CN208886757U - A kind of coal slime processing system - Google Patents
A kind of coal slime processing system Download PDFInfo
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- CN208886757U CN208886757U CN201821119697.4U CN201821119697U CN208886757U CN 208886757 U CN208886757 U CN 208886757U CN 201821119697 U CN201821119697 U CN 201821119697U CN 208886757 U CN208886757 U CN 208886757U
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- 239000003245 coal Substances 0.000 title claims abstract description 124
- 238000006243 chemical reaction Methods 0.000 claims abstract description 52
- 238000000926 separation method Methods 0.000 claims abstract description 48
- 238000001035 drying Methods 0.000 claims abstract description 18
- 238000000746 purification Methods 0.000 claims abstract description 12
- 239000002245 particle Substances 0.000 claims description 49
- 238000002485 combustion reaction Methods 0.000 claims description 48
- 238000009825 accumulation Methods 0.000 claims description 45
- 238000002156 mixing Methods 0.000 claims description 35
- 239000000463 material Substances 0.000 claims description 33
- 238000002791 soaking Methods 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 11
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 239000003638 chemical reducing agent Substances 0.000 claims description 3
- 238000009826 distribution Methods 0.000 claims description 3
- 238000010276 construction Methods 0.000 claims description 2
- 239000003818 cinder Substances 0.000 claims 1
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- 239000002994 raw material Substances 0.000 abstract description 8
- 230000003647 oxidation Effects 0.000 abstract description 7
- 238000007254 oxidation reaction Methods 0.000 abstract description 7
- 230000001590 oxidative effect Effects 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000002910 solid waste Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 23
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 16
- 239000003546 flue gas Substances 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000000428 dust Substances 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 230000033001 locomotion Effects 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000011044 inertial separation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 239000012716 precipitator Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 240000008866 Ziziphus nummularia Species 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 235000006708 antioxidants Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 210000003850 cellular structure Anatomy 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 229910052878 cordierite Inorganic materials 0.000 description 1
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 description 1
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- 229910001947 lithium oxide Inorganic materials 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The utility model discloses a kind of coal slime processing systems, including dewatering unit, drying unit, Reaction Separation unit, flue and gas purification units, the feeding line is successively connected to after dewatering unit and drying unit with Reaction Separation unit entrance, the outlet of Reaction Separation unit is connected to through pipeline with flue entrance, and flue outlet is connected to through pipeline with gas purification units entrance；The Reaction Separation unit includes reaction chamber, air compartment, separator, material-returning device and steam generation facility.The coal slime processing system is capable of providing stable coal slime oxidizing temperature by reaction chamber structure adjustment, can handle the low heat value coal slime solid waste that ash content is big, partial size is small, realizes that coal slime minimizing, harmless treatment and efficient resource 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 high, and being capable of long-period stable operation.
Description
Technical field
The utility model belongs to coal slime processing equipment field, handles coal slime using recirculating fluidized bed more particularly to a kind of
Processing system.
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 seriously pollute environment.Coal slime particle is very thin, and dehydration is extremely difficult,
After desiccation, flies upward all over the sky to the wind, meets rainwater and trickle everywhere, it is very big to environmental ecology landscape impact.But coal slime has one
Fixed calorific value, the calorific value of some low ash coal mud are even higher than some low heat value thermal coals, and the existing extensive processing mode of coal slime is made
At great energy waste, with the rapid development of coal washing industry, the slime content that China is discharged every year is also quick therewith
Increase, therefore, the harmless treatment of coal slime and resource utilization are extremely urgent;
With a large amount of drawing-off gas, gas is one of the main source of current China's greenhouse gases effect for coal production, by
In technical restriction, the methane gas 70% generated in coal in China production is all directly discharged in atmosphere, with mining depth plus
Greatly, gas and coal seam risk are prominent, and the Coal Mine Disasters such as gas explosion dominate the situation increasingly severe;
How efficiently to solve coal slime accumulation and reduce the discharge of gas in shaft production, tool is exploited and run to coal mining enterprise
