CN105754624A - Low-order powdered coal pyrolysis system and method - Google Patents
Low-order powdered coal pyrolysis system and method Download PDFInfo
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- CN105754624A CN105754624A CN201610204171.5A CN201610204171A CN105754624A CN 105754624 A CN105754624 A CN 105754624A CN 201610204171 A CN201610204171 A CN 201610204171A CN 105754624 A CN105754624 A CN 105754624A
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 204
- 239000003245 coal Substances 0.000 title claims abstract description 103
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000007789 gas Substances 0.000 claims description 131
- 238000009825 accumulation Methods 0.000 claims description 54
- 239000000463 material Substances 0.000 claims description 54
- 239000000203 mixture Substances 0.000 claims description 32
- 239000007787 solid Substances 0.000 claims description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 20
- 239000003546 flue gas Substances 0.000 claims description 20
- 239000002994 raw material Substances 0.000 claims description 18
- 239000008247 solid mixture Substances 0.000 claims description 15
- 230000008569 process Effects 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 239000000779 smoke Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 7
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- 238000001035 drying Methods 0.000 abstract description 9
- 238000009833 condensation Methods 0.000 abstract description 6
- 230000005494 condensation Effects 0.000 abstract description 6
- 239000000428 dust Substances 0.000 abstract description 5
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- 238000005516 engineering process Methods 0.000 description 5
- 230000035800 maturation Effects 0.000 description 5
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- 239000003208 petroleum Substances 0.000 description 3
- 230000000903 blocking effect Effects 0.000 description 2
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- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a low-order powdered coal pyrolysis system and method.The low-order powdered coal pyrolysis system comprises a drying lift pipe, a first cyclone separator, a first screw feeder and a pyrolysis reactor.The pyrolysis system is suitable for processing powdered coal, gas heat carrier is not needed, pyrolysis oil and gas resources are guided out fast, tar is small in secondary reaction and high in quality, pyrolysis gas is not diluted, the heat value is large, the dust content of pyrolysis oil and gas output by a pyrolysis furnace can be effectively reduced, and the number of heat preservation facilities, between the pyrolysis reactor and a pyrolysis oil and gas fast condensation device, of a pipeline can be reduced.
Description
Technical field
The present invention relates to chemical field, in particular it relates to low order pulverized coal pyrolysis system and low order pulverized coal pyrolysis method.
Background technology
The energy resource structure of China is characterized as being rich coal, gas oil-poor, few, and as coal production maximum in the world and country of consumption, within one considerably long period, coal resources are unshakable as the status of the leading energy of China.According to statistics, it is 114,500,000,000 tons that China has verified coal reserves, and in wherein, low-order coal (brown coal, lower-grade metamorphic bituminous) accounts for again about the 55.15% of whole nation reserves.Due to low-order coal there is moisture height, easy-weathering is natural, be difficult to sorting, should not transport for long-distance and the feature such as storage so that its comprehensive utilization is very limited.Wherein directly combustion power generation is one of its modal Land use systems, and according to incompletely statistics, there are the brown coal of more than 90% in China for station boiler and various Industrial Boiler.Low-order coal is directly burnt as thermal coal fuel, not only wastes the hydrocarbon rich resource contained in coal, and efficiency is low.By low-temperature pyrolysis of coal and coal-char combustion, gasification decoupling, it is achieved low-order coal classification high-efficiency cleaning trans-utilization, is the Main way of present large-scale Coal Chemical Industry.
Widely use along with modernization coal mining is polytechnic so that the ratio of lump coal declines (being declined 10～20% by current 40%), and fine coal productivity raises (being risen to 80～90% by current 60%).There is easy airborne dust in fine coal, inflammable, explosive, the problems such as comprehensive utilization difficulty is big, pyrolysis of coal technology is considered as the maximally efficient approach of coal high-efficiency clean utilization.
Pyrolysis of coal technology conventional at present has Toscoal hot solid carrier devolatilization technique, Germany's Lurgi-Spuelgas low temperature pyrogenation technique, god mansion SH type internal thermal upright carbonization furnace technique etc., but all there is certain defect.In Toscoal hot solid carrier devolatilization technique, Ceramic Balls is in cyclic process, there is mechanical wear, and in the process of airlift conveying Ceramic Balls, pipeline and equipment inner wall are had a degree of abrasion, pyrolysis reactor adopts rotary kiln, the oil gas time of staying that pyrolysis produces is long, and oil gas secondary response is violent, and tar quality declines, after pyrolysis, semicoke and Ceramic Balls are completely separated difficulty.Germany's Lurgi-Spuelgas low temperature pyrogenation technique and god mansion SH type internal thermal upright carbonization furnace technique are suitable for processing lump coal, are not suitable for pulverized coal pyrolysis, adopt gas heat carrier, the pyrolysis petroleum resources produced after pyrolysis is diluted by gas heat carrier, and calorific value is low, and pyrolysis petroleum resources condensation number is big, lump coal volume is big, heat transfer coefficient is low, and heat transfer efficiency is not high, and pyrolysis time is long, oil gas secondary response is violent, tar quality is not high, and equipment is huge, not easily operates.
