CN105273733A - Small-particle-size low-rank coal pyrolysis technology and equipment coupling multi-stage dust reducing - Google Patents
Small-particle-size low-rank coal pyrolysis technology and equipment coupling multi-stage dust reducing Download PDFInfo
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- CN105273733A CN105273733A CN201510819427.9A CN201510819427A CN105273733A CN 105273733 A CN105273733 A CN 105273733A CN 201510819427 A CN201510819427 A CN 201510819427A CN 105273733 A CN105273733 A CN 105273733A
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Abstract
The invention provides a pyrolysis furnace, small-particle-size low-rank coal pyrolysis equipment coupling multi-stage dust reducing and containing the pyrolysis furnace and a small-particle-size low-rank coal pyrolysis technology coupling multi-stage dust reducing and applying the equipment. The heat conducting efficiency of out heating pyrolysis can be improved; granular dust in the pyrolysis process is inhibited, and a raw coke oven gas dust carrying zone is minimized; high-temperature oil-dust separation is performed on dust in the raw coke oven gas carrying zone, and the tar quality is improved.
Description
Technical field
The present invention relates to is small particle size low-rank coal pyrolytic technique field, particularly relates to small particle size low-rank coal pyrolytic process and relevant device that a kind of coupling multi-stage subtracts dirt.
Background technology
Coal is one of Chinese topmost fossil energy, and the energy consumption structure of China based on coal can not change within longer one period in future.Low-rank coal comprises the bituminous coal (long-flame coal, non-caking coal and weakly caking coal) of brown coal and low metamorphic grade, and its proven reserve account for about 57% of national coal resources reserves, have become the important component part of Energy production and supply.In recent years, along with combining improving constantly and the large scale development of coal excavation apparatus of technology of adopting, broken coal rate is higher, and due to the physical strength of low-rank coal itself lower, less stable, also can be constantly broken in production and transport process, therefore in coal production at present, the lump coal of more than 20mm only accounts for about 3 one-tenth, creates small particle size low order broken coal and the fine coal of enormous amount.Chemically angle analysis, more high volatile ingredient is contained in low-rank coal, the products such as clean oil, gas can be extracted by the approach of thermal transition, and obtain the solid semicoke of high-quality, but most low-rank coal especially small particle size coal is directly used in combustion power generation more, fail to realize the efficiency utilization of resource.Small particle size low-rank coal being carried out the classification high-efficiency cleaning that pyrolysis obtains clean fuel and then realize low-rank coal resource utilizes for reduction China oil gas energy external dependence degree, reduce coal utilization environmental pollution, improve coal resources economy and social value, promote coal industry technical progress and have great importance.
Low-rank coal pyrolytic technique is from principle, be divided into external-heat (thermal barrier and coal indirect heat exchange) and internal heat type (thermal barrier and coal direct contact heat transfer) by type of heating, be divided into solid thermal carriers (hot semicoke, hot ash, hot porcelain ball etc.) and gaseous heat-carrier (heat smoke, heating gas etc.) by the type of thermal barrier.At present industrial generally apply for internal thermal upright stove pyrolytic technique, adopt 30-80mm lump coal, burning heat smoke in stove with coal direct contact heat transfer, but heat smoke circulates between coal cinder needs passage, therefore larger lump coal can only be utilized, broken coal and the fine coal of small particle size can not be utilized, otherwise can airway blockage be caused.
In recent years, small particle size low-rank coal pyrolytic technique tempo of development is very fast, but is substantially all in laboratory research and development and enlarged experiment experimental stage, and the industrialization not yet realizing real meaning runs.Verify that the pyrolysis realizing small particle size low-rank coal does not exist a technical difficult problem through stages such as laboratory research and development and enlarged experiment, but do not have at present can industrialization run its key issue of pyrolytic technique be: pyrolytic process produces a large amount of fine dusts, and the raw gas produced by pyrolysis is entrained with reactor, full-bodied tar is difficult to effectively be separated with the dust that pyrolysis oil gas is carried secretly simultaneously, not only greatly add follow-up gas purification load, and very easily there is tar condensing deposition, cause subsequent purification system process line clogging, thus affect overall continuous and steady operation.