It is of great importance.Coal slime and gas all have certain calorific value, if heat recovery and utilization therein has not only been saved resource, and
And reduce production cost.Coal slime replaces coal-fired as boiler oil and carries out burning to utilize being the preferably square of current processing coal slime
Method.Moisture and ash content and lower calorific value due to high-content, coal slime are not suitable for traditional coal-powder boiler burning.Low heat value
For coal resources using circulating fluidized bed boiler is mainly used, coal slime is widely used in circulating fluidized bed combustion.But current coal slime
Circulating fluidized bed boiler has the following problems: (1) pure coal combustion calorific value is low, low efficiency, generally requires and mixes with high heating value coal
It burns, 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
Burning fat coal is mixed, circulating fluidization is maintained；(3) coal slime water content is high, and moisture is not easy to control, easily forms clod, often adopts at present
Fed with upper furnace, due to coal slime to access point close to furnace outlet, there are a large amount of coal slimes in the case where no after-flame
It is directly fluidized wind and has gone out burner hearth, into separator, and coal slime granularity is small, and separator is captured less than becoming flying dust, lead
It causes the coal slime residence time insufficient, burns insufficient, efficiency of combustion is low；(4) for circulating fluidized bed boiler, bed endoparticle passes through one
The operation of section time, coarse granule sink to emulsion zone, and fine grained becomes flying dust, and the particle of only certain particle size range becomes stable and follows
Ring ash, for stable bed storage, needs regular deslagging.General bottom deslagging share accounts for 30% or more total ash, causes q6(lime-ash
Physics heat loss) heat loss, reduce boiler thermal efficiency.
Utility model content
Existing coal slime processing unit there are aiming at the problem that, the utility model provides a kind of coal slime processing system, described
System includes that structure is simple, Reaction Separation unit of efficiency of carbon con version and high combustion efficiency, can be mentioned by reaction chamber structure adjustment
For stable coal slime oxidizing temperature, the low heat value poor quality coal slime that ash content is big, partial size is small can handle, realize coal slime minimizing, nothing
Evilization processing and efficient resource utilize.It, can be using pure coal slime as raw material without mixing burning fat coal when handling coal slime using this system
It carries out oxidation and burns recycling heat, coal slime oxidation efficiency and the device thermal efficiency are high, and being capable of long-period stable operation.
The utility model provides a kind of coal slime processing system, the coal slime processing system include dewatering unit, drying unit,
Reaction Separation unit, flue and gas purification units, the feeding line successively after dewatering unit and drying unit with react
Separative unit connection, Reaction Separation unit are connected to through pipeline with flue entrance, and flue outlet enters through pipeline and gas purification units
Mouth connection；The Reaction Separation unit includes reaction chamber, air compartment, separator, material-returning device and steam generation facility, the steam
Generating device 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, the reaction chamber
It is divided into heat-accumulation combustion area, soaking zoneofoxidation and separation back-mixing area from the bottom to top；Cloth is equipped between the air compartment and heat-accumulation combustion area
Aerofoil, the air compartment bottom are provided with First air entrance, are equipped with the temperature adjustment medium bed of material in the heat-accumulation combustion area, separate back-mixing area
It is connected to through pipeline with separator inlet, the separator bottom outlet is connected to through refeed line with material-returning device one end, the returning charge
The device other end is connected to through pipeline with the return port in heat-accumulation combustion area, and the separator top exit is connected to through pipeline with flue.
In coal slime processing system described in the utility model, coal slime dewatering to water content can be not more than by the dewatering unit
35wt%, the dewatering unit can use mechanical dehydration or gravity dehydration, preferably mechanical dehydration, specially filter press, belt pressure
One or more of machine, disk vacuum filter, belt vacuum filter, fold belt vacuum filter.
In coal slime processing system described in the utility model, the drying unit is for will be through dewatering unit treated coal slime
It is further dried to water content no more than 15wt%.The drying unit is dry using thermal energy, can be outer hot indirect type or interior heat
Direct contact type, heat source can be flue gas or steam, specially vertical preferably using self-produced steam as the outer heated drying mode of heat source
One or more of formula, horizontal, rotary steam drying.
In coal slime processing system described in the utility model, heat exchange equipment, the heat exchange equipment foundation are equipped in the flue
One or more of actual demand and purposes, including superheater, economizer and air preheater, the superheater, economizer
It is successively set in flue with air preheater according to high-temperature flue gas sequence of flow.
