CN105598035B - A kind of parallel connection fluid bed dry separation device and method - Google Patents
A kind of parallel connection fluid bed dry separation device and method Download PDFInfo
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- CN105598035B CN105598035B CN201610015302.5A CN201610015302A CN105598035B CN 105598035 B CN105598035 B CN 105598035B CN 201610015302 A CN201610015302 A CN 201610015302A CN 105598035 B CN105598035 B CN 105598035B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B07—SEPARATING SOLIDS FROM SOLIDS; SORTING
- B07B—SEPARATING SOLIDS FROM SOLIDS BY SIEVING, SCREENING, SIFTING OR BY USING GAS CURRENTS; SEPARATING BY OTHER DRY METHODS APPLICABLE TO BULK MATERIAL, e.g. LOOSE ARTICLES FIT TO BE HANDLED LIKE BULK MATERIAL
- B07B7/00—Selective separation of solid materials carried by, or dispersed in, gas currents
- B07B7/12—Selective separation of solid materials carried by, or dispersed in, gas currents with pulsating air currents
Abstract
The invention discloses a kind of fluid bed dry separation device in parallel and methods, device is made of fluid bed (main bed, companion's bed) in parallel, main bed is connect with bed bottom through bend pipe, reciprocal transfer for particle is to form particle cycle of oscillation, valve is arranged to control particle transfer rate with bed bottom in discharger after the fluidization air of top discharge converges by the road.The present invention utilizes the particle characteristics structure particle cycle of oscillation for waiting for sorting material first in fluid bed in parallel, the cyclic fluctuation for keeping winner's bed opposite with trend is generated with superficial gas velocity in bed, so that particle to be sorted finally realizes grain sorting in main bed and with Relative sliding movement is generated in bed due to density contrast exclusive or grain size difference.The present invention can avoid realizing the self-oscillation of superficial gas velocity and bed in bed using external vibration equipment, realize grain sorting.
Description
Technical field
The present invention relates to a kind of dry separation device and methods, especially a kind of to be suitable for coal, ore and other materials
Carry out the fluid bed dry separation device in parallel and method of grain sorting.
Background technology
Grain sorting is widely used in derived energy chemical field, the utilization ratio for improving resource.By taking coal as an example, China
High-quality coal resource is few, be unevenly distributed and directly utilize it is seriously polluted, if will in coal constitute ash content mineral and sulphur component removal,
The heat production rate that coal can then be increased, makes boiler combustion stablize, while the abrasion and corrosion for reducing slag amount, reducing boiler.Therefore
Coal separation becomes the key technology means of Optimum utilization coal resource.In addition, in incineration firing field, refuse classification technology is also outstanding
To be important, refuse classification can not only improve garbage utilization efficiency, but also can improve incineration firing efficiency.Traditional wet method point
Choosing is needed using a large amount of water and need to be dehydrated and dried to sorting obtained material, therefore wet-treating consumption resource is more, mistake
Journey is complicated, is particularly unsuitable for the grain sorting processing of drought and water shortage, severe cold frost region.Therefore, have the high efficiency of separation and
The dry sorting technology of economic feasibility is developed into urgent problem to be solved.
Patent CN102921636B discloses a kind of autogenous medium fluid bed dry sorting method, is being shaken using sorting pan feeding
The autogenous medium of fluidized bed middle formation, which is realized, presses density stratification, and material is realized under the synergistic effect of ascending air and exciting force
Constantly sorting bed is discharged in high density material by fluidisation, is overcome difficult using dense media processing, recycling when additional dense medium separation
's.Patent CN1021806202B discloses a kind of vibration fluidized bed sorting machine of air distribution plate, by vibrating air distribution plate by vibrational energy
Amount passes to fluid bed, inhibits the generation of bubbles in fluidized, forms uniform and stable fluidized state, material is in Archimedes's original
Reason acts on lower leaf.But above-mentioned patent uses vibrator that sorting bed or air distribution plate is made to generate periodic swinging, drive mechanism
Complexity results in vibrational energy and destroys bed traditional structure, influences the stability of device structure；In addition vibrational energy needs to drive
Entire bed movement, power consumption is big, and vibrational energy is largely used for non-effective content.
