CN109000221A - A kind of coal slime processing method - Google Patents
A kind of coal slime processing method Download PDFInfo
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- CN109000221A CN109000221A CN201810778768.XA CN201810778768A CN109000221A CN 109000221 A CN109000221 A CN 109000221A CN 201810778768 A CN201810778768 A CN 201810778768A CN 109000221 A CN109000221 A CN 109000221A
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- Prior art keywords
- coal slime
- temperature adjustment
- processing method
- media particles
- slime processing
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/24—Devices for removal of material from the bed
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention discloses a kind of coal slime processing methods, the treating method comprises following content: coal slime enters reactor, it is contacted with the temperature adjustment media particles in reactor, it is reacted under the action of fluidized wind, flue gas after reaction carries out separating treatment, Returning reactor, coal slime and temperature adjustment media particles the abrasion fine powder of smaller particle carry out subsequent processing with flue gas in the form of flying dust to the bulky grain temperature adjustment media particles taken out of by flue gas after separation.Coal slime processing method of the present invention, by using temperature adjustment media particles in reactor, stable coal slime oxidizing temperature is provided, coal slime minimizing, harmless treatment and efficient resource can be achieved to utilize, oxidation capable of being carried out as raw material using pure coal slime and burning recycling heat, coal slime oxidation efficiency and the device thermal efficiency are higher.
Description
Technical field
The present invention relates to coal slime harmless treatment and resource utilization fields, and in particular to a kind of pure coal slime processing method.
Background technique
Coal slime is the by-product of coal washing process, since with fine size, moisture is high, the spy that ash content is big and stickiness is high
Point brings biggish difficulty to its comprehensive utilization.Due to lacking effective utilization technology, many coal mines accumulate coal slime discarded.
If coal slime is stored up for a long time, a large amount of soils are not only taken up, and pollute environment.Coal slime particle is thin, and dehydration is difficult, drying and other treatment
Afterwards, it flies upward all over the sky to the wind, meet rainwater and trickle everywhere, it is very big to the influences on environmental ecosystem.Coal slime has certain calorific value, some are low
The calorific value of ash content coal slime is even higher than some low heat value thermal coals, and the existing extensive processing mode of coal slime causes great energy wave
Take, with the rapid development of coal washing industry, the slime content that China is discharged every year also rapid growth therewith, therefore, coal slime
Harmless treatment and resource utilization are extremely urgent；
Coal slime replaces coal-fired as boiler oil and carries out burning using the best method for being current processing coal slime.Due to high-content
Moisture and ash content and lower calorific value, coal slime are not suitable for traditional coal-powder boiler burning.The low heat value coal utilization of resources is main
Using circulating fluidized bed boiler, coal slime is widely used in circulating fluidized bed combustion.But current slime circulating fluidized bed boiler is deposited
In following problems: (1) pure coal combustion calorific value is low, low efficiency, generally requires and mixes burning with high heating value coal, realizes stable operation；
(2) coal slime ash content is big, and partial size is small, and simple coal combustion, flying dust amount is big, and circulating ash quantity is insufficient, needs to mix burning fat coal, maintains
Circulating fluidization；(3) coal slime water content is high, and moisture is not easy to control, easily forms clod, feeds at present frequently with upper furnace, by
In coal slime to access point close to furnace outlet, thus there are a large amount of coal slimes be directly fluidized in the case where no after-flame wind go out
Burner hearth, into separator, and coal slime granularity is small, and separator is captured less than becoming flying dust, lead to the coal slime residence time not
Foot burns insufficient, and efficiency of combustion is low；(4) for circulating fluidized bed boiler, bed endoparticle is run after a period of time, and thick
Grain sinks to emulsion zone, and fine grained becomes flying dust, and the particle of only certain particle size range becomes stable circulating ash, for stable bed
Storage needs regular deslagging.General bottom deslagging share accounts for 30% or more total ash, and coal slime ash content is big in addition, causes q6(lime-ash
Physics heat loss) heat loss, reduce boiler thermal efficiency；
107355780 A of patent CN discloses a kind of internal circulating fluidized-bed boiler of multiple hearth structure, designs multiple burner hearths, adopts
The inner circulation fluidized bed system of the compositions such as the ladder height difference with high speed bed and low speed bed formation, can enhanced fuel empir-ical formulation,
Mixing more evenly, can satisfy the combustion requirements of different fuel, guarantee that boiler bed temperature is stablized, fuel tolerance is wide, environmental benefit
Significantly, high combustion efficiency, but the big bed of boiler is divided into more by the invention, increases wear area, and for pure coal slime
Little particle fuel is difficult to realize multithread field, multi-direction mixing and circulating effect in burner hearth.102537943 A of patent CN is disclosed
A kind of Horizontal CFB Boiler, is capable of handling the inferior fuels such as colm, solid waste, sludge or biomass, but
The invention is suitable only for the fuel combustion few containing ash content, bad for high-ash coal slime treatment effect；
In conclusion being developed at advanced coal slime for the features such as coal slime calorific value is low, ash content is big, partial size is small, moisture is not easy to control
Reason technology realizes coal slime minimizing, harmless treatment and high efficiency, resource utilization, raw for the safe green of coal enterprise
It produces and energy-saving is of great significance.
