CN102766476B - Multi-layer upright tower type duff dust and oil shale distillation plant with stirring function and process - Google Patents
Multi-layer upright tower type duff dust and oil shale distillation plant with stirring function and process Download PDFInfo
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Abstract
The invention discloses a multi-layer upright tower type duff dust and oil shale distillation plant with a stirring function and a process, and relates to a small-particle size solid fuel distillation device. An inner barrel is arranged at the inner side of an outer barrel; a sealing subassembly is arranged at the top end of the outer barrel; a stirring motor is connected with the upper part of the sealing subassembly through a stirring shaft; a sealed feeding tube is arranged at the bottom end of the outer barrel; a stirring supporter is arranged above the sealed feeding tube; a water spraying tube is arranged above the stirring supporter; a lower tube plate is arranged above the water spraying tube; an upper tube plate is arranged below the lower tube plate; a heat tube is arranged between the lower tube plate and the upper tube plate; a I-type hole material disc is arranged above the upper tube plate, and a II-type hole material disc is arranged above the I-type hole material disc. The distillation of small-particle size solid fuel is achieved; a multi-layer upright tower is adopted; the moisture generated by drying can be independently discharged when the material with high water content is dried; thermal load for gas treatment is reduced; gradual stirring is adopted, so that the heat transfer efficiency is high; and the heat utilization efficiency is improved, and the distillation time is shortened.
Description
Technical field:
The present invention relates to a kind of small particle size solid fuel destructive distillation device, be specifically related to the upright tower smalls of a kind of multilayer with stirring, oil shale distillation production equipment and technique.
Background technology:
Existing coal, resinous shale low-temperature pyrolysis technique is mainly the block raw material that is greater than 13mm for particle diameter, adopt carbonization gas and air to burn in the tunnel of gas retort, with the direct destructive distillation of hot gas of burning, final carbonization gas is owing to having mixed combustion tail gas, active principle content in carbonization gas is reduced, can utility value lower, in this course, carbonization gas and burning gas must be by destructive distillation layers, so, the raw material layer of destructive distillation must have space, so that the gas in stove is discharged, the solid high temperature that destructive distillation is complete, in the time going downwards to plug for outlet, must adopt quenching that the solid temperature of destructive distillation is reduced, general wet quenching and the dry gas of adopting, steam quenching, the heat of quenching accounts for sizable ratio in whole destructive distillation engineering, this part heat of high temperature is wasted, cause the heat utilization rate of destructive distillation low.
Coal, resinous shale that particle diameter is less are derived space because cannot form gas in traditional gas retort, and cannot adopt this technique, and therefore coal sifts out smalls less particle diameter and undersells in the time producing blue charcoal, and smalls is not utilized well.
In oil shale distillation process, be too particle diameter is less than to about 10mm carry out landfill disposal as waste material.
For destructive distillation, many achievements in research show, under the same conditions, particle diameter is less, in overhead product, the productive rate of oil is higher, particle is larger, in overhead product oil productive rate productive rate lower, gas higher, this be because, destructive distillation raw material particle size is larger, the volatile matter time is from the inside to surface longer, and contact high-temperature time is longer, and the decomposition of overhead product is just more.Therefore, the raw material of small particle size has obvious effect for the productive rate that improves oil in overhead product.
In traditional distillation process, the solid after destructive distillation is generally coal tar, the not shale of oil-containing, but the shale of carbon containing, particularly destructive distillation both, if directly discharged, carbon residue just goes out of use, and the utilization ratio of the energy is lower.In this technique, the high temperature resistates that destructive distillation finishes can be by the air of preheating, make the carbon residue burning in shale produce heat, also a part of coal tar can burn, for destructive distillation heat is provided, to reduce carbonization gas consumption, as product or there is other chemical industry purposes factory, there are important economic interests for carbonization gas.
Summary of the invention:
The object of this invention is to provide the upright tower smalls of a kind of multilayer with stirring, oil shale distillation production equipment, it has been realized the solid-fuelled destructive distillation of small particle size, adopt multi-layer type tower, when dry moisture high material, dry moisture can be discharged separately, reduce the thermal load of gas processing, and its heat tunnel and destructive distillation chamber are divided and are arranged, reduce aftertreatment tolerance, finishing apparatus investment is reduced, it adopts successively and stirs, heat transfer efficiency is high, improve heat utilization efficiency, reduce pyrolytic decomposition, improve oil, the productive rate of tar, shorten the destructive distillation time.