Particle cycle of oscillation phenomenon observes that tracing it to its cause is in recirculating fluidized bed experimental provision for the first time, in descending branch
Particle is in the form of moving bed into raising section transfer process, and when material position is too low, part circulating air will be run up by descending branch,
Gas blowby is formed, and slug flow state is formed in descending branch bottom.On the one hand so that descending branch particle is mutually changed by moving bed
Fluid bed；On the other hand so that the particle in raising section is shifted to descending branch, until descending branch forms moving bed.Thus occur
The phenomenon that particle back and forth shifts between the descending branch of raising section referred to as particle cycle of oscillation phenomenon.Coal, rubbish and mineral grain
General grain size is larger, is easy to be formed to save in a fluidized bed to gush state, therefore can form similar particle between fluid bed in parallel and shake
The phenomenon that swinging cycle so that main bed and superficial gas velocity opposite with occurring trend in bed, cyclic fluctuation, further such that waiting for point
It selects material since density or the difference of grain size generate Relative sliding movement, realizes grain sorting.
Invention content
The purpose of the present invention is the deficiencies for existing sorting technology, and a kind of structure letter is proposed based on particle cycle of oscillation
The new dry process parallel connection fluid bed separation device and method single, low energy consumption.
A kind of fluid bed dry separation device in parallel of the present invention, including main bed and with bed, are located at the fluidisation of main bed bottom
Air intake, for connecting the bend pipe with bed bottom and main bed lower part, positioned at the valve for being used to adjust particle exchange amount with bed bottom
Door is used to add the charging for waiting for sorting material for converging main bed with the pipeline of bed fluidization air be discharged on companion's bed
Mouthful, it is located at the discharge port that lightweight fine grain discharge port and heavy bulky grain are used on main bed.
The link position of the described main bed of connection and bend pipe and main bed with bed is apart from main 0.1~0.3L of bed bottom, based on L
Bed height.
The lightweight fine grained bed that the main bed is formed there are reducer, for stablizing sorting, in favor of thin of lightweight
The discharging of grain, away from main bed with bed 0.1~0.4L of junction, reducing segment length is 0.1~0.5L for reducer initial position.
The lightweight fine grained discharge port position is located at main bed reducer.
The heavy bulky grain discharge port position is less than the height of main bed and bend pipe junction, away from junction vertical range
For 0~0.1L.
The charge door positional distance is with bed height with bed 0.3~0.9H of bottom, H.
Described includes butterfly valve, ball valve, shut-off valve positioned at being used to adjust the valve types of particle exchange amount with bed bottom.
The fluid bed dry sorting method in parallel of described device includes the following steps：
A. the valve with bed bottom is closed, sorting material is waited for bed filling through feed inlet；
B. two discharge ports on main bed are closed, in the state of main bed fluidization air stable operation, are opened with bed bottom
Valve so that shift to main bed with the material in bed, finally in main bed with formation particle cycle of oscillation in bed；
C. from bed feed inlet continuous feed into device, open main bed lower part heavy bulky grain discharge port and on
Portion's lightweight fine grained discharge port, respectively obtains the sorting material of different densities or grain size；
D. it adjusts with the particle transfer rate between bed bottom valve aperture or main bed Fluidising air flow change two, it can
Control the fine grain product quality of lightweight and yield.
Main bed fluidization air superficial gas velocity is more than Particles at Critical fluidizing gas velocity and is less than particle fast fluidized bed in the step b
Rate of transformation, preferably the 1.5~5 of Particles at Critical fluidizing gas velocity times.
Valve opening variation range is 30~100% in told step d.
The present invention utilizes the particle characteristics structure particle cycle of oscillation for waiting for sorting material in fluid bed in parallel so that main bed
The cyclic fluctuation opposite with there is trend with superficial gas velocity in bed realizes table in bed so as to avoid external vibration equipment is used
See the fluctuation of gas velocity.Under the action of cyclic fluctuation gas velocity, particle to be sorted main bed and in bed due to density contrast exclusive or
Grain size difference and generate Relative sliding movement, realize grain sorting.