Summary of the invention
For need to mix burning fat coal and efficiency of combustion in existing coal slime processing method, the thermal efficiency is lower the problems such as, this
Invention provides a kind of coal slime processing method, can by, using temperature adjustment medium, providing stable coal slime oxidizing temperature in reactor
Realize that coal slime minimizing, harmless treatment and efficient resource utilize.Compared with prior art, coal slime processing method of the present invention
Without mixing burning fat coal, oxidation can be carried out as raw material using pure coal slime and burn recycling heat, and stable, coal slime oxidation efficiency
High, device thermal efficiency height.
The present invention provides a kind of coal slime processing method, the treating method comprises following content:
(1) coal slime enters reactor, contacts with the temperature adjustment media particles in the temperature adjustment medium bed in reactor, in fluidized wind
Effect is lower to carry out oxidation reaction；
(2) flue gas in step (1) after coal slime oxidizing fire carries out separating treatment, the bulky grain temperature adjustment medium taken out of by flue gas
Grain Returning reactor after separation, coal slime and temperature adjustment media particles the abrasion fine powder of smaller particle in the form of flying dust with flue gas into
Row subsequent processing.
In coal slime processing method of the present invention, coal slime described in step (1) is carried out dehydrating first, the coal after dehydration
Mud water content is generally no greater than 20wt%, preferably no greater than 15wt%.The dehydration can use in the prior art can be real
One or more of existing coal slime dewatering method, such as one or more of mechanical dehydration, gravity dehydration and thermal energy drying and dehydrating,
It is preferred that, further preferably using first mechanical dehydration, reheating can dry combination side using mechanical dehydration and the dry combination of thermal energy
Formula.Wherein, the mechanical dehydration can use filter press, band press, disk vacuum filter, belt vacuum filter, folding
It is realized with one or more of vacuum filter.The thermal energy drying mode can be external-heat or direct contact type, heat
Source can be flue gas or steam, preferably using self-produced steam as the outer heated drying mode of heat source.
In coal slime processing method of the present invention, the temperature adjustment medium bed of material described in step (1) is made of temperature adjustment media particles, temperature adjustment
Media particles can be by silica, titanium oxide, aluminium oxide, lithia, diatomite, feldspar, quartz, cordierite, mullite etc.
One or more of be made.0.5 ~ 10mm of particle size range of the temperature adjustment media particles, preferably 1 ~ 6mm, the temperature adjustment matchmaker
Jie's particle shape can be one or more of shapes such as spherical shape, sheet, bulk, jujube shape, cylindrical body, can be solid, empty
The heart, surface fluting or internal with cellular structure.1500 ~ 3000 kg/m of bulk density of temperature adjustment media particles3, accumulate close
Spend 700 ~ 2000 kg/m3.The temperature adjustment media particles have big thermal capacity, high thermal conductivity coefficient, high abrasion, anti-oxidant, anti-corruption
Erosion, the properties such as thermal expansion coefficient is small.Thermal capacity the > 1300 J/kg k, 2.6 w/m of thermal coefficient > of the temperature adjustment media particles
▪k。
In coal slime processing method of the present invention, the temperature adjustment medium bed of material described in step (1) includes two or more different-grain diameters
Temperature adjustment media particles preferably include the temperature adjustment media particles of three kinds of different-grain diameters.When the temperature adjustment medium including two kinds of different-grain diameters
When particle, one of temperature adjustment media particles partial size is 1 ~ 2mm, and another temperature adjustment media particles partial size is 4 ~ 5mm；When including three
When the temperature adjustment media particles of kind different-grain diameter, the partial size of three kinds of temperature adjustment media particles is respectively 0.5 ~ 1mm, 2 ~ 3mm, 4 ~ 6mm.
In coal slime processing method of the present invention, temperature adjustment media particles described in step (1) can with can according to actual needs into
The corresponding special modification of row or pretreatment, realize in-furnace desulfurization, denitration effect.
In coal slime processing method of the present invention, reaction temperature described in step (1) is 800 ~ 950 DEG C, 2 ~ 8 m/ of fluidizing velocity
S, 5 ~ 15 kPa of bed pressure drop.
In coal slime processing method of the present invention, total blast volume needed for reaction described in step (1) is required for practical coal combustion
Theoretical air requirement and excess air coefficient between check value, 1.05 ~ 1.2 times in theoretical oxidation air amount of general control.Institute
It states total wind and generally includes First air and Secondary Air, wherein primary air flow accounts for 40% ~ 60%(v/v of total blast volume).Fluidisation in reactor
Wind and oxidation wind are provided by First air, Secondary Air.
In coal slime processing method of the present invention, flue gas post-processing obtained in step (2) generally enters flue and is arranged in
Heat exchange equipment progress heat exchange in flue, recovered flue gas thermal energy, then after the purified treatments such as dedusting, desulphurization and denitration, row up to standard
It puts.The heat exchange equipment can be one or more of superheater, economizer and air preheater etc., the superheater, province
Coal device and air preheater are disposed in flue according to flow of flue gas direction.The purified treatments such as the dedusting, desulphurization and denitration
Can using this field it is existing can be realized dedusting, one or more of the method for desulphurization and denitration realizes that meeting gas reaches
Emission request is marked, it is easy for selecting suitable processing technique to those skilled in the art.Overheat noted earlier
The heat recoveries facility such as device, economizer and air preheater is conventional boiler carbonated drink and heat exchange design, and the present invention is no longer to these
Device structure is repeated with design.