In coal slime processing system described in the utility model, the gas purification units include cleaner, desulphurization plant and
One or more of denitration device, the cleaner, desulphurization plant and denitration device are using the existing equipment in this field
Can, it can be dedusting, desulfurization and denitration separate unit, or the dust removal integrated equipment of desulphurization denitration, those skilled in the art
Member can select suitable equipment according to processing requirement, and this selection is easy to those skilled in the art.Such as
One of gravitational precipitator, inertial dust separator, cyclone dust collectors, sack cleaner and electric precipitator, desulfurization may be selected in dedusting
It handles and dry method, semidry method or wet desulphurization equipment may be selected, denitration can be according to being arranged in flue gas NOx emission behaviour selecting reactor
SNCR denitration, flue are arranged SCR denitration facility and in one or more of subsequent setting supplement oxidation denitration devices of flue.
In coal slime processing system described in the utility model, the heat-accumulation combustion area of the reaction chamber is variable-diameter structure, described 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 separating back-mixing
The outer wall of area lower part variable-diameter structure and the angle α of horizontal plane are not less than the angle of repose of handled material.
In coal slime processing system described in the utility model, heat-accumulation combustion area minimum sectional area is S1, soaking zoneofoxidation
Sectional area is 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.
In coal slime processing system described in the utility model, the volume of the temperature adjustment medium bed of material is accumulation of heat in the heat-accumulation combustion area
The 1/3 ~ 2/3 of combustion zone volume.
In coal slime processing system described in the utility model, the indoor heat-accumulation combustion area of the reaction, soaking zoneofoxidation and
The fluidising air velocity in separation back-mixing area is controlled respectively in 4 ~ 8m/s, 3 ~ 6m/s, 2 ~ 4m/s.
In coal slime processing system described in the utility model, the heat-accumulation combustion area and the setting of soaking zoneofoxidation intersection are secondary
Wind entrance, the following are heat-accumulation combustion areas for Secondary Air entrance.
In coal slime processing system described in the utility model, the Secondary Air entrance top is additionally provided with device in Gas entrance, leads to
Crossing setting device in Gas entrance may be implemented to handle low concentration gas simultaneously.
In coal slime processing system described in the utility model, the material-returning device can be automatic adjustment material-returning device or valve
Type material-returning device.
In coal slime processing system described in the utility model, the temperature adjustment medium bed of material is made of temperature adjustment media particles, described
Temperature adjustment media particles can be by silica, titanium oxide, aluminium oxide, lithia, diatomite, feldspar, quartz, cordierite, Mo Lai
One or more of stone etc. is made.Particle size range 0.5 ~ 10 mm of the temperature adjustment media particles, preferably 1 ~ 6mm, the tune
Warm media particles shape can be one or more of shapes such as spherical shape, sheet, bulk, jujube shape, cylindrical body, can be real
The heart, hollow, surface fluting or internal with cellular structure.1500 ~ 3000 kg/m of bulk density of temperature adjustment media particles3, heap
Product 700 ~ 2000 kg/m of density3.The temperature adjustment media particles have big thermal capacity, high thermal conductivity coefficient, high abrasion, anti-oxidant, anti-
The properties such as burn into thermal expansion coefficient is small.Thermal capacity the > 1300 J/kg k, thermal coefficient > 2.6 of the temperature adjustment media particles
w/m▪k。
In coal slime processing system described in the utility model, the temperature adjustment medium bed of material includes the tune of two or more different-grain diameters
Warm 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 grain, 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 kinds
When the temperature adjustment media particles of 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 system described in the utility model, the reaction chamber section can be arbitrary shape, such as rectangular, round,
Polygon etc., it is preferably circular.
In coal slime processing system described in the utility model, baffle plate is set in the separation back-mixing area of the reaction chamber, it is described
Baffle plate is arranged one layer or more, and lowest level arrangement of baffles is in the separation above space of back-mixing area reducer, when two layers of setting or more
When baffle plate, adjacent two layers baffle plate interlaced arrangement.The baffle plate can make the material movement direction moved upwards with flue gas
One or many deflections occur, deflection angle is close to or higher than 180 °, to realize the inertial separation of different-grain diameter particle, baffling
Plate can be one of board-type, inclined plate type, groove profile, inverted V type or a variety of, preferably inverted V type baffle plate.
