CN1119400C - Fine coal granules and method and apparatus for producing the same - Google Patents
Fine coal granules and method and apparatus for producing the same Download PDFInfo
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- CN1119400C CN1119400C CN 99106591 CN99106591A CN1119400C CN 1119400 C CN1119400 C CN 1119400C CN 99106591 CN99106591 CN 99106591 CN 99106591 A CN99106591 A CN 99106591A CN 1119400 C CN1119400 C CN 1119400C
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Abstract
The present invention relates to a coal variety obtained by separation and a production method and a device thereof. Fine particle coal is a reconstructed coal variety with the granularity of 0.5 to 13mm. In the production method, feed coal is screened to obtain sieved coal, and the fine particle coal is formed by separation; a separation device is a gas separation tower, and a fluidized bed composed of a columnar vertical tower body, a tower wall, grid plate, a discharge tube and an isobaric blast tank, an air inlet, an air outlet, a coal supply opening, a coal dispersing air nozzle, etc. are arranged. The procduction device is a full hermitic pneumatic circulation sorting system which comprises the gas separation tower, a blower, a coal feeder, a separator, a coal unloader, a pipeline and a control valve. The fine particle coal can realize that the coal which enters a furnace is burnt in the mode of full share fluidization, and has the advantages of no pollution, little loss and energy saving.
Description
The present invention relates to a kind of with separating product of coal and production method and the device that obtains.
Existing domestic and international fluidizing furnace all is a kind of particle diameter d≤x with coal
2(mm) wide-size distribution reconstructed coal, wherein x
2Value is that design is selected, and the various places, various countries are not quite similar, but are generally less than 13mm, and China's industry is selected for use and is generally x
2=6～10mm.Contain particle diameter d≤x in the obvious above-mentioned reconstructed coal
1(mm) the coal dust of realizing fluidized combustion in the ebullated bed that can not be stabilized in is considered to be worth doing, wherein x
1Value depends on ebullated bed operating air velocity ω
fAnd temperature t
f, work as t
f＞800 ℃, ω
fDuring 〉=2m/s, x
1≈ 0.5mm; Work as ω
fDuring ≈ 4.5m/s, x
1≈ 1.0mm.The coal dust bits are taken out of ebullated bed and burner hearth rapidly by flue gas, just form the alleged flying dust of industry.The coal dust bits that form the fluidizing furnace flying dust are mainly from 1) natural composition in the raw coal; 2) fuel processing is broken produces; 3) coal grain burning shrinkage forms; 4) coal grain high temperature explosion.Remove the coal of thermostability extreme difference, the flying dust that preceding 3 coal dusts bits generate accounts for about 70% of total flying dust amount.And the flying dust total amount generally accounts for more than 50% of the total grey quality of stove.With layer fuel ratio, fluidizing furnace flying dust amount is very big; With the powder coal stove ratio, fluidizing furnace flying dust median size exceeds an order of magnitude, and fire box temperature is very low, and the flying dust utmost point is difficult to burn.So the flying dust amount is big, flying dust is flammable, and matter content height is fluidizing furnace design and operating biggest obstacle all the time, is the low decisive reason of China's fluidizing furnace thermo-efficiency.Burn a series of technical measures of taking for solving flying dust, make hugeization of body of heater invariably, structure complicated, and effect is unsatisfactory in industrial applications, and limited the Boiling Combustion technology and spread to the large-sized power boiler.Capture in the big burner hearth of high temperature of first-generation fluidized bed combustion boiler, flying dust stove, return that the s-generation fluidizing furnace that develops on the thorax resume combustion technical foundation---circular fluid bed is acknowledged as the high effect cleaning coal combustion technology developing goal of new millennium, its body of heater is tall and big, be furnished with complicated capture of high temperature flying dust and flying dust in the stove and return the stove circulation device, comparatively strict for ature of coal and fuel sieve size proportion requirement, the loading elasticity of high-efficiency operation is very little.10t/h industry boiling boiler body of heater height is more than 10m; The then near 50m of the power stove height of 410t/h level is suitable with the powder coal stove of same level.When ature of coal changes greatly, fineness ratio is unsuitable, when load reduces, causes that fire box temperature descends and causes the invalid vicious cycle of flying dust, and boiler thermal output sharply descends, even less than common fluidizing