In coal slime processing method of the present invention, step (2) described separation can carry out in the separator, and the separator is rotation
Wind separator or inertia separator, preferably cyclone separator, specific structure are long centrum, in cylinder, diffusion type, bypass type
It is one or more of.When the separator is cyclone separator, incising control dpIt is 20 μm -100 μm, specific incising control is by storing
Thermal medium granulometric range determines, controls dpLess than the smallest particles degree of heat storage medium particle, it is ensured that heat storage medium particle is by returning
Glassware Returning reactor carries out outer circulation.
In coal slime processing method of the present invention, reactor described in step (1) can be existing ciculation fluidized using this field
Bed reactor, it is preferred to use the circulating fluid bed reactor having the following structure, the reactor include air compartment, reaction chamber, divide
From device, material-returning device and steam generation facility, the steam generation facility includes drum and water-cooling wall, and drum is set to outside reactor
Top, water-cooling wall are set to reactor wall, and the reaction chamber is divided into heat-accumulation combustion area, soaking zoneofoxidation and separation from the bottom to top and returns
Confounding；Air distribution plate is equipped between the air compartment and heat-accumulation combustion area, the air compartment bottom is provided with First air entrance, the accumulation of heat
The temperature adjustment medium bed of material is equipped in combustion zone, separation back-mixing area is connected to through pipeline with separator inlet, the separator bottom outlet
It is connected to through refeed line with material-returning device one end, the material-returning device other end is connected to through pipeline with the return port in heat-accumulation combustion area.
In the circulating fluid bed reactor, the heat-accumulation combustion area of the reaction chamber is variable-diameter structure, the equal thermal oxide
Area is equal gauge structures, and the lower part in the separation back-mixing area is variable-diameter structure, and top is to wait gauge structures, wherein separation back-mixing area lower part
The outer wall of variable-diameter structure and the angle α of horizontal plane are not less than the angle of repose of handled material.
In the circulating fluid bed reactor, heat-accumulation combustion area minimum sectional area is S1, soaking zoneofoxidation sectional area
For S2, separation back-mixing area maximum secting area is S3, and the ratio of S1:S2:S3 is 1:3/2 ~ 3:2 ~ 5, preferably 2:3:4.
In the circulating fluid bed reactor, the volume of the temperature adjustment medium bed of material is heat-accumulation combustion area in the heat-accumulation combustion area
The 1/3 ~ 2/3 of volume.
In the circulating fluid bed reactor, the indoor heat-accumulation combustion area of the reaction, soaking zoneofoxidation and separation are returned
The fluidising air velocity of confounding is controlled respectively in 4 ~ 8m/s, 3 ~ 6m/s, 2 ~ 4m/s.
In the circulating fluid bed reactor, the heat-accumulation combustion area and soaking zoneofoxidation intersection setting Secondary Air enter
Mouthful, the following are heat-accumulation combustion areas for Secondary Air entrance.
In the circulating fluid bed reactor, the Secondary Air entrance top is additionally provided with device in Gas entrance, passes through setting
Device in Gas entrance may be implemented to handle low concentration gas simultaneously.
In the circulating fluid bed reactor, the material-returning device can be automatic adjustment material-returning device or valve-type returning charge
Device.
In the circulating fluid bed reactor, the temperature adjustment medium bed of material is made of temperature adjustment media particles, the temperature adjustment matchmaker
Jie's particle can be by silica, titanium oxide, aluminium oxide, lithia, diatomite, feldspar, quartz, cordierite, mullite etc.
One or more be made.Particle size range 0.5 ~ 10 mm, the preferably 1 ~ 6mm of the temperature adjustment media particles, the temperature adjustment medium
Particle shape can be one or more of shapes such as spherical shape, sheet, bulk, jujube shape, cylindrical body, can be it is solid, hollow,
Surface fluting is internal with cellular structure.1500 ~ 3000 kg/m of bulk density of temperature adjustment media particles3, bulk density
700~2000 kg/m3.The temperature adjustment media particles have big thermal capacity, high thermal conductivity coefficient, high abrasion, it is anti-oxidant, anticorrosive,
The properties such as thermal expansion coefficient is small.The 2.6 w/m k of thermal capacity > 1300 J/kg k, thermal coefficient > of the temperature adjustment media particles.
In the circulating fluid bed reactor, the temperature adjustment medium bed of material includes the temperature adjustment medium of two or more different-grain diameters
Particle preferably includes the temperature adjustment media particles of three kinds of different-grain diameters.When including the temperature adjustment media particles of two kinds of different-grain diameters,
A kind of middle temperature adjustment media particles partial size is 1 ~ 2mm, and another temperature adjustment media particles partial size is 4 ~ 5mm；When including three kinds of different grains
When the temperature adjustment media particles of diameter, the partial size of three kinds of temperature adjustment media particles is respectively 0.5 ~ 1mm, 2 ~ 3mm, 4 ~ 6mm.
In the circulating fluid bed reactor, the reaction chamber section can be arbitrary shape, such as rectangular, round, polygon
Deng preferably circular.