In order to solve the existing problem of background technology, the present invention takes following technical scheme: it comprises sealing tremie pipe 1, stir and support 2, water sprayer tube 3, heat pipe stationary barrier 4, I type charging tray 5 with holes, II type charging tray 6 with holes, warm-air pipe 7, chuck air bound plate 8, agitating arm 9, stir guide rail tray 10, guide assembly 11, II plate-type stirs 12, I plate-type stirs 13, stir axle sleeve 14, II type rake stirs 15, interlayer board 16, I type rake stirs 17, sealing feed-pipe 18, stir shaft 19, agitator motor 20, seal assembly 21, gas gathering manifold 22, I type sealing charging tray 23, II type sealing charging tray 24, interlayer effuser 25, thermal insulation layer 26, material pipe 27 falls in the sealing of I type, manhole 28, material pipe 29 falls in II type, upper tubesheet 30, heat pipe 31, lower tubesheet 32, inner barrel 33 and outer cylinder body 34, the inner side of outer cylinder body 34 is provided with inner barrel 33, the top of outer cylinder body 34 is provided with seal assembly 21, the top of seal assembly 21 is connected with agitator motor 20 by stir shaft 19, the bottom of outer cylinder body 34 is provided with sealing tremie pipe 1, the top of sealing tremie pipe 1 is provided with to stir supports 2, the top of stirring support 2 is provided with water sprayer tube 3, the top of water sprayer tube 3 is provided with lower tubesheet 32, the below of lower tubesheet 32 is provided with upper tubesheet 30, between lower tubesheet 32 and upper tubesheet 30, be provided with heat pipe 31, the top of upper tubesheet 30 is provided with I type charging tray 5 with holes, the top of I type charging tray 5 with holes is provided with II type charging tray 6 with holes, below one side of I type charging tray 5 with holes is provided with II type and falls material pipe 29, the top of II type charging tray 6 with holes, on the outer side wall of inner barrel 33, be provided with manhole 28, the top of manhole 28 is provided with the sealing of I type and falls material pipe 27, the top of material pipe 27 falls in the sealing of I type, on the outer side wall of inner barrel 33, each zone of heating is respectively equipped with warm-air pipe 7, the top of warm-air pipe 7 is provided with chuck air bound plate 8, the inner side of inner barrel 33 is provided with several stirring guide rail trays 10, the top of stirring guide rail tray 10 is provided with guide assembly 11, the top of chuck air bound plate 8, on the outer side wall of outer cylinder body 34, be provided with thermal insulation layer 26, on stir shaft 19, be provided with agitating arm 9, in tower, be provided with II plate-type and stir 12, II plate-type stirs a side-lower of 12, on the outer wall of outer cylinder body 34, be connected with gas gathering manifold 22 by interlayer effuser 25, the top of II plate-type stirring 12 is provided with I plate-type and stirs 13, the top of I plate-type stirring 13 is provided with stirs axle sleeve 14, the top of stirring axle sleeve 14 is provided with II type sealing charging tray 24, the top of II type sealing charging tray 24 is provided with II type rake and stirs 15, the top of II type rake stirring 15 is provided with interlayer board 16, the top of interlayer board 16 is provided with I type sealing charging tray 23, the top of I type sealing charging tray 23 is provided with I type rake and stirs 17, the top of I type rake stirring 17 is provided with sealing feed-pipe 18.