Patent of invention that Xibei Chemical Inst proposes " a kind of low degree of coalification method for pyrolysis and the product adopting the method to obtain ", public announcement of a patent application CN101880540A, as shown in Figure 1, its technical process is divided into drying, pyrolysis, quenching three sections in its technical process.Feed coal, after kiln dried, enters external-heat pyrolysis oven, and the semicoke after pyrolysis enters exterior cooling quenching stove.High temperature raw gas is first through single or multiple indirect cooler, carry out just cold, cutting out partial tar and water, then directly cooled by ammonia spray, tar is recovered to ammonia water and tar oil clarified separation groove by further deep cooling, coal gas after spray oil removing, is reclaimed tar fog wherein by electrical tar precipitator, finally obtains purified gas.The core of the method is the external-heat pyrolysis reactor that a kind of inside is provided with flood dragon, this external-heat reactor can be used as drying oven simultaneously, quenching stove uses, for telescoping structure, shown in its core reaction device Fig. 2, pass into cold and hot medium (cold water, freezing air or heat smoke) between urceolus 54 and inner core 53, thus play the effect of heating and cooling, inside is provided with spiral flood dragon 52, driven by motor, promote material and advance.Coal inlet 55 is arranged on the top of reactor one end, and heat smoke self-heating smoke inlet 56 enters, and self-heating exhanst gas outlet 58 is discharged, and the raw gas that inside reactor produces is discharged from raw gas outlet 57, and the semicoke after pyrolysis is discharged from coke outlet 59.
This essence of an invention can think that external jacket is with heating or the spiral conveyer of refrigerating function, the main drawback of this technical scheme is: 1. heat smoke runs between inner/outer tube, easily be short-circuited, only flow through the shortest shortcut from the inlet to the outlet, cause each position of inner core bucket wall to heat uneven; 2. screw auger can only promote material and moves in parallel forward, and the temperature of charge near bucket wall is high, and the temperature of charge away from bucket wall is low, and the rate of heat transfer between material is low, causes pyrolytic process material degree of pyrolysis to differ, reduces heat transfer efficiency simultaneously; 3. input and output material drop is comparatively large, does not solve the problem of fine particle airborne dust in pyrolysis reactor, as easy as rolling off a logly causes dust content in raw gas high.
Summary of the invention
The object of the invention is the Technology providing the pyrolysis of a kind of small particle size low-rank coal, can realize higher heat transfer efficiency, minimum dust carries secretly and good dust removing effects, obtains semicoke, coal gas, the tar products of high-quality.
First the invention provides a kind of pyrolysis oven, comprise pyrolysis chamber, pyrolysis chamber is provided with coal inlet, coke outlet and transmission shaft, and its emphasis improves and is: described pyrolysis oven comprises the combustion chamber of promising pyrolysis chamber heat supply; Described transmission shaft is provided with rotating inner member coal charge self-coal-inlet being delivered to coke outlet.Described rotating inner member is the scraper plate be successively set in pairs on transmission shaft, and each scraper plate drive shaft is arranged to axle extension; Every a pair scraper plate is oppositely arranged on the same plane of transmission shaft, two pairs of adjacent scraper plates to arrange plane orthogonal; A scraper plate in every a pair scraper plate and the direction of the inclination of transmission shaft phase cross surface are self-coal-inlets is inclined at acute angles to coke outlet, and another scraper plate arranged in contrast pivots after 180 degree, and situation is identical with it.Wherein, between described scraper plate and transmission shaft, the scope of acute rake angle is 30 degree to 60 degree.
Adopt external-heat to heat in the present invention, coordinate rotating inner member to carry out upset disturbance to material simultaneously, suppress dust to produce while improving heat transfer efficiency by a relatively large margin, shovel propulsion mode, be more conducive to the thermally equivalent of coal charge, reaction efficiency is high.Dedusting inner member is set in pyrolysis chamber, by the pyrolysis reactor structure design of rotating inner member coupling collision inertial dust collection, minimizes raw gas dust and carry secretly, reduce subsequent purification difficulty.
Wherein, be provided with burner in described combustion chamber, described burner is positioned at below the coal inlet of front end, pyrolysis chamber, described combustion chamber and heat smoke expanding channels; Described heat smoke passage extends to rear end, bottom from pyrolysis chamber's bottom front, and extends to side, pyrolysis chamber from rear end, bottom, and extends to pyrolysis chamber's side front end from rear end, side, pyrolysis chamber is roundabout, and extends pyrolysis chamber from pyrolysis chamber's side front end.Setting like this, by the various piece of the roundabout bosom pyrolysis oven of heat smoke passage, can reach and improve pyrolysis efficiency, reduce costs the effect of input.
In addition, in order to further reduce dust in raw gas, top, described pyrolysis chamber is provided with dust preliminary sedimentation sending down abnormally ascending room; Wherein, described dust preliminary sedimentation sending down abnormally ascending indoor are provided with dedusting inner member; Described dedusting inner member be single or multiple lift grid or shape collision dividing plate, wide aperture metal graticule mesh.
In the present invention, in pyrolysis chamber, mildization material movement suppresses dust produce and be coupled with the dedusting air chamber of dedusting inner member, further suppresses airborne dust, reduces carrying secretly of subsequent reactions dust.