In the circulating fluid bed reactor, baffle plate, the baffle plate are set in the separation back-mixing area of the reaction chamber
One layer of setting or more, lowest level arrangement of baffles is in the separation above space of back-mixing area reducer, when two layers of setting or more baffle plate
When, adjacent two layers baffle plate interlaced arrangement.The baffle plate can make the material movement direction moved upwards with flue gas occur one
Secondary or multiple deflection, deflection angle are close to or higher than 180 °, to realize the inertial separation of different-grain diameter particle, baffle plate can be with
For one of board-type, inclined plate type, groove profile, inverted V type or a variety of, preferably inverted V type baffle plate.
In the circulating fluid bed reactor, the separator can be cyclone separator and/or inertia separator, preferably
For cyclone separator.The incising control dp of the separator is not more than 100 μm, and specific incising control is by temperature adjustment medium particle size range
It determines, control dp is less than the smallest particles degree of temperature adjustment media particles, it is ensured that temperature adjustment media particles are returned by material-returning device reacts
Room heat-accumulation combustion area is recycled.One or more can be set according to reactor granules load is taken out of in the separator, setting
When more than two separators, separator can connect in parallel or series.
In the circulating fluid bed reactor, the separator, refeed line and material-returning device be can be set in reaction chamber
Outside portion or reaction chamber.
In the circulating fluid bed reactor, the reactor is equipped with feed inlet, and the feed inlet can be arranged directly on
On heat-accumulation combustion area side wall, also it can be set on the pipeline that material-returning device is connected to heat-accumulation combustion area.
In the circulating fluid bed reactor, the interior heat collecting device is set in reaction chamber separation back-mixing area, further excellent
Choosing is set to separation back-mixing area inner top.
In the circulating fluid bed reactor, drum is arranged in the outer top of the reaction chamber, and drum and reactor wall are laid
Water-cooling wall be connected.Water in water-cooling wall is heated after generation hot water and steam into drum, after drum effect in reaction chamber
Steam can be used for industrial production or domestic life, and the water in drum continuously recycles supply water-cooling wall.
In the circulating fluid bed reactor, heat-accumulation combustion area bottom is also provided with slag-drip opening.
A kind of regenerative oxidation formula coal slime processing method of the present invention, the steam of generation can be used for coal slime mining area certainly
With as coal slime drying, mining area summer underground high-temperature mine and office air-conditioning, winter equipment and office heating and employee are washed
The lives such as bath heat, it can also be used to generate electricity.
A kind of regenerative oxidation formula coal slime processing method of the present invention, not only can handle low heat value coal slime, for it
His form low heat value inferior fuel, such as dirty coal, sulphur coal, high-sulfur dirty coal, hydrogenous coal, gangue, it is equally applicable, and
It can be realized and mix burning harmless treatment with wastes such as stalk, sludge, municipal refuses.
Compared with prior art, coal slime processing method of the present invention has the advantages that
1, coal slime processing method of the present invention may not need by using temperature adjustment media particles mixes burning high-quality coal, with pure coal slime
For raw material, cooperate temperature adjustment media particles, form fluidization in reactor and carry out oxidizing fire, realizes stablizing and filling for coal slime
Divide oxidation, entire processing unit thermal stability is good, and load regulation range is big；
2, in the method for the present invention, the temperature adjustment media particles that use have big thermal capacity, high thermal conductivity coefficient, high abrasion, anti-oxidant, anti-
The properties such as burn into thermal expansion coefficient is small, are used by Cut size, under certain wind speed, can preferably be realized in reactor
Coal slime particle, temperature adjustment media particles are between fluidized particles and surface between hot wall face is taken quickly to update, and realize that homogenizing efficiently passes
Heat, oxidizing intensity are high；
3, in coal slime processing method of the present invention, since coal slime particle is smaller (average grain diameter is only 70 μm or so), by making
With temperature adjustment media particles, flying dust share af → 1 may be implemented, and bed drain purge → 0, it is not necessarily to lag cooler, not only reactor q6 → 0,
And it can be improved Matter Transfer multiplying power；
4, in coal slime processing method of the present invention, coal slime oxidation efficiency is improved, and can reduce solid-unburning hot loss q4,
And due to the method for the present invention bottom bed drain purge → 0, so that lime-ash ermal physics lose q6 → 0, heat loss is substantially reduced, and cooperation is anti-
Excessive oxidation air control system extremely low in device is answered, the existing circulating fluidized bed boiler of reactor entirety thermal efficiency ratio improves 5% or more；
5, the reaction chamber of circulating fluid bed reactor of the present invention is divided into heat-accumulation combustion area, soaking zoneofoxidation and separation back-mixing
Variable-diameter structure is arranged in area, the heat-accumulation combustion area and separation back-mixing area, and matches and temperature adjustment medium material is arranged in heat-accumulation combustion area
Layer, can be realized in reaction chamber different-grain diameter temperature adjustment media particles back-mixing and interior circulation, it is realization multizone, multithread field, more
The material movement state of circulation, when for passing through the accumulation of heat of temperature adjustment media particles when handling big ash content, fine grain coal slime raw material
The stabilization, fully oxidized of big ash content, fine grained raw material is realized in burning and equal thermal oxidation, and thermal stability is good, Load Regulation model
It encloses greatly, without adding the high-quality coal slime raw material of other bulky grains, the pure fine grain coal slime raw material of burning may be implemented；
6, it can be better achieved in circulating fluid bed reactor of the present invention by using the temperature adjustment media particles of different-grain diameter
Coal slime material particles and temperature adjustment media particles surface and its with the quick update that takes hot wall contact surface, oxidizing intensity is high, heat transfer effect
Rate is high, and the Thermal load of cross-section of heat-accumulation combustion area and soaking zoneofoxidation is up to 6MW/m2More than；
7, circulating fluid bed reactor separation of the present invention back-mixing area is variable-diameter structure, considerably increases material in reaction chamber
Residence time, keep material fully oxidized, than conventional fluidization bed boiler burning rate improve 5% or more.Further in separation back-mixing area
Inside setting baffle plate, makes the direction of motion of material that one or many deflections occur, further increases the residence time of material,
Material particles crude separation in separation back-mixing area is realized, the processing load of rear end separator is reduced；
8, the height ratio of circulating fluid bed reactor reaction chamber of the present invention can be reduced with the existing circulating fluidized bed boiler of scale
20% or more, device steel consumption is saved, cost is significantly reduced.
