CN105567267A - System and method for pyrolyzing coal - Google Patents
System and method for pyrolyzing coal Download PDFInfo
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- CN105567267A CN105567267A CN201610098982.1A CN201610098982A CN105567267A CN 105567267 A CN105567267 A CN 105567267A CN 201610098982 A CN201610098982 A CN 201610098982A CN 105567267 A CN105567267 A CN 105567267A
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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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Abstract
The invention discloses a system and method for pyrolyzing coal. The system comprises a moving bed pyrolysis reactor and a spray tower; the reactor comprises a coal material inlet, a semicoke outlet, regenerative radiant tubes, oil gas exporting pipelines, a stirring device and gas collecting tubes; the regenerative radiant tubes are arranged in the reactor in the height direction of the reactor for multiple layers, and multiple regenerative radiant tubes which are parallel to one another in the horizontal direction are arranged on each layer; through holes are formed in the pipe walls of the oil gas exporting pipelines; the stirring device comprises a stirring shaft and multiple stirring rods connected to the stirring shaft; the gas collecting tubes comprise the gas collecting header tube and the gas collecting branch tubes, and the gas collecting header tube is connected with the spray tower. According to the system, powdered coal can be effectively treated, and the treatment efficiency is high; meanwhile, oil gas resources generated through pyrolysis can be quickly exported, secondary reactions are few, the tar oil quality is high, and the content of light components in tar oil is high; in addition, due to the fact that the regenerative radiant tubes are adopted in the pyrolysis reactor and rotatable inner elements are arranged in the regenerative radiant tubes, heat transfer among particles and between the particles and the radiant tubes is increased, and the heat transfer efficiency is high.
Description
Technical field
The invention belongs to chemical field, specifically, the present invention relates to a kind of system and method for pyrolyzing coal.
Background technology
The energy structure feature of China is rich coal, oil-poor, weak breath, and as coal production maximum in the world and country of consumption, within one quite long period, the status that coal resources dominate the energy as China is unshakable.According to statistics, it is 1,145 hundred million tons that China has verified coal reserves, and wherein, low-rank coal (brown coal, lower-grade metamorphic bituminous) accounts for again about 55.15% of national reserves.Because low-rank coal has that moisture content is high, easy-weathering nature, is difficult to sorting, should not transports for long-distance and the feature such as storage, 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-rank coal is directly burnt as steam coal fuel, not only waste the hydrocarbon rich resource contained in coal, and efficiency is low.By low-temperature pyrolysis of coal and coal-char combustion, decoupling zero of gasifying, realizing low-rank 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, the ratio of lump coal is declined (declining 10 ~ 20% by current 40%), and fine coal productive rate raises (rising to 80 ~ 90% by current 60%).The problems such as fine coal exists easy airborne dust, inflammable, explosive, and comprehensive utilization difficulty is large.
Therefore, existing pyrolysis of coal technology remains to be further improved.
Summary of the invention
The present invention is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, one object of the present invention is the system and method proposing a kind of pyrolyzing coal, and this system effectively can process fine coal, and processing efficiency is high, the hydrocarbon resources that pyrolysis simultaneously produces can be derived rapidly, secondary reaction is few, and tar quality is high, and in tar, light component content is high, pyrolysis reactor adopts heat accumulation type radiant tube in addition, and inside arranges rotation inner member, add between particle and conduct heat between particular radiation pipe, heat transfer efficiency is high.