Thus, current pyrolytic process of coal still haves much room for improvement.
Summary of the invention
It is contemplated that one of technical problem solved at least to a certain extent in correlation technique.For this, it is an object of the present invention to propose one be suitable to process fine coal, do not need to adopt gas heat carrier, pyrolysis gas not to be diluted calorific value height, pyrolysis petroleum resources is quickly derived, the little quality of tar secondary reaction is high, it is possible to effectively reduces the pyrolysis oil gas dustiness pyrolysis reactor or can reduce pyrolysis reactor to the low order pulverized coal pyrolysis system of the lagging facility of pipeline between pyrolysis oil gas rapid condensation device and method for pyrolysis.
In one aspect of the invention, the invention provides a kind of low order pulverized coal pyrolysis system.According to embodiments of the invention, low order pulverized coal pyrolysis system includes:
Dry riser, described dry riser is provided with feed(raw material)inlet, smoke inlet and mixed material outlet, wherein, described feed(raw material)inlet is positioned on the sidewall of described dry riser bottom, described smoke inlet is positioned at the bottom of described dry riser, and the outlet of described mixed material is positioned on the sidewall on described dry riser top；
First cyclone separator, described first cyclone separator has the first gas-solid mixture entrance, the first gas outlet and the first solid outlet, described first gas-solid mixture entrance and described mixed material outlet；
First feed screw, described first feed screw is connected with described first solid outlet；
Pyrolysis reactor, described pyrolysis reactor is provided with pyrolysis material entrance, gas mixture outlet and semicoke outlet, described pyrolysis reactor is internally provided with many oil gas and derives pipelines, gas gathering manifold, many gas-collecting branch pipes, heat accumulation type radiant tube and the second cyclone separator
Wherein, described pyrolysis material entrance is connected with described first feed screw,
Described gas gathering manifold is arranged on the central shaft of described pyrolysis reactor,
One end of described gas-collecting branch pipe is connected with described gas gathering manifold, and the other end is communicated to described oil gas and derives pipeline；
Described second cyclone separator has the second gas-solid mixture entrance, the second gas outlet and the second solid outlet, wherein, described second gas outlet is connected with the outlet of described gas mixture, and the end of described gas gathering manifold extends the second gas-solid mixture entrance being communicated to described second cyclone separator；
Described heat accumulation type radiant tube is along the short transverse multi-tier arrangement of described pyrolysis reactor, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction.
Cyclone separator is arranged at inside pyrolysis reactor by low order pulverized coal pyrolysis system (being sometimes called for short " pyrolysis system " herein) according to embodiments of the present invention, can not only effectively reduce the dustiness of the pyrolysis of coal gas mixture discharging pyrolysis reactor, effectively suppress the pyrolysis oil gas discharging pyrolysis reactor to mix dust condensation blocking subsequent pipeline and relevant device；Meanwhile, in the built-in pyrolysis reactor of cyclone separator, it is also possible to reduce pyrolysis reactor to the lagging facility of pipeline between pyrolysis oil gas mixture rapid condensation device, reduce the thermal insulation area of equipment and reduce system heat tracing energy consumption；Additionally, gas mixture is quickly derived pyrolysis reactor by oil gas delivery line by this pyrolysis system, can effectively suppress oil gas second pyrolysis, improves pyrolysis oil yield, and by adopting heat accumulation type radiant tube heating technique, without gas, solid heat carrier heating, such that it is able to improve the thermal efficiency of reactor, additionally, adopt the pyrolysis system of the above embodiment of the present invention without complicated machinery, inside reactor each point temperature is adjustable flexibly, has the features such as technological process is simple, it is simple to large-scale industrial production.
In some embodiments of the invention, described gas-collecting branch pipe is arranged parallel to each other along the length direction of described gas gathering manifold.
In some embodiments of the invention, described gas-collecting branch pipe is perpendicular to described gas collecting main pipe.
In some embodiments of the invention, described oil gas derives the pipeline short transverse multi-tier arrangement along described pyrolysis reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline.
In some embodiments of the invention, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and the respective left and right sides of described heat accumulation type radiant tube is symmetrically arranged with two oil gas and derives pipeline.
In some embodiments of the invention, described oil gas derives 1/2-3 times that spacing is described oil gas derivation pipe diameter d of pipeline and the tube wall of contiguous described heat accumulation type radiant tube.
In some embodiments of the invention, described oil gas is derived and is provided with multiple through hole on the tube wall of pipeline, it is preferable that described through hole is derived at described oil gas and is uniformly distributed on the length direction of pipeline.