In addition, the small particle size low-rank coal pyrolysis plant that the present invention also provides a kind of coupling multi-stage to subtract dirt, comprise eccentric screw moisture eliminator, pyrolysis oven, oke-quenching device, described pyrolysis oven, comprise pyrolysis chamber, pyrolysis chamber is provided with coal inlet, coke outlet and transmission shaft, and its emphasis improves and is: described pyrolysis oven comprises the combustion chamber of promising pyrolysis chamber heat supply; Described transmission shaft is provided with rotating inner member coal charge self-coal-inlet being delivered to coke outlet; Described rotating inner member is the scraper plate be successively set in pairs on transmission shaft, and each scraper plate drive shaft is arranged to axle extension; Every a pair scraper plate is oppositely arranged on the same plane of transmission shaft, a scraper plate in every a pair scraper plate and the direction of the inclination of transmission shaft phase cross surface are self-coal-inlets is inclined at acute angles to coke outlet, and another scraper plate arranged in contrast pivots after 180 degree, and situation is identical with it.Wherein, between described scraper plate and transmission shaft, the scope of acute rake angle is 30 degree to 60 degree.
In this programme, be provided with burner in described combustion chamber, described burner is positioned at below the coal inlet of front end, pyrolysis chamber, described combustion chamber and heat smoke expanding channels; Described heat smoke passage extends to rear end, bottom from pyrolysis chamber's bottom front, and extends to side, pyrolysis chamber from rear end, bottom, and extends to pyrolysis chamber's side front end from rear end, side, pyrolysis chamber is roundabout, and extends pyrolysis chamber from pyrolysis chamber's side front end.
Wherein, top, described pyrolysis chamber is provided with dust preliminary sedimentation sending down abnormally ascending room; Described dust preliminary sedimentation sending down abnormally ascending indoor are provided with dedusting inner member.
In addition, hot precipitator, shell and tube cooler and electrical tar precipitator is also included; Described pyrolysis oven connects hot precipitator, described hot precipitator connecting column tubular cooler, and described shell and tube cooler connects electrical tar precipitator.
Wherein, be provided with primary dust removing metal screen and two-stage dust removal metal screen in described hot precipitator, wherein primary dust removing metal screen is 100 orders, and two-stage dust removal metal screen is 200 orders.
Adopt external-heat to heat in the present invention, coordinate rotating inner member to carry out upset disturbance to material simultaneously, suppress dust to produce while improving heat transfer efficiency by a relatively large margin, shovel propulsion mode, be more conducive to the thermally equivalent of coal charge, reaction efficiency is high.Dedusting inner member is set in pyrolysis chamber, by the pyrolysis reactor structure design of rotating inner member coupling collision inertial dust collection, minimizes raw gas dust and carry secretly, reduce subsequent purification difficulty.In pyrolysis chamber, mildization material movement suppresses dust produce and be coupled with the dedusting air chamber of dedusting inner member, further suppresses airborne dust, reduces carrying secretly of subsequent reactions dust.Low dust content raw gas, through the dedusting of thermal state metal net filtration, will be carried dust removing secretly, reduce dust content in tar, improve tar quality.
Finally, the invention provides the small particle size low-rank coal pyrolytic process that a kind of coupling multi-stage subtracts dirt, equipment in the right to use 8, its improvement is, comprise following technique: the heat smoke that the small particle size feed coal of granularity≤20mm is 350-400 DEG C with temperature in zone of heating (104) in eccentric screw moisture eliminator (1) carries out heat exchange, the feed coal residence time is 20-40 minute, and the coal charge moisture entering moisture eliminator is 8-10%, and after dry, coal sample moisture is less than 2%; The coal charge of drying device (1) drying enters pyrolysis oven (2), and coal charge is at interior residence time 80-160 minute, pyrolysis temperature 500-800 DEG C, and the speed of rotation of rotating inner member (205) is 0-5r/min, exports the high-temperature semi-coke after pyrolysis; High-temperature semi-coke after pyrolysis enters oke-quenching device 3, and the high-temperature semi-coke temperature entering oke-quenching device is 600-750 DEG C, and the residence time is 20-30 minute, and oke-quenching device outlet semicoke temperature controls as 50-60 DEG C.
The raw gas that pyrolysis oven (2) produces enters hot precipitator (4), and the working temperature of hot precipitator is 380-480 DEG C; High temperature raw gas after dedusting enters cooling system (5), and cooled raw gas temperature controls below 20 DEG C; Cooled waste coal enters electrical tar precipitator (6) and carries out deep purifying, collects tar and purified gas after being separated.
Wherein, the working temperature of described hot precipitator is for being preferably 400-450 DEG C.
The advantage of such scheme is as follows.
(1) the present invention improves the heat transfer efficiency of external-heat pyrolysis.
Adopt horizontal external-heat pyrolysis reactor, heat smoke reacting by heating wall, then conduct heat to coal charge, inside reactor establishes transmission inner member, coal charge spiral under the drive of transmission inner member advances, except travelling forward, upper materials slowly moves to the lower floor position of reactor wall, and the material of lower floor's heating progressively moves to upper strata.Therefore low-temperature material can contact with pyroreaction wall, and temperature head is comparatively large, and cold and hot material also can mix and then conduct heat at the volley simultaneously, and heat transfer efficiency is compared to common external-heat pyrolysis and has higher heat transfer efficiency.