Technical process of the present invention is: the solid material of 1, choosing coal that particle is less than 25mm, resinous shale and other and can produce volatile matter in heat-processed; 2, raw material adds by sealing from top of tower, at the first layer, raw material is imported to above stirring by the feed-pipe at edge or center, by the grid distributor on stirring, raw material is advanced to the tremie pipe direction of this layer, drops to one deck from tremie pipe.On adjacent destructive distillation layer, the flow direction of raw material is contrary, is arranged on falling material pipe and can being arranged to as required sealing and falling material pipe of center, the falling material pipe and also can be arranged to as required sealing material pipe of outside.Stir and transfer the raw material of shutoff tremie pipe to whole aspect, each layer of feed distribution is even; 3, first raw material enters preheating section, and the hot gas flow that utilizes retort section to rise from hot gas path carries out indirect preheating to the raw material entering in tower; 4, raw material moves up into retort section under after preheating section preheats, by with hot gas path in hot flue gas indirect heat exchange, temperature improves gradually, operating temperature is controlled at 350-950 DEG C, working time, the coal gas of generation entered gas main from each layer of gas flue at 30-360 minute; 5, the material that destructive distillation finishes enters burning zone, and in this section, the air entering is by the destructive distillation resistates burning of aperture and carbon containing, for the destructive distillation layer of epimere provides heat; 6, under raw material, move up into after cooling section, the solid of destructive distillation is cooled by circulating flue gas, the solid adverse current of flue gas and destructive distillation, progressively heated, pyrolyzate, by progressively cooling, is further lowered the temperature to air cooling layer under destructive distillation solid, equally, freezing air and pyrolyzate adverse current are progressively heated, and heated air and carbonization gas burn in burner, provide destructive distillation required heat energy; 7, consider that the raw material particle size of institute's destructive distillation is little, dry small particle size destructive distillation solid may produce dust in the time of discharging, bottom can be according to feed states, establishes water spraying cooling layer.If destructive distillation material temperature out is low, dust is little, can not establish this layer; 8, in whole retort section, destructive distillation chamber and heating chamber are isolated completely, and heat air is made different passages leave with rage from destructive distillation; 9, in retort process, by regulating air, the carbonization gas of purification, amount of circulating gas control institute heat requirement, each layer of destructive distillation institute heat requirement number regulated by the amount of heat air.Even if not independent peripheral supplemental heat source, also can provide the heat that requires according to destructive distillation by the heat storage of heating chamber; 10, the destructive distillation temperature of the discharging of the coke is 20-150 DEG C, and the temperature out of carbonization gas is 60-250 DEG C.
The present invention has following beneficial effect: it has been realized the solid-fuelled destructive distillation of small particle size, adopts multi-layer type tower, when dry moisture high material, dry moisture can be discharged separately, reduce the thermal load of gas processing, and its heat tunnel and destructive distillation chamber are divided and be arranged, reduce aftertreatment tolerance, finishing apparatus investment is reduced, and it adopts successively and stirs, and heat transfer efficiency is high, improve heat utilization efficiency, reduce pyrolytic decomposition, improved productive rate oily, tar, shortened the destructive distillation time.
Brief description of the drawings:
Fig. 1 is structural representation of the present invention;
Fig. 2 is the structural representation of embodiment 1 in the present invention;
Fig. 3 is the structural representation of embodiment 2 in the present invention;
Fig. 4 is the structural representation of embodiment 3 in the present invention.
Embodiment:
With reference to Fig. 1-4, this embodiment is taked following technical scheme: it comprises sealing tremie pipe 1, stir and support 2, water sprayer tube 3, heat pipe stationary barrier 4, I type charging tray 5 with holes, II type charging tray 6 with holes, warm-air pipe 7, chuck air bound plate 8, agitating arm 9, stir guide rail tray 10, guide assembly 11, II plate-type stirs 12, I plate-type stirs 13, stir axle sleeve 14, II type rake stirs 15, interlayer board 16, I type rake stirs 17, sealing feed-pipe 18, stir shaft 19, agitator motor 20, seal assembly 21, gas gathering manifold 22, I type sealing charging tray 23, II type sealing charging tray 24, interlayer effuser 25, thermal insulation layer 26, material pipe 27 falls in the sealing of I type, manhole 28, material pipe 29 falls in II type, upper tubesheet 30, heat pipe 31, lower tubesheet 32, inner barrel 33 and outer cylinder body 34, the inner side of outer cylinder body 34 is provided with inner barrel 33, the top of outer cylinder body 34 is provided with seal assembly 21, the top of seal assembly 21 is connected with agitator motor 20 by stir shaft 19, the bottom of outer cylinder body 34 is provided