In some embodiments of the invention, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
In some embodiments of the invention, between outer wall and the described heat accumulation type radiant tube being adjacent of described second cyclone separator, it is welded with support bar, with fixing described second cyclone separator.
In some embodiments of the invention, this pyrolysis system may further include: breaker；Second feed screw, described second feed screw is connected with described breaker；Coal bunker, described coal bunker is connected with described second feed screw；3rd feed screw, described 3rd feed screw is connected with the feed(raw material)inlet of described coal bunker and described dry riser.
In another aspect of this invention, the invention provides the method utilizing foregoing low order pulverized coal pyrolysis system to carry out low order pulverized coal pyrolysis.According to embodiments of the invention, low order pulverized coal pyrolysis method includes: by the supply of low order fine coal to being dried process with dry riser, obtain the mixed material of flue gas and fine coal；Utilize the first cyclone separator that the mixed material of flue gas and fine coal is carried out gas solid separation process, obtain flue gas and pyrolysis material；Utilize the first feed screw to be added in pyrolysis reactor by described pyrolysis material, and make described pyrolysis material carry out pyrolytic reaction, obtain gas mixture and semicoke.Inventor have found that, utilize the method, it is possible to pyrolysis fine coal fast and effectively, and utilize foregoing pyrolysis system to implement the method, having whole feature and advantage of foregoing pyrolysis system, this is no longer going to repeat them.
In some embodiments of the invention, the particle diameter of described pyrolysis material is 1-3 millimeter.
In some embodiments of the invention, the temperature on described pyrolysis reactor top is 680-730 degree Celsius, and the temperature at middle part is 500-650 degree Celsius, and the temperature of bottom is 500-600 degree Celsius.
The additional aspect of the present invention and advantage will part provide in the following description, and part will become apparent from the description below, or is recognized by the practice of the present invention.
Accompanying drawing explanation
Fig. 1 is the structural representation of pyrolysis system according to an embodiment of the invention.
Fig. 2 is the part-structure schematic diagram of pyrolysis system in accordance with another embodiment of the present invention.
Fig. 3 is the structural representation of pyrolysis system according to still another embodiment of the invention.
Fig. 4 is the schematic flow sheet of method for pyrolysis according to an embodiment of the invention.
Detailed description of the invention
Embodiments of the invention are described below in detail.The embodiments described below is illustrative of, and is only used for explaining the present invention, and is not considered as limiting the invention.Unreceipted concrete technology or condition in embodiment, technology or condition described by the document in this area or carry out according to product description.Agents useful for same or the unreceipted production firm person of instrument, be can pass through city available from conventional products.
In describing the invention, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end ", " interior ", " outward ", " clockwise ", " counterclockwise ", " axially ", " radially ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, it is for only for ease of the description present invention and simplifies description, rather than the device of instruction or hint indication or element must have specific orientation, with specific azimuth configuration and operation, therefore it is not considered as limiting the invention.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, for instance, it is possible to it is fixing connection, it is also possible to be removably connect, or integral；Can be mechanically connected, it is also possible to be electrical connection；Can be joined directly together, it is also possible to be indirectly connected to by intermediary, it is possible to be connection or the interaction relationship of two elements of two element internals, unless otherwise clear and definite restriction.For the ordinary skill in the art, it is possible to understand above-mentioned term concrete meaning in the present invention as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary mediate contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or be merely representative of fisrt feature level height higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be fisrt feature immediately below second feature or obliquely downward, or be merely representative of fisrt feature level height less than second feature.
In one aspect of the invention, the invention provides a kind of low order pulverized coal pyrolysis system.It is described in detail below with reference to Fig. 1-3 couples low order pulverized coal pyrolysis system according to embodiments of the present invention.According to embodiments of the invention, low order pulverized coal pyrolysis system includes: dry riser the 100, first cyclone separator the 200, first feed screw 300 and pyrolysis reactor 400.
According to a particular embodiment of the invention, dry riser 100 is provided with feed(raw material)inlet 110, smoke inlet 120 and mixed material outlet 130.Feed(raw material)inlet 110 is arranged on the sidewall of dry riser 100 bottom and is suitable to dry riser 100 feeding pulverized coal raw material, smoke inlet 120 is arranged in the bottom of dry riser 100 and is suitable to supply heat smoke to dry riser 100, and mixed material outlet 130 is positioned on the sidewall on dry riser 100 top and is suitable to the fine coal raw material through super-dry and preheating is discharged dry riser 100.In dry riser 100, fine coal raw material moves from the bottom to top under the effect of heat smoke, is dried and the pre-heat treatment simultaneously, and the flue gas obtained and the mixture of coal are by mixed material outlet 130 discharge.Supply is to the flue gas that the flue gas dried in riser 100 can be that in heat accumulation type radiant tube, fuel combustion produces, thus, it is possible to realize resource circulation utilization, reduces energy consumption, good economy performance.
