficiency greater than 3 seconds.The present invention adopts the hollow bead of aluminium oxide to expect as bed, the bulk specific weight of the hollow bead of aluminium oxide is little, therefore it is little to make a critical fluidising air velocity of the recirculating fluidized bed of material with the hollow bead of aluminium oxide, reach the recirculating fluidized bed of identical fluid effect, its air quantity is 2/3 of traditional recirculating fluidized bed approximately, therefore can reduce significantly the fluidisation air quantity.Because fluidising air velocity is low, its furnace height also can be lower by 20% than the height of the recirculating fluidized bed that uses conventional bed material, reduced manufacturing cost.
Recirculating fluidized bed VOC incinerator of the present invention adopts the hollow bead of aluminium oxide to expect as bed, when burning VOC, reduction along with critical fluidising air velocity, the fluidisation air quantity reduces thereupon, the power consumption that also means fluidized air blower reduces, therefore can when cleaning is burned, can reduce better operating cost.
Recirculating fluidized bed VOC incinerator of the present invention adopts the hollow bead of aluminium oxide to expect as bed, and the fluidisation air quantity is reduced, and the heat loss due to exhaust gas of corresponding incinerator also reduces, and has energy-conservation effect.
Description of drawings
Fig. 1 is the structural representation of recirculating fluidized bed VOC incinerator of the present invention.
The specific embodiment
Below in conjunction with accompanying drawing 1, structure and the running of recirculating fluidized bed VOC incinerator of the present invention is further described.
As shown in Figure 1, recirculating fluidized bed VOC incinerator of the present invention, comprise: burner hearth 1, the air compartment 2 that is positioned at burner hearth 1 bottom, the gas access 9 that is arranged at described burner hearth middle part, the separator 4 that is communicated with burner hearth 1 top, this separator 4 have top exit and outlet at bottom, with the back-end ductwork 6 of top exit connection, for be separated with air distribution plate 3 between the refeed line 5, burner hearth bottom and the air compartment that are connected outlet at bottom and burner hearth, air compartment 2 is circumscribed with fluidized air blower 7 by pipeline.
It is the hollow bead 8 of aluminium oxide of 400mm that a layer thickness is laid in the bottom of burner hearth 1, and the particle diameter of the hollow bead of this aluminium oxide is about 3mm.This circulating fluidized bed incinerator also is provided with the back-end ductwork 6 with separator 4 upper end UNICOMs, and the flue gas that produces in the combustion process is discharged from this back-end ductwork; Fluidized air blower 7 is used for providing fluidized wind to air compartment 2, and then with the bed material fluidisation in the burner hearth 1.
Select the hollow bead of aluminium oxide to expect as bed, because the hollow bead bulk specific weight of aluminium oxide is little, therefore the critical fluidising air velocity of required circulating fluidized bed incinerator is little, means that also the power consumption of fluidized air blower reduces.The critical flow wind transmission speed ratio regular circulation fluid bed of this recirculating fluidized bed low 30%.
During the operation of this circulating fluidized bed incinerator, the hollow bead 8 of aluminium oxide is added into first burner hearth 1, VOC and assistant coal are sent into the burner hearth 1 from gas access 9 and fuel inlet respectively, the fluidized wind that fluidized air blower 7 is produced by boasting enters air compartment 2, then enter burner hearth 1 by air distribution plate 3, hollow bead 8 fluidisations of aluminium oxide are got up, the hollow bead of aluminium oxide is brought into burner hearth 1 middle and upper part heat exchange by a wind, the hollow bead of aluminium oxide 8 is raised suction by flue gas, be entrained in the separator 4 and pass through centrifugal force, gravity falls into refeed line 5 and loops back into burner hearth 1, and the time of staying of VOC in about 900 ± 20 ℃ burner hearth of temperature was above 3 seconds, discharge by back-end ductwork 6 through separator 4 behind the clean burning, assistant coal burns the flue gas that produces and also discharges by back-end ductwork 6.