with sealing tremie pipe 1, the top of sealing tremie pipe 1 is provided with to stir supports 2, the top of stirring support 2 is provided with water sprayer tube 3, the top of water sprayer tube 3 is provided with lower tubesheet 32, the below of lower tubesheet 32 is provided with upper tubesheet 30, between lower tubesheet 32 and upper tubesheet 30, be provided with heat pipe 31, the top of upper tubesheet 30 is provided with I type charging tray 5 with holes, the top of I type charging tray 5 with holes is provided with II type charging tray 6 with holes, below one side of I type charging tray 5 with holes is provided with II type and falls material pipe 29, the top of II type charging tray 6 with holes, on the outer side wall of inner barrel 33, be provided with manhole 28, the top of manhole 28 is provided with the sealing of I type and falls material pipe 27, the top of material pipe 27 falls in the sealing of I type, on the outer side wall of inner barrel 33, each zone of heating is respectively equipped with warm-air pipe 7, the top of warm-air pipe 7 is provided with chuck air bound plate 8, the inner side of inner barrel 33 is provided with several stirring guide rail trays 10, the top of stirring guide rail tray 10 is provided with guide assembly 11, the top of chuck air bound plate 8, on the outer side wall of outer cylinder body 34, be provided with thermal insulation layer 26, on stir shaft 19, be provided with agitating arm 9, in tower, be provided with II plate-type and stir 12, II plate-type stirs a side-lower of 12, on the outer wall of outer cylinder body 34, be connected with gas gathering manifold 22 by interlayer effuser 25, the top of II plate-type stirring 12 is provided with I plate-type and stirs 13, the top of I plate-type stirring 13 is provided with stirs axle sleeve 14, the top of stirring axle sleeve 14 is provided with II type sealing charging tray 24, the top of II type sealing charging tray 24 is provided with II type rake and stirs 15, the top of II type rake stirring 15 is provided with interlayer board 16, the top of interlayer board 16 is provided with I type sealing charging tray 23, the top of I type sealing charging tray 23 is provided with I type rake and stirs 17, the top of I type rake stirring 17 is provided with sealing feed-pipe 18.
The technical process of this embodiment is: the solid material of 1, choosing coal that particle is less than 25mm, resinous shale and other and can produce volatile matter in heat-processed; 2, raw material adds by sealing from top of tower, at the first layer, raw material is imported to above stirring by the feed-pipe at edge or center, by the grid distributor on stirring, raw material is advanced to the tremie pipe direction of this layer, drops to one deck from tremie pipe.On adjacent destructive distillation layer, the flow direction of raw material is contrary, and the material passage that falls between each layer has raw material from top to bottom to seal at tremie pipe all the time, transfers the raw material of tremie pipe to whole aspect by stirring, and each layer of feed distribution is even; 3, first raw material enters preheating section, and the hot gas flow that utilizes retort section to rise from hot gas path carries out indirect preheating to the raw material entering in tower; 4, raw material moves up into retort section under after preheating section preheats, by with hot gas path in hot flue gas indirect heat exchange, temperature improves gradually, operating temperature is controlled at 350-950 DEG C, working time, the coal gas of generation entered gas main from each layer of gas flue at 30-360 minute; 5, the material that destructive distillation finishes enters burning zone, and in this section, the air entering is by the destructive distillation resistates burning of aperture and carbon containing, for the destructive distillation layer of epimere provides heat; 6, under raw material, move up into after cooling section, the solid of destructive distillation is cooled by circulating flue gas, the solid adverse current of flue gas and destructive distillation, progressively heated, pyrolyzate, by progressively cooling, is further lowered the temperature to air cooling layer under destructive distillation solid, equally, freezing air and pyrolyzate adverse current are progressively heated, and heated air and carbonization gas burn in burner, provide destructive distillation required heat energy; 7, consider that the raw material particle size of institute's destructive distillation is little, dry small particle size destructive distillation solid may produce dust in the time of discharging, bottom can be according to feed states, establishes water spraying cooling layer.If destructive distillation material temperature out is low, dust is little, can not establish this layer; 8, in whole retort section, destructive distillation chamber and heating chamber are isolated completely, and heat air is made different passages leave with rage from destructive distillation; 9, in retort process, by regulating air, the carbonization gas of purification, amount of circulating gas control institute heat requirement, each layer of destructive distillation institute heat requirement number regulated by the amount of heat air.Even if not independent peripheral supplemental heat source, also can provide the heat that requires according to destructive distillation by the heat storage of heating chamber; 10, the destructive distillation temperature of the discharging of the coke is 20-150 DEG C, and the temperature out of carbonization gas is 60-250 DEG C.