According to a particular embodiment of the invention, the first cyclone separator 200 has the first gas-solid mixture entrance the 210, first gas outlet 220 and the first solid outlet 230, and described first gas-solid mixture entrance 210 exports 130 with described mixed material and is connected.First cyclone separator 200 is suitable to be easily separated the mixture of the flue gas obtained through super-dry riser 100 and coal, specifically, the mixture of flue gas and coal enters the first cyclone separator by the first gas-solid mixture entrance 210, the flue gas obtained through gas solid separation is discharged through the first gas outlet 220, separate the pyrolysis material (i.e. fine coal) obtained to discharge through the first solid outlet 230, enter subsequent processing.In some embodiments, in order to reach better separating effect, the first cyclone separator 200 can be two or more, and in this case, multiple first cyclone separator 200 are one another in series, and has illustrated the situation that the first cyclone separator 200 is two in Fig. 1.
According to a particular embodiment of the invention, first feed screw 300 is connected with the first solid outlet 230 of the first cyclone separator, and the pyrolysis material discharged through the first solid outlet 230 is supplied carried out pyrolytic reaction to pyrolysis reactor 400 by the first feed screw 300.
According to a particular embodiment of the invention, pyrolysis reactor 400 is provided with pyrolysis material entrance 410, gas mixture outlet 420, semicoke outlet 430, and this pyrolysis reactor 400 is internally provided with many oil gas and derives pipelines 440, gas gathering manifold 451, many gas-collecting branch pipes 452, heat accumulation type radiant tube 460 and the second cyclone separator 470.
According to a particular embodiment of the invention, pyrolysis material entrance 410 is arranged at the top of pyrolysis reactor 400, is suitable in pyrolysis material supply to reactor.
According to a particular embodiment of the invention, the tops that gas mixture outlet 420 is arranged at pyrolysis reactor 400, and and pyrolysis material entrance 410 interval arrange, the gas mixture being suitable to obtain pyrolysis discharges pyrolysis reactor 400.
According to a particular embodiment of the invention, semicoke outlet 430 is arranged at the bottom of pyrolysis reactor 400, and is suitable to pyrogenous origin semicoke is discharged pyrolysis reactor 400.
According to a particular embodiment of the invention, heat accumulation type radiant tube 460 is in the inside of pyrolysis reactor 400 along the short transverse multi-tier arrangement of pyrolysis reactor, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction.According to a particular embodiment of the invention, to include multiple parallel and equally distributed heat accumulation type radiant tube and each heat accumulation type radiant tube parallel with each heat accumulation type radiant tube in adjacent upper and lower two-layer heat accumulation type radiant tube for every layer of heat accumulation type radiant tube.Concrete example according to the present invention, heat accumulation type radiant tube can be the circle of DN200～300mm or semicircle radial canal.Thus, it is possible to significantly improve the pyrolysis efficiency of pyrolysis material, and then improve pyrolysis oil yield.
According to a particular embodiment of the invention, adjacent heat accumulation type radiant tube left and right center distance can be 300～500mm, and adjacent heat accumulation type radiant tube vertical centre spacing can be 400～800mm.It should be explained that, adjacent heat accumulation type radiant tube left and right center distance can be understood as on same layer in heat accumulation type radiant tube distance in the heart, and adjacent heat accumulation type radiant tube vertical centre spacing can be understood as in the adjacent heat accumulation type radiant tube of adjacent upper and lower two interlayers distance in the heart.
According to a particular embodiment of the invention, the number of plies of multilamellar heat accumulation type radiant tube can be 10-30 layer.Inventor have found that, this kind of structure is arranged and so that reactor temperature field distribution is uniform, such that it is able to significantly improve the pyrolysis efficiency of material, and then can be improved the yield of pyrolysis oil.
According to a particular embodiment of the invention, heat accumulation type radiant tube can be unidirectional, gas heat-accumulated type radial canal, and the heat namely produced by combustion gas by heat accumulation type radiant tube body carries out heat supply in the way of radiation.According to a particular embodiment of the invention, heat accumulation type radiant tube can be provided with gas control valve (not shown).Thus, it is possible to the flow regulating the combustion gas passing into heat accumulation type radiant tube by adjusting gas control valve realizes the accurate temperature controlling to pyrolytic process, such that it is able to significantly improve the pyrolysis efficiency of material, and then improve the yield of pyrolysis oil.