(2) suppress particle airborne dust in pyrolytic process, minimize raw gas dust and carry secretly.
The motion of material in reactor is all in surface sliding state, and rotating inner member speed of rotation is slow simultaneously, suppresses the motion of particle to greatest extent, therefore avoids airborne dust from source as far as possible and produces; Pyrolysis reactor top coupling dust-settling compartment, by special " it " shape structure design, raw gas can be subject to inertial impaction dedusting and the dual depositing dust effect of dust gravity settling at ascent stage, to leave after dust-settling compartment dust entrainment in raw gas minimum.
(3) separation of dust high temperature oil dirt carried secretly by raw gas, improves tar quality.
The subparticle of minute quantity carried secretly by the raw gas left behind dust preliminary sedimentation sending down abnormally ascending room, enter thermal state metal net filtration fly-ash separator, after 100 orders (0.147mm) and 200 orders (0.074mm) two-stage metal mesh filter, enter tar condensing collecting device, condensed tar enters tar storer, hot precipitator is outer to be heated by for the useless flue gas after pyrolysis reactor heating, improves energy utilization efficiency.
Accompanying drawing explanation
Fig. 1 is the schematic diagram of a kind of low degree of coalification method for pyrolysis in prior art.
Fig. 2 is the external-heat pyrolysis reactor that in prior art, a kind of inside is provided with spiral flood dragon.
Fig. 3 is the small particle size low-rank coal pyrolytic process route map that a kind of coupling multi-stage of the present invention subtracts dirt.
Fig. 4 is the side structure schematic diagram of external-heat moisture eliminator in the present invention.
Fig. 5 is the schematic cross-section of external-heat moisture eliminator in the present invention.
Fig. 6 is the side structure schematic diagram of pyrolysis oven in the present invention.
Fig. 7 is the schematic cross-section of pyrolysis oven in the present invention.
Fig. 8 is the another kind of exhaust gases passes side elevational view of pyrolysis oven in the present invention.
Fig. 9 is thermal state metal net filtration fly-ash separator schematic diagram in the present invention.
Figure 10 is the structural representation of middle scraper of the present invention.
Figure number explanation.
1-external-heat moisture eliminator; 2-pyrolysis oven; 3-oke-quenching device; 4-hot precipitator; 5-shell and tube cooler; 6-electrical tar precipitator; 7-coal feeding pipe line; 8-steam vent line; 9-moisture-free coal enters reactor line; 10-high-temperature semi-coke enters oke-quenching device pipeline; 11-cools semicoke vent line; 12-high temperature raw gas enters fly-ash separator pipeline; 13-coal gas of high temperature enters water cooler pipeline; After 14-cooling, coal gas enters electrically trapped tar oil pipeline; 15-purified gas vent line; 16-part coal gas melts down pipeline; 17,18,19-tar and water discharge pipe line; 20-air enters combustion chamber pipeline; 21-part hot waste gas enters moisture eliminator pipeline; 22-part hot waste gas enters high-temperature dust removal pipeline; 23,24-hot waste gas vent line; 25-hot precipitator ash discharging hole; Other combustion gas of 26-enter combustion chamber pipeline.
101-drive-motor; 102-step-down gear; 103-coal inlet; 104-zone of heating; 105-screw-blade; 106-moisture outlet; 107-coal outlet; 108-hot gas inlet; 109-heat outlet; 110-screw-blade; 111-moisture eliminator wall of the outer-rotor; 112-transmission shaft.
201-drive-motor; 202-step-down gear; 203-coal inlet; 204-transmission shaft; 205-rotating inner member; 206-raw gas exports; 207-high-temperature semi-coke outlet (coke outlet); 208-dust settling air chamber; 209-pyrolysis chamber; 210-thermal insulation layer; 211-dedusting inner member; 212-heat smoke passage; 213-combustion chamber.
401-dust-laden raw gas entrance; 402-heat smoke entrance; 403-heat smoke exports; 404-primary dust removing metal screen; 405-two-stage dust removal metal screen; 406-purified gas exports; 407-heat smoke passage; 408-dust relief outlet.
Embodiment
As shown in Figure 3, it is the small particle size low-rank coal pyrolytic process route map that a kind of coupling multi-stage of the present invention subtracts dirt.From structure, the equipment that whole set process comprises has: external-heat moisture eliminator 1, pyrolysis oven 2, oke-quenching device 3, hot precipitator 4, shell and tube cooler 5, electrical tar precipitator 6.External-heat moisture eliminator 1 connects pyrolysis oven 2, and pyrolysis oven 2 connects oke-quenching device 3, forms solids treatment path.Pyrolysis oven 2 connects hot precipitator 4, hot precipitator 4 connecting column tubular cooler 5, and shell and tube cooler 5 connects electrical tar precipitator 6, forms coal gas process path.