Detailed description of the invention
Fig. 1 is circulating fluid bed reactor structural schematic diagram of the present invention.
In figure, 1- reaction chamber, 2- separator, 3- refeed line, 4- material-returning device, 5- interior heat collecting device, 6- drum, 7- air compartment,
8- air distribution plate, 11- First air entrance, 12- Secondary Air entrance, 13- device in Gas entrance, 14- feed inlet, 15- separator outlet,
16- slag-drip opening, 17- return port, 18- baffle plate, A- heat-accumulation combustion area, B- soaking zoneofoxidation, C- separate back-mixing area.
Specific embodiment
Illustrate to further illustrate concrete condition of the invention with specific embodiment with reference to the accompanying drawing, but is not limited to following
Embodiment.
In the description of the present invention, it should be noted that term " on ", "lower", "inner", "outside", "top", "bottom" etc. refer to
The orientation or positional relationship shown is to be based on the orientation or positional relationship shown in the drawings, and is merely for convenience of the description present invention and simplifies
Description, rather than the device or element of indication or suggestion meaning must have a particular orientation, constructed and grasped with specific orientation
Make, therefore is not considered as limiting the invention.In addition, term " first ", " second " are used for description purposes only, and cannot manage
Solution is indication or suggestion relative importance.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " being equipped with " " is set
In ", " connected ", " connection ", " installation " etc. shall be understood in a broad sense, for example, it may be being fixedly connected, be also possible to detachably connect
It connects, or is integrally connected；It can be mechanical connection, be also possible to be electrically connected；It can be directly connected, intermediate matchmaker can also be passed through
Jie is indirectly connected, and can be the connection inside two elements.It for the ordinary skill in the art, can be with concrete condition
Understand the concrete meaning of above-mentioned term in the present invention.
As shown in Figure 1, the present invention provides a kind of circulating fluid bed reactor, including reaction chamber 1, separator 2, material-returning device
4, air compartment 7, drum 6 and water-cooling wall, drum 6 are set to the outer top of reactor, and water-cooling wall is laid in reactor wall (water in Fig. 1
Cold wall is not drawn into, and is those skilled in the art's common knowledge)；The reaction chamber 1 is divided into heat-accumulation combustion area A, equal thermal oxide from the bottom to top
Area B and separation back-mixing area C；Air distribution plate 8,7 bottom of air compartment are equipped between the air compartment 7 and the heat-accumulation combustion area A of reaction chamber
It is provided with First air entrance 11, the temperature adjustment medium bed of material is provided in the heat-accumulation combustion area A, the temperature adjustment medium bed of material is by temperature adjustment
Media particles are constituted, and slag-drip opening 16, heat-accumulation combustion area A and the setting of soaking zoneofoxidation B intersection is arranged in bottom in heat-accumulation combustion area A
Secondary Air entrance 12, Secondary Air entrance are provided with device in Gas entrance on the side wall of soaking zoneofoxidation B the following are heat-accumulation combustion area A
13, device in Gas entrance 13 is located at 12 top of Secondary Air entrance, is provided with baffle plate 18 above separation back-mixing area C reducer, separates
Back-mixing area C inner top is provided with interior heat collecting device 5, and shown interior heat collecting device 5 can be superheater, and separation back-mixing area C is through pipeline and divides
It is connected to from 2 entrance of device, 2 outlet at bottom of separator is connected to through refeed line 3 with 4 one end of material-returning device, and the material-returning device 4 is another
One end is connected to through pipeline with heat-accumulation combustion area A return port 17, and material outlet 15 is equipped at the top of separator 2.The feed inlet 14 is straight
It connects and is arranged on heat-accumulation combustion area A side wall, or the returning charge that material-returning device 4 is connected to the heat-accumulation combustion area A of reaction chamber 1 is set
On pipe 3.Feed inlet 14 and return port 17 are lower than overfiren air port 12, and device in Gas entrance 13 is slightly above overfiren air port 12.