In coal slime processing system described in the utility model, the separator can be cyclone separator and/or inertial separation
Device, preferably 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 determines that control dp is less than the smallest particles degree of temperature adjustment media particles, it is ensured that temperature adjustment media particles pass through material-returning device
Reaction chamber heat-accumulation combustion area is returned to be recycled.The separator can be set one or more according to reactor granules load is taken out of
A, when more than two separators are arranged, separator can connect in parallel or series.
In coal slime processing system described in the utility model, the separator, refeed line and material-returning device be can be set in anti-
It answers outside chamber interior or reaction chamber.
In coal slime processing system described in the utility model, the reactor is equipped with feed inlet, and the feed inlet can be direct
It is arranged on heat-accumulation combustion area side wall, also can be set on the pipeline that material-returning device is connected to heat-accumulation combustion area.
In coal slime processing system described in the utility model, the interior heat collecting device is set in reaction chamber separation back-mixing area, into
One step is preferably disposed on separation back-mixing area inner top.
In coal slime processing system described in the utility model, the outer top of the reaction chamber is arranged drum, in drum and reactor
The water-cooling wall of wall laying is connected.Water in water-cooling wall is heated after generation hot water and steam into drum in reaction chamber, and drum is made
Steam after can be used for industrial production or domestic life, and the water in drum continuously recycles supply water-cooling wall.
In coal slime processing system described in the utility model, heat-accumulation combustion area bottom is also provided with slag-drip opening.
Compared with prior art, coal slime processing system described in the utility model has the advantage that
1, in coal slime processing system described in the utility model, the reaction chamber in the Reaction Separation unit is divided into heat-accumulation combustion
Variable-diameter structure is arranged in area, soaking zoneofoxidation and separation back-mixing area, the heat-accumulation combustion area and separation back-mixing area, and matches in accumulation of heat
The temperature adjustment medium bed of material is set in combustion zone, can realize that the back-mixing of different-grain diameter temperature adjustment media particles is followed with interior in reaction chamber
Ring realizes multizone, multithread field, multicycle material movement state, when for handling big ash content, fine grain coal slime raw material
When, heat-accumulation combustion and equal thermal oxidation by temperature adjustment media particles, realize big ash content, fine grained raw material stabilization, sufficiently
Oxidation, thermal stability is good, and load regulation range is big, and without adding the high-quality coal slime raw material of other bulky grains, pure burn carefully may be implemented
The coal slime raw material of particle;
2, in coal slime processing system described in the utility model, by using the temperature adjustment medium of different-grain diameter in reaction chamber
Grain, can be better achieved coal slime material particles and temperature adjustment media particles surface and its with the quick update that takes hot wall contact surface, oxygen
It is high to change intensity, heat transfer efficiency is high, and the Thermal load of cross-section of heat-accumulation combustion area and soaking zoneofoxidation is up to 6MW/m2More than;
3, in coal slime processing system described in the utility model, separation back-mixing area is variable-diameter structure, considerably increases material and exists
The indoor residence time is reacted, keeps material fully oxidized, improves 5% or more than conventional fluidization bed boiler burning rate.Further dividing
From baffle plate is arranged inside back-mixing area, makes the direction of motion of material that one or many deflections occur, further increase material
Residence time realizes material particles crude separation in separation back-mixing area, reduces the processing load of rear end separator;
4, in coal slime processing system described in the utility model, the height ratio of reaction chamber is the same as the existing circulating fluidized bed boiler of scale
20% or more can be reduced, device steel consumption is saved, significantly reduces cost.
Detailed description of the invention
Fig. 1 is coal slime processing system schematic diagram described in the utility model.
Fig. 2 is structure of reactor schematic diagram described in the utility model.
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, 20- charging
Pipeline, 21- dewatering unit, 22- drying unit, 23- Reaction Separation unit, 24- flue, 25- gas purification units, 26- overheat
Device, 27- economizer, 28- air preheater.
Specific embodiment
The concrete condition of the utility model is further illustrated below by specific embodiment, but is not limited to following implementation
Example.