As shown in Figure 4 and Figure 5, it is the structural representation of the external-heat moisture eliminator in the present invention.It comprises drive-motor 101, step-down gear 102, coal inlet 103, zone of heating 104, screw-blade 105; Moisture outlet 106, coal outlet 107, hot gas inlet 108, heat outlet 109, screw-blade 110, moisture eliminator wall of the outer-rotor 111 and transmission shaft 112.
External-heat moisture eliminator 1(is also known as spiral dryer) be eccentric screw structure, connect step-down gear 102 by drive-motor 101 and drive transmission shaft 112, transmission shaft 112 is arranged screw-blade 105, screw-blade 105 and moisture eliminator wall of the outer-rotor 111 are eccentric design, as shown in Figure 5, bottom screw-blade with barrel bottom tangent, top is away from barrel top, therefore go up sheaf space comparatively large, be convenient to steam effusion.Moisture eliminator wall of the outer-rotor 111 periphery is heat smoke flow cavity, i.e. zone of heating 104.Burn and produce heat smoke first to after pyrolysis oven heating in the combustion chamber 213 of following pyrolysis oven 2, waste heat enters the peripheral zone of heating 104 of spiral dryer by hot gas inlet 108, heats, and discharge from heat outlet 109 to moisture eliminator.Raw material of the present invention is applicable to below 20mm small particle size brown coal, long-flame coal, non-caking coal, weakly caking coal.Feed coal self-coal-inlet 103 after screening enters external-heat moisture eliminator 1, under the effect of screw-blade 110, is delivered to the other end from one end, in course of conveying, carries out indirect heating drying, and discharge from coal outlet 107.
Dried coal sample seals device (not indicating in figure) through punishment in advance and pipe connecting slips into pyrolysis oven 2.Pyrolysis oven 2 of the present invention is by combustion chamber 213, pyrolysis chamber 209, dust preliminary sedimentation sending down abnormally ascending room 208 3 part composition, as shown in Figure 6 and Figure 7, combustion chamber 213 is positioned at bottom, adopt Sweet natural gas, liquefied petroleum gas (LPG) or coal gas and air mixed are burnt, first heat smoke is gathered in bottom pyrolysis oven 2 and heats to pyrolysis chamber 209 coal charge, concrete implementation can be set gradually multiple burner in combustion chamber 213, the area of heat-supply service of burner is covered with the below of pyrolysis chamber 209, in such cases, the both sides of pyrolysis chamber 209 form heat smoke passage 212, heat can be provided for the side of pyrolysis chamber, as shown in Figure 8, there is another kind of heat-supplying mode, specifically, described burner is positioned at below pyrolysis chamber 209 front end coal inlet 203, described combustion chamber 213 is connected with heat smoke passage 212 ', described heat smoke passage 212 ' extends to rear end, bottom from pyrolysis chamber 209 bottom front, and extend to side, pyrolysis chamber 209 from rear end, bottom, and extend to pyrolysis chamber's side front end from rear end, side, pyrolysis chamber 209 is roundabout, and extend pyrolysis chamber 209 from pyrolysis chamber 209 side front end, for pyrolysis chamber 209 and the insulation of dust preliminary sedimentation sending down abnormally ascending room 208 sidewall, and finally enter moisture eliminator 1 zone of heating 104 and fly-ash separator heat preservation sandwich layer at pyrolysis oven 2 top.
As shown in Figure 6, described pyrolysis oven 2 also comprises drive-motor 201, drive-motor 201 connects step-down gear 202, drive transmission shaft 204, described driving transmission shaft 204 is arranged at intervals with multiple rotating inner member 205, each rotating inner member 205 center is arranged on transmission shaft 204, and is inclined to set with transmission shaft 204.Pyrolysis oven 2 side is provided with coal inlet 203, and opposite side is provided with coke outlet 207, and upper end, pyrolysis chamber 209 is provided with dedusting inner member 211, and raw gas outlet 206 and heat smoke passage 212, pyrolysis oven 2 outer wall is provided with thermal insulation layer 210.
Wherein, as shown in Figure 7, described rotating inner member 205 is be successively set on straight plate on transmission shaft 204 or paddle scraper plate in pairs, and each scraper plate drive shaft 204 is arranged to axle extension; Every a pair scraper plate is oppositely arranged on the same plane of transmission shaft 204, two pairs of adjacent scraper plates to arrange plane orthogonal; As shown in Fig. 6 and Figure 10, the direction of a scraper plate in every a pair scraper plate and the inclination of axle intersecting plane be self-coal-inlet 203 to coke outlet 207 in inclined at acute angles, another scraper plate arranged in contrast pivots after 180 degree, and situation is identical with it.Between described scraper plate and transmission shaft 204, the scope of acute rake angle is 30 degree to 60 degree.