furnace; Big slightly or break flour ratio increase then causes flying dust to capture when load, and recycle system decrease in efficiency has worsened operating mode.The situation that circulating fluidized bed Industrial Boiler design thermal efficiency falls short of the reality even even more serious than other Industrial Boilers." Industrial Boiler " clauses and subclauses of 1996 " Chinese engineering goods yearbook " are write by former dynamo-electric portion, claim: China's " Industrial Boiler identifies that thermo-efficiency reaches 80%, and actual motion thermo-efficiency is not high ".Though there is a planning eighties in China, target is with 80 years Industrial Boiler thermo-efficiency mean level (ML)s 60%, brings up to 76% to 2000, and year is economized on coal 1.65 hundred million tons, in fact can realize far away.At present, organized the GEF plan again, target is that the thermo-efficiency level improves 10%～15%, and year is economized on coal 6,000 ten thousand tons, is worth 12,000,000,000 yuan.About 500,000 of the existing Industrial Boiler of China, year consumption coal be more than 400,000,000 tons, and it is about 40% to account for the coal aggregate consumption, is first user, also is first source of pollution.In the planned economy age of coal shortage, what the design of Industrial Boiler and manufacturing were carried out is " adapting to many coals with many kinds ", and boiler circle is paid huge effort for this reason.But facts have proved of four more than ten years, only according to working hard in combustion technology and combustion equipment, effect is little, gets half the result with twice the effort.The proterties that changes bunker coal then will be opened up brand-new situation.
Fluidizing furnace is the application of fluidization technology at combustion equipment, is originated in the fifties, the Circulation fluidized-bed furnace of the s-generation occurs to the eighties.They all have a fluidized combustion bed, are commonly called as ebullated bed.Ebullated bed comprises coal gangue to any coal, can realize that high efficiency quick low temperature grills thoroughly to being fluidised fuel pellet in the bed, and efficiency of combustion can reach more than 98%.Low-temperature burning makes its NO
xQuantity discharged is very low and need not to handle, and the low temperature fluidization makes it can realize at low cost that flue gas desulphuization rate reaches more than 90% again, and this is that grate furnace, powder coal stove are incomparable.As everyone knows, the investment of the desulphurization denitration of fine coal power boiler accounts for 20%～30% of thermoelectric power station gross investment, the running cost height, and also denitration technology does not reach a standard so far.Just based on this, the Boiling Combustion mode is acknowledged as the high performance clean burning technology, and various countries competitively develop, and China also classifies Boiling Combustion technology and equipment as the important content of clean coal technology system, write China's Agenda 21, become national environmental protection and energy-conservation strategic problem.
Purpose of the present invention aims to provide Bed for Fine Coal and production method and the device that a kind of particle diameter is 0.2～13mm.
So-called Bed for Fine Coal is that size range is 0.2～13mm, is preferably the reconstructed coal kind of 0.5～8mm.
The production method of Bed for Fine Coal is: 1) the feed coal process is handled, screening obtains the screened coal that granularity is not more than the Bed for Fine Coal granularity upper limit; 2) screened coal that granularity is not more than the Bed for Fine Coal granularity upper limit is through separating, respectively granularity is the Bed for Fine Coal of Bed for Fine Coal size range and less than the coal dust bits of Bed for Fine Coal size range.
The device that separation size is not more than the screened coal of the dry granularity upper limit of particulate is fluidized-bed pneumatic separation tower (is designated hereinafter simply as gas and divides tower), gas divides tower to be provided with the vertically upright tower body of column, fluidized-bed is formed by tower wall, air distribution plate, discharge tube and isobaric bellows in the bottom, discharge tube places the central lower of air distribution plate and passes the bottom of tower body, isobaric bellows place the below of air distribution plate, establish blast inlet and pressure tap at isobaric bellows sidewall, offer clean-out door in isobaric bellows bottom; The top of tower body sets out the air port; Establish coal feeding hole in the tower body upper portion side wall, the coal feeding hole below is provided with the coal spread wind nozzle, is provided with hagioscope at fluidized-bed aspect height; At the tower body sidewall, the top of air distribution plate offers inspection manhole.