Concrete, the flow etc. that can pass through to adjust the combustion gas passing into heat accumulation type radiant tube realizes the accurate temperature controlling to pyrolytic process, and heat accumulation type radiant tube adopts the combustion system of regularly commutation, the temperature field making single heat accumulation type radiant tube is more or less the same in 30 DEG C, and the every independent temperature control of heat accumulation type radiant tube, thus ensureing the uniformity of reactor temperature field, the flow of the combustion gas such as passing into heat accumulation type radiant tube by adjustment makes pyrolysis reactor be divided into three districts from top to bottom, i.e. drying and dehydrating district, pyrolysis reaction region, semicoke maturation zone, the temperature range in the control realization drying and dehydrating district to heat accumulation type radiant tube can be passed through at 680-730 degree Celsius, it is possible to quickly slough the moisture contained by pyrolysis material, drying and dehydrating district temperature is slightly higher simultaneously, drying and dehydrating section length can be reduced.Pyrolysis reaction region temperature range can control at 500-650 degree Celsius, and to ensure the abundant pyrolysis of material, semicoke maturation zone temperature can control at 500-600 degree Celsius, thus a heating part further does not have the material of complete pyrolysis.
According to a particular embodiment of the invention, gas gathering manifold 451 is arranged on the central shaft of described pyrolysis reactor 400, and one end of gas-collecting branch pipe 452 is connected with described gas gathering manifold 451, and the other end is communicated to described oil gas and derives pipeline 440.The concrete set-up mode of gas-collecting branch pipe 452 is not particularly limited, for instance include but not limited to that the length direction along gas gathering manifold 451 is arranged parallel to each other.According to embodiments of the invention, can having certain angle between gas-collecting branch pipe 452 and gas gathering manifold 451, in some concrete examples, gas-collecting branch pipe 452 is perpendicular to gas collecting main pipe 451 and arranges.Thus, the quick derivation of gas mixture is conducive to.
According to a particular embodiment of the invention, oil gas is derived pipeline 440 and is connected with one end of gas-collecting branch pipe 452, and is provided with through hole on the tube wall of oil gas delivery line.Thus, by arranging oil gas derivation pipeline so that the pyrolysis oil gas produced in pyrolytic process is quickly derived, thus effectively suppressing oil gas second pyrolysis, improves pyrolysis oil yield.According to embodiments of the invention, the quantity of through hole is not particularly limited, and in some concrete examples, oil gas is derived and is provided with multiple through hole on the tube wall of pipeline 440, it is preferable that the plurality of through hole is derived at oil gas and is uniformly distributed on the length direction of pipeline 440.Thus, gas mixture is conducive to quickly to derive.
According to a particular embodiment of the invention, oil gas derives the pipeline 440 short transverse multi-tier arrangement along pyrolysis reactor 400, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline.
According to a particular embodiment of the invention, oil gas is derived pipeline 440 and is arranged in parallel with heat accumulation type radiant tube 460, and the left and right sides of heat accumulation type radiant tube 460 is symmetrically arranged with two oil gas and derives pipeline 440.Inventor have found that, by deriving pipeline at every heat accumulation type radiant tube both sides installation oil gas, the gas mixture that pyrolysis produces is derived rapidly by deriving pipeline, thus restrained effectively the second pyrolysis of oil gas, and then the yield of raising pyrolysis oil, good in economic efficiency.
According to a particular embodiment of the invention, as in figure 2 it is shown, oil gas derives 1/2-3 times that spacing L is oil gas derivation pipe diameter d of pipeline 440 and the tube wall of contiguous heat accumulation type radiant tube 460.Thus can derive the pyrolysis oil gas mixture of generation at once, it is to avoid pyrolysis oil cracks, improve pyrolysis oil productivity.
According to a particular embodiment of the invention, same layer oil gas is derived pipeline 440 and is communicated to same gas-collecting branch pipe 452.Thereby, it is possible to gas mixture is concentrated, is derived rapidly.
According to a particular embodiment of the invention, second cyclone separator 470 has the second gas-solid mixture entrance the 471, second gas outlet 473 and the second solid outlet 472, wherein, second gas outlet 473 exports 420 with gas mixture and is connected, and the end of gas gathering manifold 451 extends the second gas-solid mixture entrance 471 being communicated to this second cyclone separator 470.Inventor have found that, by arranging cyclone separator inside pyrolysis reactor, thermal decomposition product is carried out gas solid separation process, can effectively reduce the dustiness of the gas mixture discharging pyrolysis reactor, effectively suppress the pyrolysis oil gas pyrolysis reactor to mix dust condensation blocking subsequent pipeline and relevant device；Meanwhile, in the built-in pyrolysis reactor of cyclone separator, pyrolysis reactor can be reduced to the lagging facility of pipeline between gas mixture condensing unit, reduce the thermal insulation area of equipment and reduce system heat tracing energy consumption.
According to a particular embodiment of the invention, between outer wall and the heat accumulation type radiant tube 460 being adjacent of the second cyclone separator 470, it is welded with support bar 480, it is possible to be firmly fixed to inside pyrolysis reactor this cyclone separator.Generally, the second cyclone separator 470 is arranged at the top of pyrolysis reactor 400, therefore, it can welding support bar 480 between the second cyclone separator 470 outer wall and ground floor heat accumulation type radiant tube.