In the description of the present invention, it should be noted that term " on ", "lower", "inner", "outside", "top", "bottom"
The orientation or positional relationship of equal instructions is to be based on the orientation or positional relationship shown in the drawings, and being merely for convenience of description, this is practical new
Type and simplified description, rather than the device or element of indication or suggestion meaning must have a particular orientation, with specific orientation
Construction and operation, therefore should not be understood as limiting the present invention.In addition, term " first ", " second " are only used for describing
Purpose is not understood to indicate or imply relative importance.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " is set
Have ", " being placed in ", " connected ", " connection ", " installation " etc. shall be understood in a broad sense, for example, it may be being fixedly connected, being also possible to can
Dismantling connection, or be integrally connected；It can be mechanical connection, be also possible to be electrically connected；It can be directly connected, can also pass through
Intermediary is indirectly connected, and can be the connection inside two elements.For the ordinary skill in the art, can have
Body situation understands the concrete meaning of above-mentioned term in the present invention.
As depicted in figs. 1 and 2, the utility model provides a kind of coal slime processing system, and the coal slime processing system includes de-
Water unit 21, drying unit 22, Reaction Separation unit 23, flue 24 and gas purification units 25, the dewatering unit can be adopted
With mechanical dehydration or gravity dehydration, preferably mechanical dehydration, specially filter press, band press, disk vacuum filter, belt is true
One or more of empty filter, fold belt vacuum filter；The drying unit is dry using thermal energy, can be for outer heat indirectly
Formula or interior hot 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, tool
Body is one or more of vertical, horizontal, rotary steam drying.The raw material is through feeding line 20 successively through dewatering unit
21 and drying unit 22 after be connected to 23 entrance of Reaction Separation unit, Reaction Separation unit 23 export through pipeline and 24 entrance of flue
It is connected to, is disposed with superheater 26, economizer 27 and air preheater 28 according to flow of flue gas direction in the flue 24；Cigarette
The outlet of road 24 is connected to through pipeline with 25 entrance of gas purification units；The Reaction Separation unit 23 include 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-cooling wall is not drawn into Fig. 2, is those skilled in the art's common knowledge)；The reaction chamber 1 be divided into from the bottom to top heat-accumulation combustion area A,
Soaking zoneofoxidation B and separation back-mixing area C；Air distribution plate 8, the wind are equipped between the air compartment 7 and the heat-accumulation combustion area A of reaction chamber
7 bottom of room is provided with First air entrance 11, and the temperature adjustment medium bed of material, the temperature adjustment medium material are provided in the heat-accumulation combustion area A
Layer is made of temperature adjustment media particles, and slag-drip opening 16 is arranged in bottom in heat-accumulation combustion area A, and heat-accumulation combustion area A and soaking zoneofoxidation B are handed over
Secondary Air entrance 12 is set at boundary, and Secondary Air entrance is provided with watt the following are heat-accumulation combustion area A on the side wall of soaking zoneofoxidation B
This gas entrance 13, device in Gas entrance 13 are located at 12 top of Secondary Air entrance, are provided with baffle plate above separation back-mixing area C reducer
18, separation back-mixing area C inner top is provided with interior heat collecting device 5, and shown interior heat collecting device 5 can be superheater, separates back-mixing area C through pipe
Line is connected to 2 entrance of separator, and 2 outlet at bottom of separator is connected to through refeed line 3 with 4 one end of material-returning device, the returning charge
4 other end of device is connected to through pipeline with heat-accumulation combustion area A return port 17, and material outlet 15, material outlet are equipped at the top of separator 2
15 are connected to by pipeline with flue 24.The feed inlet 14 is set up directly on heat-accumulation combustion area A side wall, or is arranged in returning charge
On the refeed line 3 that device 4 is connected to the heat-accumulation combustion area A of reaction chamber 1.Feed inlet 14 and return port 17 are lower than overfiren air port 12,
Device in Gas entrance 13 is slightly above overfiren air port 12.