The column tower body that stands is generally uniform cross section, tapers such as air distribution plate can be, discharge tube is opened at the bottom of the awl of air distribution plate, coal feeding hole apart from the height of air distribution plate best＞4m, the air outlet of cat head and the spacing of coal feeding hole preferably are no less than 1m, the spacing of coal spread wind nozzle and coal feeding hole is 50mm, and both A/Fs are identical.
The invention provides a kind of Bed for Fine Coal production equipment---totally-enclosed strength circulation separation system, system comprises that gas divides tower, recirculation blower, feeder, separator, Bed for Fine Coal to unload the fortune machine, the coal dust bits unload fortune machine and air circulation loop pipeline and control corresponding valve thereof.Recirculation blower divides the blast inlet of tower to be connected with the coal spread wind nozzle with gas by pipeline respectively with the control corresponding valve, feeder divides the coal feeding hole of tower to be connected with gas, gas divides the air outlet of tower to be connected with the inlet of separator by pipeline, the air outlet of separator is connected with recirculation blower by pipeline, control valve, the coal dust of separator bits discharge port connects the coal dust bits and unloads the fortune machine, and gas divides the discharge tube discharge port of tower to connect Bed for Fine Coal to unload the fortune machine.
Its size range of the said Bed for Fine Coal of the present invention is d=x
1-x
2Mm, wherein lower value x
1=0.2mm, higher limit x
2=13mm, it is a kind of fluidizing furnace (comprising Boiling Combustion stove and fluidized-bed gasification furnace) that is applicable to, can realize the new variety coal of stove coal complete set volume fluidized combustion, it is different from all listed kind coals of standard GB/T 3715-1996 " about coal and products thereof ", for fluidizing furnace, Bed for Fine Coal is a kind of fresh fuel of giving full play to its advantage, it will reduce its flying dust amount about 60%, thermo-efficiency improves more than 15%, economize on coal more than 20%, and realize that boiler keeps the high thermal efficiency operation under low load condition; To expedite the emergence of third generation fluidizing furnace simultaneously, the very simple novel furnace of promptly a kind of low burner hearth, small volume, structure, this also is the target of world's combustion technology circle long-term struggle.The change of fuel character causes the revolution of combustion technology and equipment, and the revolution of combustion technology expedites the emergence of new fuel band, and the dialectical development relation between fuel-fuel technology-combustion equipment is proved conclusively by the combustion technology history.Coal furnace all is such by bulk coal-fired grate furnace, the powder coal stove that burns superfine coal dust and coal water slurry stove to the fluidizing furnace that burns the wide-size distribution reconstructed coal.
The said Bed for Fine Coal production method of the present invention is the very strong industrialized preparing process of a kind of practicality, and its core is fine powder bits realization low cost, high-level efficiency, the granularity of particle diameter d＜(0.2～1.0) mm can not had the sorting of magnitude regulation and control.Obtain the wide-size distribution coal of granularity≤13mm by processing, again through separating, separablely go out granularity＜(coal dust bits of 0.2～1.0mm), promptly get the said new coal kind of the present invention---Bed for Fine Coal, its technological process of production is very simple, especially by closed strength circulation separation system, can realize polluting the industrialization streamline operration little, that efficient is high, equipment is simple, cost is low.
It is simple in structure for the said fluidized-bed pneumatic separation of the present invention tower, and regulation and control are not established screen cloth flexibly, and failure rate is extremely low.Form closed strength circulation separation system if unload fortune machine and air circulation loop connection line and control corresponding valve thereof etc. with recirculation blower, feeder, separator, Bed for Fine Coal and coal dust bits, it is little with loss then to have pollution, can realize automated operation, the production efficiency height, power consumption low (about 0.5KWh/t), invest little, advantage such as running cost is low.Just it not only realizes the automatic industrial production of Bed for Fine Coal, and has dedusting, environmental protection, function such as energy-conservation concurrently.
Fig. 1 is a kind of processing process figure of Bed for Fine Coal
Fig. 2 is a fluidized-bed pneumatic separation tower structure sketch.
Fig. 3 cuts open figure for the B-B of Fig. 2.