The present invention provides a kind of coal slime processing method, handles coal slime using above-mentioned circulating fluid bed reactor, coal slime is first
It is carried out dehydrating, coal slime that treated enters the heat-accumulation combustion area of reactor from circulating fluid bed reactor bottom, with temperature adjustment
Media particles contact, and it is in fluidized state under fluidized wind effect, coal slime is aoxidized with the air in fluidized wind simultaneously
Combustion reaction, First air that fluidized wind is introduced by reactor bottom, Secondary Air provide, and aoxidize the heat recovery of generation for producing
The mixed material part of steam, coal slime and temperature adjustment media particles circulation in reactor carries out, partially enters separator with flue gas,
Enter the material of separator with flue gas, larger particles are through (being greater than separator incising control dpParticle) by separator separation simultaneously
It after trapping, is formed and is recycled through material-returning device Returning reactor, smaller particle (is less than separator incising control dpParticle, mainly
It is the ash content after coal slime oxidation) in the form of flying dust enter flue below with flue gas, after flue gas enters flue, and it is arranged in flue
Superheater, economizer and air preheater carry out heat exchange, recovered flue gas thermal energy, then through dedusting, desulphurization and denitration gas purification
After cell processing, qualified discharge is realized.
Embodiment 1
Certain mining area slime initial aqueous 70wt% or so, coal slime Industrial Analysis and Elemental analysis data are as follows:
1 coal slime master data of table
| War | Aar | Var | Car | Har | Oar | Nar | Sar | Qnet.ar |
| % | % | % | % | % | % | % | % | MJ/kg |
| 15 | 48.71 | 17.65 | 25.38 | 2.07 | 8.00 | 0.61 | 0.23 | 9700 |
Operating condition and treatment effect in treatment process is as follows:
Temperature adjustment medium preparation process in the present embodiment 1 is as follows:
1) premium high-alumina alumina is taken, alumine main component is as follows: Al2O3=71.22%、SiO2=22.53%、Fe2O3=
2.48%、TiO2=0.58%、CaO=0.7%、MgO=1.06%、K2O=0.61%、Na2Alumine is broken into powder, mesh by O=0.82%
Number 200；Taking purity is 99% industrial alumina powder, mesh number 800；
2) above-mentioned alumine powder and industrial alumina powder 2:1 in mass ratio are mixed and stirred for uniformly, while with water mist spray
The adhesive of mixed material gross mass 10% is added in mode, and adhesive is the polyvinyl alcohol and mass fraction 10% of mass fraction 10%
The aqueous solution of water soluble acrylic acid；
3) by above-mentioned material squeeze, cohere, and further using pan-pelletizer be rolled onto partial size 0.5mm ~ 1mm, 2mm ~ 3mm, 4mm ~
The spheric granules of 6mm；
4) above-mentioned material is dried, 200 DEG C of temperature, dry 1 ~ 2h, then carries out high-temperature calcination, 1300 ~ 1500 DEG C of temperature, protected
Required temperature adjustment medium is made after cooling in 2 ~ 4h of temperature.
Prepared temperature adjustment media particles thermal capacity 1400J/kg.k, bulk density 2.2g/cm3, bulk density 950kg/
m3, temperature adjustment media particles particle diameter distribution is selected as 0.5mm ~ 1mm=50wt%, 2mm ~ 3mm=30wt%, 4mm ~ 6mm=20wt%.Coal washing
Factory's coal slime is slightly dehydrated through belt filter press first, and moisture is down to 45wt% or so, is entered back into steam rotary dryer and is done
Dry processing, makes moisture of coal fines be further reduced to 15wt%.Reactor scale: 40t/h(3.82MPa), slime treatment quantity 11t/h(contains
Water 15wt%).Reactor reaction condition are as follows: 850 ~ 920 DEG C of reaction temperature, bed pressure drop 10kPa, heat-accumulation combustion area, equal thermal oxide
Area and separation back-mixing area fluidizing gas velocity are controlled respectively in 5m/s, 4.5m/s, 3m/s, separate the V that is staggered two layers to fall in back-mixing area
Type baffle plate, the ratio of S1:S2:S3 are 2:3:4.Coal slime material particles after reaction chamber oxidizing fire with flue gas enter separation
Device, the particle in separator less than 60 μm of separator incising control enter flue with flue gas, are greater than cutting grain particles through returning charge
Device Returning reactor becomes outer circulation material, after recycling thermal energy into the flue gas of flue and to the heat exchange of water and air wind, through removing
After the purified treatments such as dirt, desulphurization and denitration, qualified discharge is realized.Coal slime is handled by the method for the invention, when increasing coal slime oxidation
Between, cooperate the multizone fluidising effect of temperature adjustment medium and reactor, coal slime oxygenation efficiency is up to 98% or more.Coal slime oxidation efficiency
It improves, can reduce solid-unburning hot loss q4, and due to the method for the present invention bottom bed drain purge → 0, so that q6 → 0,
Heat loss substantially reduces, and the reactor entirety thermal efficiency can reach 90% or more.
Comparative example 1
It is same as Example 1, the difference is that not using temperature adjustment media particles, run using pure coal combustion, due to not having
Have the material that gradation particle diameter distribution is added, the ciculation fluidized state effect of reactor substantially reduces, influence between material particles, material with
Heat-transfer effect between reactor wall surface is difficult to realize the stabilization oxidizing fire of coal slime particle, so that coal slime oxidation efficiency and reaction
The device thermal efficiency is lower, and the coal slime oxidation efficiency of pure coal combustion operating condition is lower than 80% in this comparative example 1.