When in use, specific work process is as follows for coal slime processing system described in the utility model: raw material coal slime first passes around
Dewatering unit and drying unit are slightly dehydrated and are dried, and coal slime that treated enters Reaction Separation unit, coal slime from into
Material mouth enters the reaction chamber of Reaction Separation unit, successively in heat-accumulation combustion area, soaking zoneofoxidation and separation back-mixing area internal oxidition
Burning processing, wherein releasing heat is more in heat-accumulation combustion the area in, the heat of generation by greater particle size temperature adjustment media particles accumulation of heat
It absorbs；It is continued up compared with the material of small particle and temperature adjustment media particles with the flue gas generated after burning and flows into equal thermal oxide
Area, further occurrence aoxidizes under the supplement of Secondary Air；When material enters separation back-mixing area, since gas flow area increases,
Flow velocity reduces, and the gas residence time for carrying particle increases, and the ash content in flue gas has time enough to complete reaction, while rolling over
Under the effect of flowing plate separation assembly, biggish particles fall realizes initial gross separation with flue gas, due to the difference of fluidizing velocity, anti-
It answers interior to form interior circulation, enhances the mixing of transverse direction and longitudinal direction.Material is sufficiently mixed in flow process with temperature adjustment medium,
The two constantly collides and rubs, so that larger particles material is gradually crushed under the action of temperature adjustment medium, becomes smaller, and temperature adjustment
Medium is smaller due to itself having certain rigidity loss, the subsequent circulation that can be separated from flue gas when flowing through separator
It utilizes.Temperature adjustment medium constantly absorbs material and aoxidizes discharged heat, maintains reaction room temperature at 800 ~ 950 DEG C, make newly into
The material for entering reaction chamber is brought rapidly up and oxidizing fire；Temperature adjustment medium is sufficiently mixed and fluidizes with material simultaneously, will be a large amount of
Heat pass to reaction chamber surrounding water-cooling wall and separate back-mixing area in setting take thermal, not only heat was efficiently used, but also avoids
Reaction room temperature is excessively high to be caused coking and generates thermal NO x.The flue gas for carrying particle enters from reaction chamber separation back-mixing area
It is further separated after separator, material particles, which are returned to through refeed line with material-returning device with temperature adjustment medium from separator tail portion, to react
Interior, the flue gas after separation are discharged into flue below from separator outlet；After flue gas enters flue, high-temperature flue gas is passed sequentially through
Superheater, economizer and the air preheater being arranged in flue carry out heat exchange, and recovered flue gas thermal energy, flue gas passes through again out
After gas purification units processing, qualified discharge.
Claims (28)
1. a kind of coal slime processing system, the coal slime processing system includes feeding line, dewatering unit, drying unit, reaction point
From unit, flue and gas purification units, it is characterized in that: the feeding line is successively after dewatering unit and drying unit and anti-
Separative unit is answered to be connected to, Reaction Separation unit is connected to through pipeline with flue entrance, and flue outlet is through pipeline and gas purification units
Entrance connection；The Reaction Separation unit includes reaction chamber, air compartment, separator, material-returning device and steam generation facility, the steaming
Vapour generating device 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, the reaction
Room is divided into heat-accumulation combustion area, soaking zoneofoxidation and separation back-mixing area from the bottom to top；It is equipped between the air compartment and heat-accumulation combustion area
Air distribution plate, the air compartment bottom are provided with First air entrance, are equipped with the temperature adjustment medium bed of material in the heat-accumulation combustion area, separate back-mixing
Area 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 to return
The material device other end is connected to through pipeline with the return port in heat-accumulation combustion area, and the top exit of the separator connects through pipeline and flue
It is logical.
2. coal slime processing system described in accordance with the claim 1, it is characterised in that: the dewatering unit is using mechanical dehydration or again
Power dehydration.
3. coal slime processing system according to claim 2, it is characterised in that: the dewatering unit uses filter press, belt
One or more of press, disk vacuum filter, belt vacuum filter.
4. coal slime processing system described in accordance with the claim 1, it is characterised in that: the drying unit is dry using thermal energy, is
Outer hot indirect type or interior hot direct contact type.
5. coal slime processing system described in accordance with the claim 1, it is characterised in that: be provided with heat exchange equipment, institute in the flue
Stating heat exchange equipment is one or more of superheater, economizer and air preheater.
6. coal slime processing system described in accordance with the claim 1, it is characterised in that: the gas purification units include that dedusting is set
One or more of standby, desulphurization plant and denitration device.
7. coal slime processing system described in accordance with the claim 1, it is characterised in that: the heat-accumulation combustion area is variable-diameter structure, institute
Stating soaking zoneofoxidation 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.
8. coal slime processing system according to claim 7, it is characterised in that: the outer wall of separation back-mixing area lower part variable-diameter structure
It is not less than the angle of repose of handled material with the angle α of horizontal plane.