Description of the drawings
Fig. 1 is the fluid bed dry separation device schematic diagram in parallel of the present invention；In figure：1- heavy bulky grain discharge ports, 2-
Main bed, 3- lightweight fine grained discharge ports, 4- connect main bed and the bend pipe with bed, and 4- valves, for 6- with bed, 7- waits for that sorting material is fed
Mouthful, 8- converges main bed and the pipeline with bed eluting gas.
Fig. 2 is main bed and the fluctuation with superficial gas velocity in bed during grain sorting.
Fig. 3 is the concentration distribution based on bulky grain (a) and little particle (b) after the sorting of particle cycle of oscillation of the present invention.
In Fig. 4 (a), (b), (c) be respectively the present invention based on particle cycle of oscillation sort after gas phase, bulky grain, small
The velocity vector distribution map of grain.
Specific embodiment
One embodiment of the present of invention is further described below in conjunction with the accompanying drawings：
Fluid bed dry separation device in parallel as shown in Figure 1, main bed elbow junction become away from main bed bottom 0.1L, main bed
Away from main bed elbow junction 0.2L, heavy bulky grain unloading position is located at main bed bottom and is connected away from main bed elbow for diameter section initial position
Locate 0.05L, use butterfly valve with bed bottom valve, wait for that sorting material feed entrance point is located at 0.4H, L is main bed height, H is with bed
Highly.
First in the state of being closed with bed bottom butterfly valve filling certain altitude be uniformly mixed grain size be respectively 2.5mm (
1) and the same density granule of 0.5mm (particle 2) grain.Main bed superficial gas velocity is adjusted, so that it is stablized in 1m/s, which is 2.5mm
1.5 times of grain size PP GRANULES minimum fluidizing velocity.It opens with bed bottom valve, makes uniformly mixed two kinds of particles in main bed
Particle cycle of oscillation is formed between companion's bed, so that the cyclic fluctuation gas velocity that main bed is opposite with occurring trend in bed,
Further such that waiting for that sorting material generates Relative sliding movement due to density or the difference of grain size, grain sorting is gradually realized.
The present embodiment simulates the assorting room using Fluent hydrodynamics software, and Fig. 2 is cycle of oscillation process
In in the main bed of cyclic swing with bed superficial gas velocity, main bed is opposite with bed superficial gas velocity fluctuation tendency as shown in Figure 2.In Fig. 3
(a), (b) respectively simulates the concentration profile of particle 1 and particle 2 after obtained cycle of oscillation 30s.From the figure 3, it may be seen that big at this time
Particle concentrates on main bed bottom with inside bend pipe, and fine grained then concentrates on main bed reducer and with bed middle and lower part, thus proves
Fluid bed dry separation device in parallel and method based on cycle of oscillation can realize grain sorting.(a), (b), (c) point in Fig. 4
Obtained corresponding moment gas phase, particle 1,2 velocity vector distribution map of particle Wei not simulated, in Fig. 4 known to (a) at this time gas phase by
It is flowed to bed in pipe bent position part after entering main bed bottom.1 speed vector figure of particle shown in (b) shows that particle 1 exists in Fig. 4
The particle speed very little that the larger region of its concentration has, and have in the minimum main bed reducer of granule density and with bed bottom
Larger speed, and direction is downward, this is because the gas phase drag force suffered by the larger particle 1 of grain size is compared with its own gravity herein
It is smaller, thus accelerate downwards.2 speed vector figure of particle shown in (c) shows larger in its concentration in particle 2 in Fig. 4
There is smaller particle speed at main bed reducing and with bed middle and lower part, and there is larger and upward velocity in main bed lower part and elbow
Vector makes its acceleration move upwards this is because gas phase drag force suffered by little particle is more than particle its own gravity herein.It can thus be appreciated that
There is different movement tendencies under the action of size particles during particle cycle of oscillation are in gas phase drag force and its own gravity, more
Grain sorting easy to implement.