Comparative example 2
It is same as Example 1, the difference is that reactor use current regular circulation fluidized-bed combustion boiler, i.e., boiler dilute-phase zone without
Variable cross-section setting, and temperature adjustment media particles are not used in reactor, the operation of burning form, gangue heat are mixed using Slime Mixed Coal Gangue
Quite (9700MJ/kg or so) with coal slime calorific value, coal slime is mixed burns mass ratio 70% to value, in gangue particle diameter distribution and embodiment 1
Temperature adjustment medium is identical, and when reaching 1 coal slime treatment scale of embodiment, Thermal Efficiency of Circulating Fluidized Bed Boiler 85% is left in this comparative example 2
The right side, coal combustion efficiency 93% or so.
Claims (33)
1. a kind of coal slime processing method, the treating method comprises following content:
(1) coal slime enters reactor, contacts with the temperature adjustment media particles in the temperature adjustment medium bed in reactor, in fluidized wind
Effect is lower to carry out oxidation reaction；
(2) flue gas in step (1) after coal slime oxidizing fire carries out separating treatment, the bulky grain temperature adjustment medium taken out of by flue gas
Grain Returning reactor after separation, coal slime and temperature adjustment media particles the abrasion fine powder of smaller particle in the form of flying dust with flue gas into
Row post-processing.
2. coal slime processing method described in accordance with the claim 1, it is characterised in that: coal slime described in step (1) enters reactor
It is carried out dehydrating before, the coal slime water content after dehydration is not more than 20wt%, preferably no greater than 15wt%.
3. coal slime processing method described in accordance with the claim 1, it is characterised in that: the temperature adjustment medium bed of material described in step (1) by
Temperature adjustment media particles constitute, temperature adjustment media particles by silica, titanium oxide, aluminium oxide, lithia, diatomite, feldspar, quartz,
One or more of cordierite, mullite are made.
4. coal slime processing method described in accordance with the claim 1, it is characterised in that: the partial size of the temperature adjustment media particles be 0.5 ~
10mm, preferably 1 ~ 6mm, further preferably 1 ~ 4mm.
5. coal slime processing method described in accordance with the claim 1, it is characterised in that: the temperature adjustment media particles shape be it is spherical,
One or more of sheet, bulk, jujube shape, cylindrical shape.
6. coal slime processing method described in accordance with the claim 1, it is characterised in that: the temperature adjustment media particles be it is solid, hollow,
Surface fluting is internal with cellular structure.
7. coal slime processing method described in accordance with the claim 1, it is characterised in that: the bulk density of the temperature adjustment media particles
1500~3000 kg/m3, 700 ~ 2000 kg/m of bulk density3。
8. coal slime processing method described in accordance with the claim 1, it is characterised in that: the temperature adjustment media particles thermal capacity is greater than
1300 J/kg k, thermal coefficient are greater than 2.6 w/m k.
9. coal slime processing method described in accordance with the claim 1, it is characterised in that: temperature adjustment medium bed of material packet described in step (1)
The temperature adjustment media particles for including two or more different-grain diameters preferably include the temperature adjustment media particles of three kinds of different-grain diameters.
10. coal slime processing method according to claim 9, it is characterised in that: as the temperature adjustment matchmaker including two kinds of different-grain diameters
When Jie's particle, one of temperature adjustment media particles partial size is 1 ~ 2mm, and another temperature adjustment media particles partial size is 4 ~ 5mm；When including
When the temperature adjustment media particles of three kinds of different-grain diameters, the partial size of three kinds of temperature adjustment media particles is respectively 0.5 ~ 1mm, 2 ~ 3mm, 4 ~ 6mm.
11. coal slime processing method described in accordance with the claim 1, it is characterised in that: reaction temperature described in step (1) be 800 ~
950 DEG C, 2 ~ 8 m/s of fluidizing velocity, 5 ~ 15 kPa of bed pressure drop.
12. coal slime processing method described in accordance with the claim 1, it is characterised in that: flue gas obtained in step (2), which post-processes, is
Heat exchange is carried out into flue and the heat exchange equipment that is arranged in flue, recovered flue gas thermal energy, then it is net through dedusting, desulphurization and denitration
Qualified discharge after change processing.
13. coal slime processing method described in accordance with the claim 1, it is characterised in that: step (2) it is described separation in the separator into
Row, the separator are cyclone separator or inertia separator.
14. coal slime processing method described in accordance with the claim 1, it is characterised in that: reactor described in step (1), which uses, to be had
It is described such as the circulating fluid bed reactor of flowering structure, including air compartment, reaction chamber, separator, material-returning device and steam generation facility
Steam generation facility includes drum and water-cooling wall, and drum is set to the outer top of reactor, and water-cooling wall is set to reactor wall, described anti-
Room is answered to be divided into heat-accumulation combustion area, soaking zoneofoxidation and separation back-mixing area from the bottom to top；It is set between the air compartment and heat-accumulation combustion area
There is air distribution plate, the air compartment bottom is provided with First air entrance, is equipped with the temperature adjustment medium bed of material in the heat-accumulation combustion area, separation is returned
Confounding is connected to through pipeline with separator inlet, and the separator bottom outlet is connected to through refeed line with material-returning device one end, described
The material-returning device other end is connected to through pipeline with the return port in heat-accumulation combustion area.