Coal charge slips into from pyrolysis chamber 209 upper angled, under the driving of rotating inner member 205, is slided and advances, and slip into coke outlet 207 to oke-quenching device 3 at the rear portion of pyrolysis chamber 209 and indirectly cool quenching by forward direction rear screw formula.Pyrolysis chamber 209 main body and the rotating inner member 205 of pyrolysis oven 2 select 310S stainless steel, heat smoke passage 212 selects 304L stainless steel, combustion chamber 213 is built into by refractory brick, and overall body of heater periphery forms thermal insulation layer 210 by the material such as calcium silicate board, ceramic fiber cotton.Material is at pyrolysis residing time in furnace 80-160min, pyrolysis temperature 500-800 DEG C, and the speed of rotation of rotating inner member 205 is 0-5r/min.The drive-motor of rotating inner member 205 adopts variable-frequency motor, and stepless change is adjustable, controls the residence time of coal charge thus.
Coal charge and heat smoke adverse current indirect heat exchange, the dry hot steam produced enters water vapor condenser and collects.Coal charge residence time in eccentric screw moisture eliminator is 20-40 minute, and spiral dryer peripheral cavity heat smoke temperature is 350-400 DEG C, and the coal charge moisture entering moisture eliminator is about 8-10%, and after dry, coal sample moisture is below 2%.Spiral dryer material adopts high-temperature-resistant steel, and screw rod is 304 stainless steels preferably, Q245R or Q345 steel selected by urceolus.Eccentric screw moisture eliminator is driven by variable-frequency motor, controls residence time of material thus.
High-temperature semi-coke after pyrolysis enters oke-quenching device 3 by coke outlet 207, oke-quenching device 3 is indirect-cooling form concentric spirals oke-quenching device, spiral conveyer periphery is water jacket, indirect heat exchange refrigeration is carried out by recirculated water, the hot semicoke temperature entering oke-quenching device is 600-750 DEG C, in spiral conveyer, stop about 20-30 minute, oke-quenching device outlet semicoke temperature controls to be 50 DEG C about-60 DEG C.Oke-quenching device is driven by variable-frequency motor, controls residence time of material thus.
First the raw gas that pyrolysis oven 2 produces enters thermal state metal net filtration fly-ash separator 4, hot precipitator 4 structural representation as shown in Figure 8, it has dust-laden raw gas entrance 401, heat smoke entrance 402, heat smoke outlet 403, primary dust removing metal screen 404, two-stage dust removal metal screen 405, purified gas outlet 406, heat smoke passage 407 and dust relief outlet 408, wherein primary dust removing metal screen 404 is 100 orders, and two-stage dust removal metal screen 405 is 200 orders.Dust-laden raw gas successively carries out dust removal by filtration through 100 orders and 200 order two-stage wire nettings.Hot fly-ash separator is jacketed type fly-ash separator, and the waste heat flue gas produced by pyrolysis oven enters the outer chuck of fly-ash separator and is incubated, and guarantees that tar steam condensation does not occur, and the fine particle filtered down is drained into ash output hole by concussion blowback by filtering net.The working temperature of hot precipitator is 380-480 DEG C, is preferably 400-450 DEG C.
High temperature raw gas after dedusting enters cooling system, cooling system is made up of one or more levels shell and tube heat exchanger, tar under condensation and water enter profit and store in separator and carry out next step and be separated, shell-and tube condenser is cooled by the efficient circulating refrigerant such as recirculated water or aqueous glycol solution, cooled raw gas temperature controls below 20 DEG C, cooled raw gas still containing certain vaporific tar, enters electrical tar precipitator and carries out deep purifying, collects tar and purified gas after being separated.Purified gas part returns to pyrolysis oven combustion chamber and burns, and part is sent outside.
As shown in Figure 3, it is process flow sheet of the present invention, the small particle size feed coal of granularity≤20mm enters in eccentric screw moisture eliminator 1 through coal feeding pipe line 7, carries out adverse current indirect heat exchange with the high-temperature flue gas of 350-400 DEG C entering moisture eliminator pipeline 21 from part hot waste gas.The steam produced in drying process enters moisture condensation gathering system via steam vent line 8.Heat smoke after heat exchange enters waste gas afterheat recovery system through hot waste gas vent line 23.
The dry coal charge drying coal of drying device enters reactor line 9 and enters pyrolysis oven 2, and pyrolysis occurs in pyrolysis chamber and generates semicoke, tar steam and coal gas, final pyrolysis temperature is 500-800 DEG C.
Pyrolysis chamber produce high-temperature semi-coke through high-temperature semi-coke enter oke-quenching device pipeline 10 enter between cold spiral oke-quenching device 3, as semicoke product output after being cooled to about 50 DEG C.