This embodiment has realized the solid-fuelled destructive distillation of small particle size, adopts multi-layer type tower, when dry moisture high material, dry moisture can be discharged separately, reduce the thermal load of gas processing, and its heat tunnel and destructive distillation chamber are divided and be arranged, reduce aftertreatment tolerance, finishing apparatus investment is reduced, and it adopts successively and stirs, and heat transfer efficiency is high, improve heat utilization efficiency, reduce pyrolytic decomposition, improved productive rate oily, tar, shortened the destructive distillation time.
In the present invention, according to the difference of pyrolyzate, this device is changed or is reconfigured and all belongs in protection scope of the present invention.
Embodiment 1: choose particle diameter < 13mm, total water (MT): 10%, volatile matter (Vad): 35%, the long bituminous coal smalls that caking index is 3, adopts Fig. 2 technical process.
Smalls enters in tower from sealing feed-pipe 18, stir on axle sleeve 14 and establish three agitating arms 9, high temperature resistant and wear-resisting material group sheet is installed on agitating arm 9, upper strata is I type sealing charging tray 23, being convenient to coal ecto-entad advances, fall material pipe 27 in the sealing of the I of this layer type and be arranged to tubular, the upper end of pipe is concordant with destructive distillation aspect, lower end is through zone of heating B, a destructive distillation on above zone of heating B being, drying layer A, establish successively heat resistant and wear resistant layer, sheet-metal layers, below is provided with the interlayer board 16 with lower floor's destructive distillation layer, there are heat-storing material or heating tube in heating chamber B inside, for example thermal storage ceramic, mix hot gas 7. by the carbonization gas purifying and air combustion, 5. burning gas imports and enters from channel C from i, mixing hot gas is 7. mixed into, coal is by sealing material feeder, enter into the first layer of gas retort, stir 17 by I type rake smalls is fallen to 27 propellings of material pipe to the I type sealing at center, fall into next dry, destructive distillation layer A, stir 15 by II type rake and will expect that therefrom mind-set outer ring advances, until fall into II type, material pipe 29 falls, in progradation, coal seam is heated by zone of heating B below, carbonization gas is by the upper space that is discharged into destructive distillation layer in the smalls being heated, concentrate and be expelled to gas gathering manifold 22 from interlayer effuser 25, also can Sprayer Circulation ammoniacal liquor in gas gathering manifold 22, make gas cooling, the destructive distillation time is 45-90min, and burning gas 5. temperature is 500-750 DEG C, enters from e, and after the gas burning with lower floor mixes, regulating the temperature of heating chamber B is 560 DEG C, dry, retort section is established 13 layers from top to bottom, and drying layer is 1,2 layer, and the temperature in coal seam is from normal temperature to 105 DEG C, and every layer of temperature difference is 50 DEG C of left and right, and destructive distillation layer A is from the 3rd layer, and temperature progressively improves from 105-550 DEG C, the mixing hot gas of destructive distillation heating 7. from j discharge become circulation gas 6., the useless flue gas of part discharge 9., the temperature of discharge flue gas is 150 DEG C, at burning zone
in heating chamber B, not establishing heat storage, is dead level, and this layer is plate with holes, and the air of preheating is 4. through orifice plate, with the upper red-hot coal combustion of A, for gas retort provides part heat.Hot gas passes through tower internal layer above A, from the sandwich passage C of tower to upper strata; ?
section, all bearing material layers with
section is the same, is flaggy with holes, and 6. circulating flue gas is entered by k, and through hot coal seam, temperature is raised to 400-500 DEG C by 150 DEG C, and the temperature of burnt foam drops to 160 DEG C by 150; ?
section, 4. air enters by 1, in the dividing plate of heat pipe layer, come and go through, the temperature of burnt foam is dropped to 60-80 DEG C from 160 DEG C, freezing air is heated to 140 DEG C by normal temperature, from b outlet, arrives roasting kiln and d; ?
section, sprays into water, makes temperature drop to 50 DEG C by 80 DEG C, makes the moisture of burnt foam be increased to 5% simultaneously, the water vapor of spray water and hot burnt foam generation
discharged by a, burnt foam 2 is by the discharging of sealed discharging device; In standpipe layer, be provided with stirring sleeve, stir to facilitate to install, in tower, the pressure of destructive distillation chamber is-300-500Pa, the semicoke of this explained hereafter, it is 1.67 tons that burnt foam per ton consumes smalls, and adopting already known processes to reclaim tar is 100kg, and coal gas is 350Nm
3, caloric power of gas is greater than 4000kcal/Nm
3.