According to a particular embodiment of the invention, pyrolysis reactor 400 is additionally provided with the smoke entrance after the required fuel of heat accumulation type radiant tube burning, air and burning simultaneously, fuel gas inlet is connected with heat accumulation type radiant tube 460 respectively with air intake, burn in heat accumulation type radiant tube produce pre-heat smoke through with air heat-exchange after, it is cooled to 90-150 degree Celsius, low-temperature flue gas can smoke inlet 120 supply of drying riser 100 to dry riser 100, for raw material being dried and the pre-heat treatment, further increase pyrolysis reactor efficiency and efficiency of combustion.
According to a particular embodiment of the invention, the height of pyrolysis reactor 400 and width should quite, and width can be 2-6 rice, and the quantity and spacing that highly can pass through to control every layer of heat accumulation type radiant tube controls, and the height of usual pyrolysis reactor can be 5～20m.Thus, it is possible to realize the complete pyrolysis to material.
According to a particular embodiment of the invention, with reference to Fig. 3, the pyrolysis system of the present invention can further include: breaker the 500, second feed screw 600, coal bunker 700 and the 3rd feed screw 800.
According to a particular embodiment of the invention, breaker 500 is for being crushed to 1-3 millimeter by the particle diameter of feed coal.Thus, the fine coal raw material obtained is heated evenly in pyrolysis reactor 400, is conducive to improving efficiency and the pyrolysis oil yield of pyrolytic reaction.
According to a particular embodiment of the invention, the second feed screw 600 is connected with breaker 500, for by the broken fine coal raw material obtained supply to coal bunker 700.
According to a particular embodiment of the invention, coal bunker 700 is connected with the second feed screw 600, is suitable to store fine coal raw material.
According to a particular embodiment of the invention, described 3rd feed screw 800 is connected with the feed(raw material)inlet 110 of coal bunker 700 and dry riser 100, is suitable to extremely dry in riser 100 the fine coal raw material supply being stored in coal bunker 700.
In another aspect of this invention, the invention provides the method utilizing foregoing low order pulverized coal pyrolysis system to carry out low order pulverized coal pyrolysis.According to embodiments of the invention, with reference to Fig. 4, low order pulverized coal pyrolysis method comprises the following steps:
S100: the supply of low order fine coal is dried process to dry riser, obtains the mixed material of flue gas and coal.
According to a particular embodiment of the invention, before carrying out step S100, it is possible to advance with breaker and feed coal is carried out break process so that the particle diameter of broken pyrolysis material subsequently is 1-3 millimeter.Thus, pyrolysis material is heated evenly in pyrolysis reactor, and pyrolytic reaction efficiency is higher, and pyrolysis oil yield is higher.
According to a particular embodiment of the invention, in this step, utilize the flue gas that the burning of the heat accumulation type radiant tube in pyrolysis reactor produces that low order fine coal is dried process, while reducing feed coal water content, low order fine coal the pre-heat treatment be can also be carried out, thus, reactor efficiency and efficiency of combustion further increased, achieve resource circulation utilization, good economy performance.
S200: utilize the first cyclone separator that the mixed material of flue gas and coal is carried out gas solid separation process, obtain flue gas and pyrolysis material.
S300: utilize the first feed screw to be added in pyrolysis reactor by described pyrolysis material, and make described pyrolysis material carry out pyrolytic reaction, obtain gas mixture and semicoke.
According to a particular embodiment of the invention, the temperature on pyrolysis reactor top is 680-730 degree Celsius, and the temperature at middle part is 500-650 degree Celsius, and the temperature of bottom is 500-600 degree Celsius.Specifically, pyrolysis material from top to bottom moves in pyrolysis reactor, sequentially pass through drying and dehydrating district, top, pyrolysis reaction region, middle part and semicoke maturation zone, bottom, moisture is quickly sloughed at drying and dehydrating district pyrolysis material, then pyrolytic reaction is carried out in pyrolysis reaction region, obtain gas mixture and semicoke, gas mixture is derived pipeline by oil gas and is quickly derived, and through gas-collecting branch pipe, gas gathering manifold collects and supplies to the second cyclone separator, pyrolysis reactor is discharged after removing dust, the semicoke obtained continues to move downwardly into semicoke maturation zone, then pass through semicoke outlet and discharge pyrolysis reactor.
Inventor have found that, utilize the method, it is possible to the fine coal of pyrolysis low order fast and effectively, and utilize foregoing pyrolysis system to implement the method, having whole feature and advantage of foregoing pyrolysis system, this is no longer going to repeat them.