First the raw gas that pyrolysis oven produces enters fly-ash separator pipeline 12 through high temperature raw gas and enters thermal state metal filter collector 4, fly-ash separator operating temperature is 380-480 DEG C, the superfine dust carried secretly in raw gas can be filtered, and discharges through hot precipitator ash discharging hole 25.The pyrolysis oven part waste heat flue gas of discharging enters through part hot waste gas the heat preservation sandwich layer that high-temperature dust removal pipeline 22 enters filter collector 4 and is incubated to fly-ash separator, and the waste heat flue gas of discharging from fly-ash separator is mixed into Waste Heat Recovery System (WHRS) through hot waste gas vent line 24 and the useless flue gas from pipeline 23.
High temperature raw gas after purification contains water vapour, tar steam and coal gas, enter water cooler pipeline 13 through coal gas of high temperature and enter cooling system 5 by fly-ash separator, cooling system 5 is made up of one or more groups shell and tube heat exchanger, carry out indirect heat exchange by the efficient refrigeration agent such as recirculated cooling water or aqueous glycol solution to freeze to less than 20 DEG C, congeal into most tar and water-cooled liquid, and the tar that cooling receives and water enter tar and water separator through tar and water discharge pipe line 17.
Containing a certain amount of tar fog in cooled coal gas, after cooling, coal gas enters electrically trapped tar oil pipeline 14 and enters electrical tar precipitator 6 and carry out deep purifying, and the tar that the tar that electrical tar precipitator 6 traps and water are collected through tar and water discharge pipe line 18 and cooling system 5 and water are mixed into pipeline 19 and enter tar and water separator.
A coal gas part after electrical tar precipitator 6 purifies is sent into coal gas storage facility through purified gas vent line 15 or delivers to subsequent processing outward, another part melts down pipeline 16 by part coal gas and is back to the combustion chamber of pyrolysis reactor 2 and burns from the air mixed of pipeline 20, also can other of combustion chamber pipeline 26 are more low-calorie to be substituted as fuel gas such as artificial coal gas by entering from other combustion gas, thus save the pyrolysis coal gas being rich in methane.The high-temperature flue gas produced after burning, to after the heating of pyrolysis chamber's coal charge, through the sedimentation dust settling chamber insulation that twisting flue is coupled to pyrolysis chamber's wall and top, is finally discharged by hot waste gas vent line 23 and 24.
Claims (13)
1. a pyrolysis oven (2), comprises pyrolysis chamber (209), and pyrolysis chamber (209) are provided with coal inlet (203), coke outlet (207) and transmission shaft (204), it is characterized in that:
Described pyrolysis oven (2) comprises the combustion chamber (213) of promising pyrolysis chamber (209) heat supply;
Described transmission shaft (204) is provided with the rotating inner member (205) coal charge self-coal-inlet (203) being delivered to coke outlet (207);
Wherein, described rotating inner member (205) is the scraper plate be successively set in pairs on transmission shaft (204), and each scraper plate drive shaft (204) is arranged to axle extension;
Every a pair scraper plate is oppositely arranged on the same plane of transmission shaft (204), two pairs of adjacent scraper plates to arrange plane orthogonal;
A scraper plate in every a pair scraper plate and the direction of the inclination of transmission shaft (204) phase cross surface be self-coal-inlet (203) to coke outlet (207) in inclined at acute angles, another scraper plate arranged in contrast pivots after 180 degree, and situation is identical with it.
2. pyrolysis oven (2) as claimed in claim 1, is characterized in that: between described scraper plate and transmission shaft (204), the scope of acute rake angle is 30 degree to 60 degree.
3. pyrolysis oven (2) as claimed in claim 2, it is characterized in that: described combustion chamber is provided with burner in (213), described burner is positioned at below, pyrolysis chamber (209) front end coal inlet (203), and described combustion chamber (213) are connected with heat smoke passage (212 ');
Described heat smoke passage (212 ') extends to rear end, bottom from pyrolysis chamber (209) bottom front, and extend to pyrolysis chamber (209) side from rear end, bottom, and roundaboutly from pyrolysis chamber (209) rear end, side extend to pyrolysis chamber (209) side front end, and extend pyrolysis chamber (209) from pyrolysis chamber (209) side front end.
4. the pyrolysis oven (2) as described in claim any in claims 1 to 3, is characterized in that: described pyrolysis chamber (209) top is provided with dust preliminary sedimentation sending down abnormally ascending room (208).
5. pyrolysis oven (2) as claimed in claim 4, is characterized in that: be provided with dedusting inner member (211) in described dust preliminary sedimentation sending down abnormally ascending room (208).
6. pyrolysis oven (2) as claimed in claim 5, is characterized in that: described dedusting inner member be single or multiple lift grid or shape collision dividing plate, wide aperture metal graticule mesh.