Fig. 4 is totally-enclosed strength circulation separation system synoptic diagram.
The new coal kind of the said Bed for Fine Coal of the present invention is that size range is 0.2～13mm, is preferably the reconstructed coal kind of 0.5～8mm.If the Bed for Fine Coal size range is (x
1～x
2) nm.
The production method of Bed for Fine Coal through multi-deck screen A, gets granularity≤x with feed coal respectively as shown in Figure 1 after the screening
2Mm, x
2～25mm and＞the preliminary working coal (screened coal) of 25mm, again with granularity≤x
2The screened coal of mm is through tripping device B, and getting granularity respectively is x
1～x
2The Bed for Fine Coal of mm and granularity＜x
1The coal dust bits of mm, the Bed for Fine Coal of gained is the said new coal kind of the present invention.As for＜x
1The coal dust bits of mm then can be processed as moulded coal or use for him.x
1Value can realize not having the magnitude regulation and control.
Fig. 2,3 provide the structure diagram that gas of the present invention divides tower, and tower body 1 is the column that stands of square sectional, and the bottom is provided with the fluidized-bed of being made up of tower wall, air distribution plate 2, discharge tube 3 and isobaric bellows 4, and wherein air distribution plate 2 adopts the porous plate design.Be tapered shape, the level inclination of the conical surface is got 15～20 °; Discharge tube 3 is located at the bottom of the awl of air distribution plate and is passed the tower body bottom vertically downward; Isobaric bellows 4 are established blast inlet 11 and pressure tap P at sidewall between at the bottom of air distribution plate and the tower, offer the clean-out door 9 of about 300mm * 300mm in the bottom.Establish coal feeding hole 5 in tower body 1 upper portion side wall, coal feeding hole 5 is apart from the about 4m of air distribution plate, and the tower body top sets out air port 6, the distance 〉=1m of coal feeding hole and air outlet, and coal feeding hole below is provided with coal spread wind nozzle 7, the about 50mm of clear spacing between the two, A/F is identical.At fluidized-bed aspect height transparent hagioscope 8 is housed, its size can be height * wide=500mm * 100mm.Establish inspection manhole 10 above tower body sidewall, air distribution plate, inspection manhole 10 is apart from the about 0.5m of air distribution plate.As needs control x
2During value, also can offer the regulatable canopy shape of overflow height overflow port at sidewall.
Fig. 4 provides application gas and divides tower to carry out isolating totally-enclosed strength circulation separation system synoptic diagram.This system is unloaded by recirculation blower 12, feeder 13, primary separator 14, second-stage separator 15, Bed for Fine Coal that fortune machine 16, coal dust bits unload fortune machine 17, air circulation loop pipeline and control corresponding valve 18 thereof, 19 gentle minutes towers 20 are formed.Wherein recirculation blower 12 divides the air outlet 151 of blast inlet 11, coal spread wind nozzle 7 and the second-stage separator 15 of tower 20 to be connected with gas by pipeline respectively with control valve, the air quantity of recirculation blower divides tower fluidization design given by gas, and total head is fallen sum by systemic resistance and determined; Granularity＜x
2The wide-size distribution reconstructed coal of (higher limit) divides the coal feeding hole 5 of tower 20 evenly to go into tower continuously by feeder 13 by gas, under the effect of horizontal coal spread wind, coal disperses, and is reverse and go with the upstream that divides the tower fluidized-bed through gas, takes place just to fall into fluidized-bed after the separation, coal grain fluidisation in fluidized-bed, produce intensive between particle and seethe friction, gas bubbling, bubble a large amount of, intensive, rapid rising the bed surface of constantly the coal grain being dished out, under the control of operating air velocity, d≤x
1The break flour of (lower value) rises with air-flow, is discharged outside the tower by air outlet 6, and Bed for Fine Coal is then keeping under the fluidized layer height condition that needs, and is evenly discharged continuously by discharge tube 3, and unloads fortune machine 16 by Bed for Fine Coal and collect.Move air quantity with control Bed for Fine Coal lower value x by regulation and control
1, by regulating the average retention time of fluidized layer height control coal, to reach design requirements d＜x at fluidized-bed
1Separation rate.It all should be stepless speed regulation that feeder and Bed for Fine Coal are unloaded the fortune machine, with the material balance of Controlling System.Can select worm conveyor, conveyor, bucket elevator, rotary disc feeder etc. for use.