Claims (4)
1. a kind of parallel connection fluid bed dry separation device, it is characterised in that including main bed and with bed, be located at the fluidisation of main bed bottom
Air intake, for connecting the bend pipe with bed bottom and main bed lower part, positioned at the valve for being used to adjust particle exchange amount with bed bottom
Door is used to add the charging for waiting for sorting material for converging main bed with the pipeline of bed fluidization air be discharged on companion's bed
Mouthful, it is located at the discharge port that lightweight fine grain discharge port and heavy bulky grain are used on main bed;
The lightweight fine grained discharge port position is located at main bed reducer；
The heavy bulky grain discharge port position is less than the height of main bed and bend pipe junction, away from junction vertical range for 0 ~
0.1L, L are main bed height；
The gating location distance is with bed height with bed 0.3 ~ 0.9H of bottom, H；
The main bed is there are reducer, and away from main bed with bed 0.1 ~ 0.4L of junction, reducing segment length is for reducer initial position
0.1 ~ 0.5L, L are main bed height.
2. parallel connection fluid bed dry separation device according to claim 1, it is characterised in that：The main bed of the connection and companion
The bend pipe of bed is main bed height apart from main 0.1 ~ 0.3L of bed bottom, L with the link position of main bed.
3. parallel connection fluid bed dry separation device according to claim 1, it is characterised in that：Described is located at bed bottom
Valve types for adjusting particle exchange amount include butterfly valve, ball valve, shut-off valve.
4. a kind of fluid bed dry sorting method in parallel of device as described in claim 1, it is characterised in that：Including following step
Suddenly：
A. the valve with bed bottom is closed, sorting material is waited for bed filling through feed inlet；
B. two discharge ports on main bed are closed, in the state of main bed fluidization air stable operation, open the valve with bed bottom
Door so that shifted to main bed with the material in bed, finally in main bed with formation particle cycle of oscillation in bed；It is main in the step b
Bed fluidization air superficial gas velocity is more than Particles at Critical fluidizing gas velocity and is less than particle fast fluidized bed rate of transformation, main bed fluidization air
Superficial gas velocity is 1.5 ~ 5 times of Particles at Critical fluidizing gas velocity；
C. it from feed inlet continuous feed into device with bed, opens main bed lower part heavy bulky grain discharge port and middle and upper part is light
Matter fine grained discharge port respectively obtains the sorting material of different densities or grain size；
D. it adjusts with the particle transfer rate between bed bottom valve aperture or main bed Fluidising air flow change two, can control
The fine grain product quality of lightweight and yield；Valve opening variation range is 20 ~ 100% in the step d.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201610015302.5A CN105598035B (en) | 2016-01-08 | 2016-01-08 | A kind of parallel connection fluid bed dry separation device and method |
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| CN201610015302.5A CN105598035B (en) | 2016-01-08 | 2016-01-08 | A kind of parallel connection fluid bed dry separation device and method |
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| CN106862077B (en) * | 2017-01-21 | 2018-10-19 | 中国矿业大学 | A kind of coupled system and method for wetted coal fines sorting and drying |
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| JPS5921650B2 (en) * | 1979-11-29 | 1984-05-21 | 東洋エンジニアリング株式会社 | Granulation method |
| CN2229829Y (en) * | 1995-06-14 | 1996-06-26 | 蒋大洲 | Equipment for crystallisation of melamine |
| JPH1019222A (en) * | 1996-06-28 | 1998-01-23 | Mitsubishi Heavy Ind Ltd | Fluidied bed incinerator |
| CN2339296Y (en) * | 1998-09-25 | 1999-09-22 | 清华大学 | Close-phase circulation fluidizing-bed reactor for strong heat-discharging reaction process |
| CN1133844C (en) * | 2000-05-12 | 2004-01-07 | 清华大学 | Method and equipment for separating ash from slags by fluidized bed |
| CN1214857C (en) * | 2002-09-24 | 2005-08-17 | 中国科学院过程工程研究所 | Circulating fluidized bed reactor for ultrafine and sticky particles |
| US10010847B2 (en) * | 2010-11-08 | 2018-07-03 | Ohio State Innovation Foundation | Circulating fluidized bed with moving bed downcomers and gas sealing between reactors |
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