The hollow bead 8 of aluminium oxide plays the effect of circulation fluidized bed material, and the hollow bead 8 of the oxidized aluminium of fuel combustion liberated heat absorbs, and guarantees that temperature stabilization is about 900 ℃ in the burner hearth.The hollow bead of aluminium oxide by the centrifugation of separator 4, can be taken back burner hearth 1 to the heat that produces after blowing out burner hearth 1, guarantee that burner hearth 1 temperature is even.
Above embodiment is only in order to technical scheme of the present invention to be described but not limit it; in the situation that does not deviate from spirit of the present invention and essence thereof; those of ordinary skill in the art work as can make according to the present invention various corresponding changes and distortion, but these corresponding changes and distortion all should belong to the protection domain of the appended claim of the present invention.
Claims (6)
1. the circulating fluidized bed incinerator of a VOC comprises:
Burner hearth;
Be positioned at the air compartment of described burner hearth bottom;
Be arranged at the gas access at described burner hearth middle part;
With the separator that described roof of the furnace is communicated with, this separator has top exit and outlet at bottom;
The back-end ductwork that is communicated with described top exit;
Be used for connecting the refeed line of described outlet at bottom and burner hearth;
Be separated with air distribution plate between described burner hearth bottom and the air compartment;
Described air compartment is circumscribed with fluidized air blower by pipeline;
It is characterized in that the bottom of described burner hearth is equipped with the bed material, described bed material is the hollow bead of aluminium oxide.
2. the circulating fluidized bed incinerator of VOC as claimed in claim 1 is characterized in that, the bulk density of the hollow bead of described aluminium oxide is 600～900kg/m
3
3. the circulating fluidized bed incinerator of VOC as claimed in claim 1 is characterized in that, the particle diameter of the hollow bead of described aluminium oxide is 1～5mm.
4. utilize the technique of the circulating fluidized bed incinerator burning VOC of each described VOC in the claim 1～3, it is characterized in that, described VOC enters burner hearth from the gas access, jointly burns with auxiliary fuel under the effect of bed material and fluidized air blower.
5. the technique of burning VOC as claimed in claim 4 is characterized in that, the temperature range in the described burner hearth is 850～950 ℃.
6. the technique of burning VOC as claimed in claim 4 is characterized in that, the treating capacity scope of described VOC is 100～10000m
3/ h.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012104549396A CN102913917A (en) | 2012-11-13 | 2012-11-13 | Technology for incinerating volatile organic gases and circulating fluidized bed incinerator utilizing technology |
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| CN2012104549396A CN102913917A (en) | 2012-11-13 | 2012-11-13 | Technology for incinerating volatile organic gases and circulating fluidized bed incinerator utilizing technology |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2791491Y (en) * | 2005-01-14 | 2006-06-28 | 浙江大学 | Medical refuse circulating fluidized bed incinerator |
| CN102728181A (en) * | 2012-07-23 | 2012-10-17 | 东南大学 | Fluidized bed jetting adsorbent smoke demercuration device and method thereof |
| CN202973118U (en) * | 2012-11-13 | 2013-06-05 | 浙江大学 | Circulating fluidized bed incinerator for volatile organic gas |
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2012
- 2012-11-13 CN CN2012104549396A patent/CN102913917A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2791491Y (en) * | 2005-01-14 | 2006-06-28 | 浙江大学 | Medical refuse circulating fluidized bed incinerator |
| CN102728181A (en) * | 2012-07-23 | 2012-10-17 | 东南大学 | Fluidized bed jetting adsorbent smoke demercuration device and method thereof |
| CN202973118U (en) * | 2012-11-13 | 2013-06-05 | 浙江大学 | Circulating fluidized bed incinerator for volatile organic gas |
Non-Patent Citations (2)
| Title |
|---|
| 王同章等: "气体流化床中传热的研究", 《江苏工学院学报》 * |
| 贾海龙: "有机废气流化床焚烧处理试验研究", 《中国学位论文全文数据库》 * |
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Application publication date: 20130206 |