Divide the coal dust bits of tower air outlet 6 discharges to cross pipeline with air communication by gas and enter separator, separator preferably is no less than 2 grades, Zong separation rate should be in operation greater than 98%, the powder content in the fluidizing medium can reach trim point automatically, does not influence system works.Primary separator can adopt inertial separator, and is simple in structure, and separation rate is generally greater than 50%; Separator reaching or above grade two can be selected the series product of centicell unit for use, and dust removal efficiency should be not less than 98%.Present embodiment adopts the two-stage separator: primary separator 14 and second-stage separator 15, it is definite that the operation air quantity of separator divides the tower fluidization to calculate by gas.The coal dust bits of separator gained unload fortune machine 17 by the coal dust bits and collect.
For example, set device throughput D=60t/h, lower limit of separation value x
1=0.5～1.0mm, raw coal size d≤8mm, full moisture content Mt＜9%, ambient operating temperature T=20 ℃.Get through size analysis: break flour weight quota ratio beta=35% of d＜1mm, d＞1mm Bed for Fine Coal mean diameter d=2.5mm, shape factor
c=0.65.After measured, the true specific gravity Y of coal
0=1700Kg/m
3, d=1～8mm Bed for Fine Coal bulk density r=1000Kg/m
3, then it piles up voidage ε=0.412.In the fluidized-bed design, fluidization calculates the air conveying speed omega of d=0.5mm coal grain
1=2.12m/s, and the air conveying speed omega of d=1.0mm coal grain
2=4.05m/s, fluidized-bed critical fluidization velocity ω
0=0.64m/s is because ω
1＞ω
0So, but fluidized-bed steady running.The working flow rate ω of fluidized-bed is: get ω
Min=2m/s, the aperture wind speed control number during as the minimum operation of air distribution plate eye of wind air quantity is got minimum eye of wind wind speed ω '=12m/s; Get ω
Max=1.25 ω
2=5m/s is as recirculation blower air quantity parameter.
Air distribution plate area i.e. gas divides the tower cross-sectional area can connect following method to determine: the preliminary election Bed for Fine Coal is mean residence time n=15s in fluidized-bed, and then the static bed of material quantity of fluidized-bed B=n * D=2.55Kg (is 0.255m
3).Choosing fluidized-bed bed of material static height h is 0.2m, then the horizontal area F=B/h=1.275m of air distribution plate
2If select the square sectional tower for use, then the length of side is 1130mm in the cross section of tower.Four sides taper such as air distribution plate employing, conical surface level inclination is got 12 °.Choose minimum operation air quantity Q
Min=9180m
3/ h, air distribution plate aperture perforate total area f=0.2125m
2Maximum operation air quantity Q
Max=22950m
3/ h, coal spread wind amount Q
1=0.05Q, nozzle wind speed ω
3=2 ω.
Feeder, unload the load of fortune machine and separator, the insider then can be supporting according to above-mentioned data.
Obviously, the native system technology is reliable, and operation troubles is few, reduced investment, and working cost is low, and system has dedusting function concurrently, and is pollution-free, loss is little, coal realized the principle of optimality of " the excellent usefulness of high-quality, low-quality is suitable for ".
When feed coal moisture content is bigger, when being unfavorable for that the break flour strength is separated, then can put calandria heat exchanger at the fluidized-bed lining, realization is dry to separate synchronization job with strength; Also can adopt warm air flow process, realization drying to separate synchronization job with strength.But this moment, it is open that system should be, and promptly fluidizing medium enters atmosphere behind the separation and collection break flour.
Claims (7)
1, a kind of fluidized-bed pneumatic separation tower of production Bed for Fine Coal, it is characterized in that being provided with the column tower body that stands, fluidized-bed is formed by tower wall, air distribution plate, discharge tube and isobaric bellows in the bottom, discharge tube places the central lower of air distribution plate and passes the tower body bottom, isobaric bellows place the below of air distribution plate, establish blast inlet and pressure tap at isobaric bellows sidewall, offer clean-out door in isobaric bellows bottom; The top of tower body sets out the air port, establishes coal feeding hole in the tower body upper portion side wall, is provided with the coal spread wind nozzle below coal feeding hole; Be provided with hagioscope at fluidized-bed aspect height; Above tower body sidewall, air distribution plate, offer inspection manhole.