Embodiment 2: choose particle diameter < 13mm, total water (MT): 45%, volatile matter (Vad): 43% brown coal smalls, adopts Fig. 3 technical process.
For the high smalls of water content, the moisture content amount being dried out is larger, effuser independently arranges, to reduce the processing load in carbonization gas later stage, and 1,2,3 layer of top of tower, as drying layer, the moisture content at dry place removes to reclaim heat and water, and destructive distillation layer A is from the 4th layer, and temperature progressively improves from 105-550 DEG C, drying layer and destructive distillation interlayer are implemented isolation by the sealing of falling in material pipe, and other technique is with embodiment 1.
Embodiment 3: choose particle diameter < 10mm, moisture: 1.2%, ash content 72.8%, volatile matter: 16%%, the resinous shale of oil-containing 10%, adopts Fig. 3 or Fig. 4 technical process.
Full tower destructive distillation layer
section is 11 layers, burning zone
for 3-6 layer, cooling section
be 3 layers, spraying cooling section
be 1 layer,
section pyrolysis temperature successively improves from normal temperature to 550 DEG C, and destructive distillation goes out the more than 95% of total oil, and the oil that destructive distillation does not go out and volatile matter, carbon residue enter burning zone, and by the carbon residue burning of the 95-98% in shale, for gas retort provides heat, distillation process is similar to Example 1; Destructive distillation time 30-60min, the resinous shale generation shale oil per ton 95kg of destructive distillation, carbonization gas 150Nm3, calorific value 4500kcal/Nm3.
Claims (2)
1. the upright tower smalls of multilayer that band stirs, oil shale distillation production equipment, it is characterized in that it comprises sealing tremie pipe (1), stir and support (2), water sprayer tube (3), heat pipe stationary barrier (4), I type charging tray with holes (5), II type charging tray with holes (6), warm-air pipe (7), chuck air bound plate (8), agitating arm (9), stir guide rail tray (10), guide assembly (11), II plate-type stirs (12), I plate-type stirs (13), stir axle sleeve (14), II type rake stirs (15), interlayer board (16), I type rake stirs (17), sealing feed-pipe (18), stir shaft (19), agitator motor (20), seal assembly (21), gas gathering manifold (22), I type sealing charging tray (23), II type sealing charging tray (24), interlayer effuser (25), thermal insulation layer (26), material pipe (27) falls in the sealing of I type, manhole (28), material pipe (29) falls in II type, upper tubesheet (30), heat pipe (31), lower tubesheet (32), inner barrel (33) and outer cylinder body (34), the inner side of outer cylinder body (34) is provided with inner barrel (33), the top of outer cylinder body (34) is provided with seal assembly (21), the top of seal assembly (21) is connected with agitator motor (20) by stir shaft (19), the bottom of outer cylinder body (34) is provided with sealing tremie pipe (1), the top of sealing tremie pipe (1) is provided with to stir supports (2), the top of stirring support (2) is provided with water sprayer tube (3), the top of water sprayer tube (3) is provided with lower tubesheet (32), the below of lower tubesheet (32) is provided with upper tubesheet (30), between lower tubesheet (32) and upper tubesheet (30), be provided with heat pipe (31), the top of upper tubesheet (30) is provided with I type charging tray with holes (5), the top of I type charging tray with holes (5) is provided with II type charging tray with holes (6), below one side of I type charging tray with holes (5) is provided with II type and falls material pipe (29), the top of II type charging tray with holes (6), on the outer side wall of inner barrel (33), be provided with manhole (28), the top of manhole (28) is provided with the sealing of I type and falls material pipe (27), the top of material pipe (27) falls in the sealing of I type, on the outer side wall of inner barrel (33), each zone of heating is respectively equipped with warm-air pipe (7), the top of warm-air pipe (7) is provided with chuck air bound plate (8), the inner side of inner barrel (33) is provided with several stirring guide rail trays (10), the top of stirring guide rail tray (10) is provided with guide assembly (11), the top of chuck air bound plate (8), on the outer side wall of outer cylinder body (34), be provided with thermal insulation layer (26), on stir shaft (19), be provided with agitating arm (9), in tower, be provided with II plate-type and stir (12), II plate-type stirs a side-lower of (12), on the outer wall of outer cylinder body (34), be connected with gas gathering manifold (22) by interlayer effuser (25), the top that II plate-type stirs (12) is provided with I plate-type stirring (13), the top that I plate-type stirs (13) is provided with stirring axle sleeve (14), the top of stirring axle sleeve (14) is provided with II type sealing charging tray (24), the top of II type sealing charging tray (24) is provided with II type rake and stirs (15), the top that II type rake stirs (15) is provided with interlayer board (16), the top of interlayer board (16) is provided with I type sealing charging tray (23), the top of I type sealing charging tray (23) is provided with I type rake and stirs (17), the top that I type rake stirs (17) is provided with sealing feed-pipe (18).