Referring to Fig. 3 and Fig. 4, the duty of low order pulverized coal pyrolysis system according to embodiments of the present invention and low order pulverized coal pyrolysis method is described in detail, specific as follows:
nullThe supply of low order fine coal is carried out break process to breaker 500，The granularity obtained supplies to coal bunker 700 storage at the fine coal of 1-3 millimeter through the second feed screw 600，It is stored in the fine coal in coal bunker 700 under the effect of the 3rd feed screw 800 through feed(raw material)inlet 110 supply to dry riser 100，In dry riser 100, pass into flue gas through smoke inlet 120 simultaneously，Under the effect of flue gas，Fine coal moves from the bottom to top，The mixture of flue gas and fine coal blended material outlet 130 and the first gas-solid mixture entrance 210 successively enter the first cyclone separator 200，Gas after separation is discharged through the first gas outlet 220，Separate the solid obtained and enter the first feed screw 300 through the first solid outlet 230，Under the progradation of the first feed screw 300，It is supplied in pyrolysis reactor 400，Heat accumulation type radiant tube 460 provides the temperature field being suitable for for pyrolysis reactor 400 simultaneously，Inside pyrolysis reactor 400，Pyrolysis material from top to bottom moves，Sequentially pass through drying and dehydrating district、Pyrolysis reaction region and semicoke maturation zone，Pyrolysis material generates gas mixture and semicoke through pyrolytic reaction，Wherein，The through hole that gas mixture derives pipeline 440 by oil gas rapidly enters oil gas derivation pipeline，And sequentially enter the gas-collecting branch pipe 452 communicated therewith、Gas gathering manifold 451，Then pass through the second gas-solid mixture entrance 471 and enter the second cyclone separator 470，The solid obtained after gas solid separation enters pyrolysis reactor by the second solid outlet 472，430 discharge pyrolysis reactors are exported through semicoke together with semicoke，Separate the gas obtained and export 420 discharge pyrolysis reactors through the second gas outlet 473 and gas mixture successively，Enter subsequent treatment operation.
Below with reference to specific embodiment, present invention is described, it is necessary to explanation, and these embodiments are only illustrative, and do not limit the present invention in any way.
Embodiment
It is as follows that fine coal is carried out pyrolysis processing, pyrolysis material and pyrolysis reactor parameters by the pyrolysis system utilizing the present invention:
The Industrial Analysis of Yulin brown coal: Mad%, 6.75%, Vad%, 31.59%, Aad%, 5.41%, Fcad%, 56.25%, coal crushes particle diameter 1～3mm.
Technological parameter: pyrolysis reactor upper temp 580 DEG C, middle portion temperature 605 DEG C, temperature of lower 594 DEG C, gas mixture outlet temperature 583 DEG C, cyclone separator gas outlet temperature 565 DEG C, pyrolysis reactor internal pressure 4.73Kpa, pyrolysis oil gas mixture exports thin dirt removal efficiency 95%, exports dustiness 85mg/Kg.Pyrolysis oven adopts the circle of DN250, and radial canal left and right center distance 300mm, vertical centre spacing is 450mm, and the radial canal number of plies is advisable at about 20 layers, and reactor width is 4.5m, is highly 15m.
Pyrolysis tertiary industry is distributed: tar 17.4%, pyrolysis gas 12.8%, semicoke 69.8%.
In describing the invention, term " first ", " second " only for descriptive purposes, and it is not intended that instruction or hint relative importance or the implicit quantity indicating indicated technical characteristic.Thus, define " first ", the feature of " second " can express or implicitly include one or more these features.In describing the invention, " multiple " are meant that two or more, unless otherwise expressly limited specifically.
In the description of this specification, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means in conjunction with this embodiment or example describe are contained at least one embodiment or the example of the present invention.In this manual, the schematic representation of above-mentioned term is necessarily directed to identical embodiment or example.And, the specific features of description, structure, material or feature can combine in one or more embodiments in office or example in an appropriate manner.Additionally, when not conflicting, the feature of the different embodiments described in this specification or example and different embodiment or example can be carried out combining and combining by those skilled in the art.
Although above it has been shown and described that embodiments of the invention, it is understandable that, above-described embodiment is illustrative of, it is impossible to be interpreted as limitation of the present invention, and above-described embodiment can be changed, revises, replace and modification by those of ordinary skill in the art within the scope of the invention.