15. coal slime processing method according to claim 14, it is characterised in that: the heat-accumulation combustion area of the reaction chamber is to become
Gauge structure, the soaking zoneofoxidation are to wait gauge structures, and the lower part in the separation back-mixing area is variable-diameter structure, and top is isometrical knot
Structure, wherein the outer wall of separation back-mixing area lower part variable-diameter structure and the angle α of horizontal plane are not less than the angle of repose of handled material.
16. coal slime processing method according to claim 14, it is characterised in that: heat-accumulation combustion area minimum sectional area is
S1, soaking zoneofoxidation sectional area are S2, and separation back-mixing area maximum secting area is S3, and the ratio of S1:S2:S3 is 1:3/2 ~ 3:2 ~ 5,
Preferably 2:3:4.
17. coal slime processing method according to claim 14, it is characterised in that: temperature adjustment medium material in the heat-accumulation combustion area
The volume of floor is the 1/3 ~ 2/3 of heat-accumulation combustion area volume.
18. coal slime processing method according to claim 14, it is characterised in that: the indoor heat-accumulation combustion area of the reaction,
Soaking zoneofoxidation and the fluidising air velocity for separating back-mixing area are controlled respectively in 4 ~ 8m/s, 3 ~ 6m/s, 2 ~ 4m/s.
19. coal slime processing method according to claim 14, it is characterised in that: the heat-accumulation combustion area and soaking zoneofoxidation
Secondary Air entrance is arranged in intersection, and the following are heat-accumulation combustion areas for Secondary Air entrance.
20. coal slime processing method according to claim 19, it is characterised in that: the Secondary Air entrance top is additionally provided with
Device in Gas entrance is realized by setting device in Gas entrance while handling low concentration gas.
21. coal slime processing method described in accordance with the claim 1, it is characterised in that: the material-returning device returns for automatic adjustment
Expect device or valve-type material-returning device.
22. coal slime processing method described in accordance with the claim 1, it is characterised in that: the temperature adjustment medium bed of material is by temperature adjustment medium
Particle is constituted, and the temperature adjustment media particles are green by silica, titanium oxide, aluminium oxide, lithia, diatomite, feldspar, quartz, violet
One or more of Shi Zhi, mullite are made.
23. according to the coal slime processing method described in claim 22, it is characterised in that: the particle size range of the temperature adjustment media particles
0.5 ~ 10 mm, preferably 1 ~ 6mm.
24. according to the coal slime processing method described in claim 22, it is characterised in that: the temperature adjustment media particles shape is ball
One or more of shape, sheet, bulk, jujube shape, cylindrical shape.
25. according to the coal slime processing method described in claim 22, it is characterised in that: the temperature adjustment media particles are solid, empty
The heart, surface fluting or internal with cellular structure.
26. according to the coal slime processing method described in claim 22, it is characterised in that: the temperature adjustment medium bed of material include two kinds with
The temperature adjustment media particles of upper different-grain diameter preferably include the temperature adjustment media particles of three kinds of different-grain diameters.
27. according to the coal slime processing method described in claim 26, it is characterised in that: as the temperature adjustment matchmaker including two kinds of different-grain diameters
When Jie's particle, one of temperature adjustment media particles partial size is 1 ~ 2mm, and another temperature adjustment media particles partial size is 4 ~ 5mm；When including
When the temperature adjustment media particles of three kinds of different-grain diameters, the partial size of three kinds of temperature adjustment media particles is respectively 0.5 ~ 1mm, 2 ~ 3mm, 4 ~ 6mm.
28. coal slime processing method according to claim 14, it is characterised in that: set in the separation back-mixing area of the reaction chamber
Baffle plate is set, the baffle plate is arranged one layer or more, and lowest level arrangement of baffles is separating the above space of back-mixing area reducer, when
When two layers of setting or more baffle plate, adjacent two layers baffle plate interlaced arrangement.
29. according to the coal slime processing method described in claim 28, it is characterised in that: the baffle plate be board-type, inclined plate type,
One of groove profile, inverted V type are a variety of, preferably inverted V type baffle plate.
30. coal slime processing method according to claim 14, it is characterised in that: the separator be cyclone separator and/
Or inertia separator, preferably cyclone separator.
31. coal slime processing method according to claim 14, it is characterised in that: the reactor is equipped with feed inlet, described
Feed inlet is set up directly on heat-accumulation combustion area side wall, or is arranged on the pipeline that material-returning device is connected to heat-accumulation combustion area.
32. coal slime processing method according to claim 14, it is characterised in that: the interior heat collecting device is set to reaction chamber point
Back-mixing area inner top is separated from being further preferably set in back-mixing area.
33. coal slime processing method according to claim 14, it is characterised in that: heat-accumulation combustion area bottom is additionally provided with
Slag-drip opening.
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| CN110332528A (en) * | 2019-08-09 | 2019-10-15 | 江苏恒科新材料有限公司 | A kind of biomass circulating fluidized bed furnace |
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