2. band stirs the upright tower smalls of multilayer, oil shale distillation production technique, is characterized in that its technical process is: (1), choose coal that particle is less than 25mm, resinous shale and other and can produce the solid material of volatile matter in heat-processed; (2), raw material adds by sealing from top of tower, at the first layer, raw material is imported to above stirring by the feed-pipe at edge or center, by the grid distributor on stirring, raw material is advanced to the sealing tremie pipe direction of this layer, drop to one deck from sealing tremie pipe, on adjacent destructive distillation layer, the flow direction of raw material is contrary, between each layer falling material passage have all the time raw material from top to bottom sealing tremie pipe end with naturally in heaps to upper strata, be filled in and in passage, play sealing function, the raw material that shutoff is sealed to tremie pipe by stirring is transferred whole aspect to, and each layer of feed distribution is even; (3), first raw material enter preheating section, the hot gas flow that utilizes retort section to rise from hot gas path carries out indirect preheating to the raw material entering in tower; (4), raw material moves up into retort section under after preheating section preheats, by with hot gas path in hot flue gas indirect heat exchange, temperature improves gradually, operating temperature is controlled at 350-950 DEG C, working time, the coal gas of generation entered gas main from each layer of gas flue at 30-360 minute; (5), the material that finishes of destructive distillation enters burning zone, in this section, the air entering is by the destructive distillation resistates burning of aperture and carbon containing, for the destructive distillation layer of epimere provides heat; (6), under raw material, move up into after cooling section, the solid of destructive distillation is cooled by circulating flue gas, the solid adverse current of flue gas and destructive distillation, progressively heated, pyrolyzate, by progressively cooling, is further lowered the temperature to air cooling layer under destructive distillation solid, equally, freezing air and pyrolyzate adverse current are progressively heated, and heated air and carbonization gas burn in burner, provide destructive distillation required heat energy; (7), consider that the raw material particle size of institute's destructive distillation is little, dry small particle size destructive distillation solid may produce dust in the time of discharging, bottom can be according to feed states, establishes water spraying cooling layer, if destructive distillation material temperature out is low, dust is little, can not establish this layer; (8), in whole retort section, destructive distillation chamber and heating chamber are isolated completely, heat air is made different passages leave with rage from destructive distillation; (9), in retort process, by regulating air, the carbonization gas of purification, amount of circulating gas control institute heat requirement, the number of each layer of destructive distillation institute heat requirement is regulated by the amount of heat air, even if not independent peripheral supplemental heat source, also can provide the heat that requires according to destructive distillation by the heat storage of heating chamber; (10), the destructive distillation temperature of the discharging of the coke is 20-150 DEG C, the temperature out of carbonization gas is 60-250 DEG C.
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| CN103666508B (en) * | 2013-12-24 | 2015-07-01 | 辽宁东大粉体工程技术有限公司 | Low-rank coal low-temperature dry distillation pyrolysis process |
| CN103897759A (en) * | 2014-02-13 | 2014-07-02 | 新疆科利尔能源有限公司 | External combustion and internal heating type methane generation device |
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