9. coal slime processing system described in accordance with the claim 1, 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.
10. coal slime processing system according to claim 9, it is characterised in that: the ratio of S1:S2:S3 is 2:3:4.
11. coal slime processing system described in accordance with the claim 1, 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.
12. coal slime processing system according to claim 11, it is characterised in that: the Secondary Air entrance top is provided with watt
This gas entrance.
13. coal slime processing system described in accordance with the claim 1, it is characterised in that: the material-returning device is valve-type material-returning device.
14. coal slime processing system 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.
15. coal slime processing system according to claim 14, it is characterised in that: the particle size range of the temperature adjustment media particles
0.5 ~ 10 mm, the shape of the temperature adjustment media particles are one or more of spherical shape, sheet, bulk, cylindrical body.
16. coal slime processing system according to claim 15, it is characterised in that: the temperature adjustment media particles are solid, empty
The heart or surface notching construction.
17. coal slime processing system according to claim 16, it is characterised in that: the hollow structure is internal with duct
Structure.
18. coal slime processing system described in accordance with the claim 1, 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, when including the temperature adjustment media particles of two kinds of different-grain diameters, one of temperature adjustment medium
Grain diameter is 1 ~ 2mm, and another temperature adjustment media particles partial size is 4 ~ 5mm.
19. coal slime processing system described in accordance with the claim 1, it is characterised in that: the temperature adjustment medium bed of material include three kinds not
With the temperature adjustment media particles of partial size, when including the temperature adjustment media particles of three kinds of different-grain diameters, the grain of three kinds of temperature adjustment media particles
Diameter is respectively 0.5 ~ 1mm, 2 ~ 3mm, 4 ~ 6mm.
20. coal slime processing system described in accordance with the claim 1, it is characterised in that: baffle plate is set in the separation back-mixing area,
The baffle plate is arranged one layer or more, and lowest level arrangement of baffles is in the separation above space of back-mixing area reducer.
21. coal slime processing system according to claim 20, it is characterised in that: when two layers of setting or more baffle plate, phase
Adjacent two layers of baffle plate interlaced arrangement.
22. coal slime processing system according to claim 20, it is characterised in that: the baffle plate be board-type, inclined plate type,
One or more of groove profile, inverted V type.
23. coal slime processing system described in accordance with the claim 1, it is characterised in that: the separator is inertia separator.
24. according to the coal slime processing system described in claim 23, it is characterised in that: the inertia separator is cyclonic separation
Device.
25. coal slime processing system described in accordance with the claim 1, it is characterised in that: more than one is arranged in the separator, setting
When more than two separators, separator can connect in parallel or series.
26. coal slime processing system described in accordance with the claim 1, it is characterised in that: the reactor is provided 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.
27. coal slime processing system described in accordance with the claim 1, it is characterised in that: separation back-mixing area's inner top setting takes
Hot equipment.
28. coal slime processing system described in accordance with the claim 1, it is characterised in that: heat-accumulation combustion area bottom is provided with row
Cinder notch.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821119697.4U CN208886757U (en) | 2018-07-16 | 2018-07-16 | A kind of coal slime processing system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201821119697.4U CN208886757U (en) | 2018-07-16 | 2018-07-16 | A kind of coal slime processing system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110107890A (en) * | 2019-04-02 | 2019-08-09 | 张正周 | A method of preventing circulating fluidized bed boiler coking |
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2018
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110107890A (en) * | 2019-04-02 | 2019-08-09 | 张正周 | A method of preventing circulating fluidized bed boiler coking |
| CN110107890B (en) * | 2019-04-02 | 2020-06-26 | 淄博齐林贵和热电有限公司 | Method for preventing circulating fluidized bed boiler from coking |
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| CP01 | Change in the name or title of a patent holder |
Address after: 116041 No. 113 Middle Road, Lushunkou District, Dalian City, Liaoning Province Co-patentee after: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. Patentee after: Dalian Yiside Special Intelligent Equipment Co.,Ltd. Address before: 116041 No. 113 Middle Road, Lushunkou District, Dalian City, Liaoning Province Co-patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. Patentee before: Dalian East Refrigeration Equipment Co.,Ltd. |
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| CP01 | Change in the name or title of a patent holder | ||
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Granted publication date: 20190521 |