2, fluidized-bed pneumatic separation tower as claimed in claim 1 is characterized in that tower body is a uniform cross section, and air distribution plate such as is at taper, and discharge tube is opened at the bottom of the awl of air distribution plate.
3, fluidized-bed pneumatic separation tower as claimed in claim 2 is characterized in that tower body is a square equal cross-section, and air distribution plate such as is at the four sides taper, and the level inclination of the conical surface is 15～20 °, and air distribution plate adopts porous plate.
4, fluidized-bed pneumatic separation tower as claimed in claim 1 is characterized in that the distance of coal feeding hole and air outlet is not less than 1m more than the coal feeding hole square air distribution plate 4m.
5, a kind of totally-enclosed strength circulation separation system of production Bed for Fine Coal, it is characterized in that this system comprises the said fluidized-bed pneumatic separation of claim 1 tower, recirculation blower, feeder, separator, Bed for Fine Coal is unloaded the fortune machine, the coal dust bits unload fortune machine and air circulation loop pipeline and control corresponding valve thereof, recirculation blower is connected with the coal spread wind nozzle with the blast inlet of fluidized-bed pneumatic separation tower respectively with the control corresponding valve by pipeline, feeder is connected with the coal feeding hole of fluidized-bed pneumatic separation tower, the air outlet of fluidized-bed pneumatic separation tower is connected with the inlet of separator by pipeline, the air outlet of separator passes through pipeline, control valve is connected with the recirculation blower import, the coal dust bits discharge port of separator connects the coal dust bits and unloads the fortune machine, and the discharge tube discharge port of fluidized-bed pneumatic separation tower connects Bed for Fine Coal and unloads the fortune machine.
6, totally-enclosed strength circulation separation system as claimed in claim 5 is characterized in that said separator is no less than 2 grades.
7, totally-enclosed strength circulation separation system as claimed in claim 6 is characterized in that primary separator adopts inertial separator, and separator reaching or above grade two is selected centicell unit for use.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 99106591 CN1119400C (en) | 1999-05-10 | 1999-05-10 | Fine coal granules and method and apparatus for producing the same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 99106591 CN1119400C (en) | 1999-05-10 | 1999-05-10 | Fine coal granules and method and apparatus for producing the same |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 98121510 Division CN1250079A (en) | 1998-10-07 | 1998-10-07 | High-efficiency and low-pollution fuel coal and its making process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1235187A CN1235187A (en) | 1999-11-17 |
| CN1119400C true CN1119400C (en) | 2003-08-27 |
Family
ID=5272449
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 99106591 Expired - Fee Related CN1119400C (en) | 1999-05-10 | 1999-05-10 | Fine coal granules and method and apparatus for producing the same |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1119400C (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102784757B (en) * | 2012-07-27 | 2014-05-07 | 安徽理工大学 | Efficient airflow classification fine-coal remover for power coal before selecting |
| CN103666503B (en) * | 2012-09-04 | 2016-03-30 | 中国科学院工程热物理研究所 | External-heat solid carbonic material method for pyrolysis and pyrolysis system |
| CN110787999A (en) * | 2019-11-04 | 2020-02-14 | 中冶长天国际工程有限责任公司 | Winnowing removal device for fine particle dust in lime kiln, control method and lime kiln |
| CN110788000A (en) * | 2019-11-04 | 2020-02-14 | 中冶长天国际工程有限责任公司 | Winnowing removal device for fine particle dust in lime kiln, control method and lime kiln |
| CN111804567B (en) * | 2020-06-08 | 2022-08-30 | 新兴铸管股份有限公司 | Process for filtering superfine active coke powder |
-
1999
- 1999-05-10 CN CN 99106591 patent/CN1119400C/en not_active Expired - Fee Related
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|---|---|
| CN1235187A (en) | 1999-11-17 |
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