Claims (10)
1. a low order pulverized coal pyrolysis system, it is characterised in that including:
Dry riser, described dry riser is provided with feed(raw material)inlet, smoke inlet and mixed material outlet, described feed(raw material)inlet is positioned on the sidewall of described dry riser bottom, described smoke inlet is positioned at the bottom of described dry riser, and the outlet of described mixed material is positioned on the sidewall on described dry riser top；
First cyclone separator, described first cyclone separator has the first gas-solid mixture entrance, the first gas outlet and the first solid outlet, described first gas-solid mixture entrance and described mixed material outlet；
First feed screw, described first feed screw is connected with described first solid outlet；
Pyrolysis reactor, described pyrolysis reactor is provided with pyrolysis material entrance, gas mixture outlet and semicoke outlet, described pyrolysis reactor is internally provided with many oil gas and derives pipelines, gas gathering manifold, many gas-collecting branch pipes, heat accumulation type radiant tube and the second cyclone separator
Wherein, described pyrolysis material entrance is connected with described first feed screw,
Described gas gathering manifold is arranged on the central shaft of described pyrolysis reactor,
One end of described gas-collecting branch pipe is connected with described gas gathering manifold, and the other end is communicated to described oil gas and derives pipeline；
Described second cyclone separator has the second gas-solid mixture entrance, the second gas outlet and the second solid outlet, wherein, described second gas outlet is connected with the outlet of described gas mixture, and the end of described gas gathering manifold extends the second gas-solid mixture entrance being communicated to described second cyclone separator；
Described heat accumulation type radiant tube is along the short transverse multi-tier arrangement of described pyrolysis reactor, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction.
2. low order pulverized coal pyrolysis system according to claim 1, it is characterised in that described gas-collecting branch pipe is arranged parallel to each other along the length direction of described gas gathering manifold,
Optional, described gas-collecting branch pipe is perpendicular to described gas collecting main pipe.
3. low order pulverized coal pyrolysis system according to claim 1, it is characterised in that described oil gas derives the pipeline short transverse multi-tier arrangement along described pyrolysis reactor, every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline,
Optional, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and the respective left and right sides of described heat accumulation type radiant tube is symmetrically arranged with two oil gas and derives pipeline,
Optional, described oil gas derives 1/2-3 times that spacing is described oil gas derivation pipe diameter d of pipeline and the tube wall of contiguous described heat accumulation type radiant tube.
4. the low order pulverized coal pyrolysis system according to any one of claim 1-3, it is characterised in that described oil gas is derived and is provided with multiple through hole on the tube wall of pipeline, it is preferable that described through hole is derived at described oil gas and is uniformly distributed on the length direction of pipeline.
5. low order pulverized coal pyrolysis system according to claim 4, it is characterised in that oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
6. low order pulverized coal pyrolysis system according to claim 1, it is characterised in that be welded with support bar between outer wall and the described heat accumulation type radiant tube being adjacent of described second cyclone separator, with fixing described second cyclone separator.
7. low order pulverized coal pyrolysis system according to claim 1, it is characterised in that farther include:
Breaker；
Second feed screw, described second feed screw is connected with described breaker；
Coal bunker, described coal bunker is connected with described second feed screw；
3rd feed screw, described 3rd feed screw is connected with the feed(raw material)inlet of described coal bunker and described dry riser.
8. utilize the method that the low order pulverized coal pyrolysis system according to any one of claim 1-7 carries out low order pulverized coal pyrolysis, it is characterised in that including:
The supply of low order fine coal is dried process to dry riser, obtains the mixed material of flue gas and fine coal；
Utilize the first cyclone separator that the mixed material of described flue gas and fine coal is carried out gas solid separation process, obtain flue gas and pyrolysis material；
Utilize the first feed screw to be added in pyrolysis reactor by described pyrolysis material, and make described pyrolysis material carry out pyrolytic reaction, obtain gas mixture and semicoke.
9. method according to claim 8, it is characterised in that the particle diameter of described pyrolysis material is 1-3 millimeter.
10. method according to claim 8, it is characterised in that the temperature on described pyrolysis reactor top is 680-730 degree Celsius, and the temperature at middle part is 500-650 degree Celsius, and the temperature of bottom is 500-600 degree Celsius.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107057735A (en) * | 2017-05-25 | 2017-08-18 | 北京神雾电力科技有限公司 | Fine coal high/low temperature thermal decomposition integrated reactor and its application |
| CN112745868A (en) * | 2019-10-29 | 2021-05-04 | 中国石油化工股份有限公司 | Pyrolysis device, pyrolysis system and pyrolysis method for coal and biological carbonaceous raw materials |
| CN114348684A (en) * | 2020-10-13 | 2022-04-15 | 核工业北京化工冶金研究院 | Continuous automatic feeding device and method for triuranium octoxide |
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2016
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107057735A (en) * | 2017-05-25 | 2017-08-18 | 北京神雾电力科技有限公司 | Fine coal high/low temperature thermal decomposition integrated reactor and its application |
| CN112745868A (en) * | 2019-10-29 | 2021-05-04 | 中国石油化工股份有限公司 | Pyrolysis device, pyrolysis system and pyrolysis method for coal and biological carbonaceous raw materials |
| CN114348684A (en) * | 2020-10-13 | 2022-04-15 | 核工业北京化工冶金研究院 | Continuous automatic feeding device and method for triuranium octoxide |
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