7. a coupling multi-stage subtracts the small particle size low-rank coal pyrolysis plant of dirt, comprise eccentric screw moisture eliminator (1), pyrolysis oven (2), oke-quenching device (3), described pyrolysis oven (2), comprise pyrolysis chamber (209), pyrolysis chamber (209) is provided with coal inlet (203), coke outlet (207) and transmission shaft (204), it is characterized in that:
Described pyrolysis oven (2) comprises the combustion chamber (213) of promising pyrolysis chamber (209) heat supply;
Described transmission shaft (204) is provided with the rotating inner member (205) coal charge self-coal-inlet (203) being delivered to coke outlet (207);
Described rotating inner member (205) is the scraper plate be successively set in pairs on transmission shaft (204), and each scraper plate drive shaft (204) is arranged to axle extension;
Every a pair scraper plate is oppositely arranged on the same plane of transmission shaft (204), two pairs of adjacent scraper plates to arrange plane orthogonal;
A scraper plate in every a pair scraper plate and the direction of the inclination of transmission shaft (204) phase cross surface be self-coal-inlet (203) to coke outlet (207) in inclined at acute angles, another scraper plate arranged in contrast pivots after 180 degree, and situation is identical with it.
8. a kind of coupling multi-stage as claimed in claim 7 subtracts the small particle size low-rank coal pyrolysis plant of dirt, it is characterized in that: described combustion chamber is provided with burner in (213), described burner is positioned at below, pyrolysis chamber (209) front end coal inlet (203), and described combustion chamber (213) are connected with heat smoke passage (212 ');
Described heat smoke passage (212 ') extends to rear end, bottom from pyrolysis chamber (209) bottom front, and extend to pyrolysis chamber (209) side from rear end, bottom, and extend to pyrolysis chamber's side front end from pyrolysis chamber (209) rear end, side is roundabout, and extend pyrolysis chamber (209) from pyrolysis chamber (209) side front end.
9. a kind of coupling multi-stage as claimed in claim 8 subtracts the small particle size low-rank coal pyrolysis plant of dirt, it is characterized in that: described pyrolysis chamber (209) top is provided with dust preliminary sedimentation sending down abnormally ascending room (208); Dedusting inner member (211) is provided with in described dust preliminary sedimentation sending down abnormally ascending room (208).
10. a kind of coupling multi-stage as claimed in claim 9 subtracts the small particle size low-rank coal pyrolysis plant of dirt, also includes hot precipitator (4), shell and tube cooler (5) and electrical tar precipitator (6); Described pyrolysis oven (2) connects hot precipitator (4), described hot precipitator (4) connecting column tubular cooler (5), and described shell and tube cooler (5) connects electrical tar precipitator (6).
11. a kind of coupling multi-stages as claimed in claim 10 subtract the small particle size low-rank coal pyrolysis plant of dirt, it is characterized in that: in described hot precipitator (4), be provided with primary dust removing metal screen (404) and two-stage dust removal metal screen (405), wherein primary dust removing metal screen (404) is 100 orders, and two-stage dust removal metal screen (405) is 200 orders.
12. 1 kinds of coupling multi-stages subtract the small particle size low-rank coal pyrolytic process of dirt, and the equipment in the right to use 1 to 11, is characterized in that, comprises following technique:
The heat smoke that the small particle size feed coal of granularity≤20mm is 350-400 DEG C with temperature in zone of heating (104) in eccentric screw moisture eliminator (1) carries out heat exchange, the feed coal residence time is 20-40 minute, the coal charge moisture entering moisture eliminator is 8-10%, and after dry, coal sample moisture is less than 2%;
The coal charge of drying device (1) drying enters pyrolysis oven (2), and coal charge is at interior residence time 80-160 minute, pyrolysis temperature 500-800 DEG C, and the speed of rotation of rotating inner member (205) is 0-5r/min, exports the high-temperature semi-coke after pyrolysis;
High-temperature semi-coke after pyrolysis enters oke-quenching device 3, and the high-temperature semi-coke temperature entering oke-quenching device is 600-750 DEG C, and the residence time is 20-30 minute, and oke-quenching device outlet semicoke temperature controls as 50-60 DEG C;
The raw gas that pyrolysis oven (2) produces enters hot precipitator (4), and the working temperature of hot precipitator is 380-480 DEG C;
High temperature raw gas after dedusting enters cooling system (5), and cooled raw gas temperature controls below 20 DEG C;
Cooled waste coal enters electrical tar precipitator (6) and carries out deep purifying, collects tar and purified gas after being separated.
13. a kind of coupling multi-stages as claimed in claim 12 subtract the small particle size low-rank coal pyrolytic process of dirt, it is characterized in that, the working temperature of described hot precipitator is for being preferably 400-450 DEG C.
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