In one aspect of the invention, the present invention proposes a kind of system of pyrolyzing coal.According to embodiments of the invention, this system comprises:
Moving bed pyrolysis reactor and spray column,
Wherein, described moving bed pyrolysis reactor comprises:
Coal charge entrance and semicoke outlet;
Described coal charge entrance is positioned at the top of described reactor;
Described semicoke outlet is positioned at the bottom of described reactor;
Heat accumulation type radiant tube, the short transverse multilayer of described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along described reactor is arranged, every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Oil gas derives pipeline, and the tube wall of described oil gas derivation pipeline is provided with through hole;
Whipping appts, described whipping appts comprises stir shaft and is connected to the multiple agitator arms on described stir shaft, and described stir shaft is extend into the inside of described reactor by described semicoke outlet and is configured to rotate in described reactor;
Effuser, the gas-collecting branch pipe that described effuser comprises gas gathering manifold and is connected with described gas gathering manifold,
Wherein, it is outside that described gas gathering manifold is arranged on described reactor vertically, and described gas gathering manifold is connected with described spray column,
The sidewall that described gas-collecting branch pipe extends through described reactor to extend in described reactor and derives pipeline with described oil gas and is connected.
Thus, system according to the pyrolyzing coal of the embodiment of the present invention effectively can process fine coal, and processing efficiency is high, the hydrocarbon resources that pyrolysis simultaneously produces can be derived rapidly, and secondary reaction is few, tar quality is high, in tar, light component content is high, and pyrolysis reactor adopts heat accumulation type radiant tube in addition, and inside arranges rotation inner member, add between particle and conduct heat between particular radiation pipe, heat transfer efficiency is high.
In addition, the system of pyrolyzing coal according to the above embodiment of the present invention can also have following additional technical characteristic:
In some embodiments of the invention, described gas-collecting branch pipe is multiple, and arranged parallel to each other along the length direction of described gas gathering manifold.Thus, the oil gas that can significantly improve in reactor derives efficiency.
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 is derived pipeline and is arranged along the short transverse multilayer of described reactor, and every layer has many oil gas derivation pipelines parallel to each other in the horizontal direction.Thus, the oil gas that can improve further in reactor derives efficiency.
In some embodiments of the invention, described oil gas derives pipeline and described heat accumulation type radiant tube is arranged in parallel, and the described heat accumulation type radiant tube left and right sides is separately symmetrically arranged with two oil gas derivation pipelines.Thus, the oil gas that can improve further in reactor derives efficiency.
In some embodiments of the invention, described oil gas derives pipeline with the spacing of the tube wall of contiguous described heat accumulation type radiant tube is that described oil gas derives the 1/2-3 of pipe diameter d doubly.
In some embodiments of the invention, the tube wall that described oil gas derives pipeline is provided with multiple through hole.Thus, the oil gas that can improve further in reactor derives efficiency.
In some embodiments of the invention, described through hole is uniformly distributed on the length direction of described oil gas derivation 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, all there is one or more agitator arm the top of every layer of radiator tube, and the vertical range of agitator arm and radiator tube is 20 ~ 300mm.Thereby, it is possible to enhancement of heat transfer effect.Such as, agitator arm can between radiation tube layer and oil gas delivery line channel layer.
In some embodiments of the invention, described agitator arm is perpendicular to described stir shaft, and spaced apart along the length direction of described stir shaft.Thus, the yield of pyrolytic tar can be improved further.
In some embodiments of the invention, the adjacent projections of described agitator arm on the same cross section of described stir shaft at an angle.Thus, the yield of pyrolytic tar can be improved further.
In some embodiments of the invention, the angle ranging from 0 ~ 90 degree, not containing end value, preferably, the angle ranging from 30 ~ 90 degree, not containing 90 degree.Thus, the yield of pyrolytic tar can be improved further.
In some embodiments of the invention, the system of described pyrolyzing coal comprises further: crusher, and described crusher has lump coal entrance and broken coal export; First conveyor screw, described first conveyor screw has the first opening for feed and the first discharge port, and described first opening for feed is connected with described broken coal export; Coal bunker, described coal bunker has coal bunker import and coal bunker outlet, and described coal bunker import is connected with described first discharge port; Second conveyor screw, described second conveyor screw has the second opening for feed and the second discharge port, and described second opening for feed exports with described coal bunker and is connected; Dry riser tube, described dry riser tube has the outlet of smoke inlet, fine coal opening for feed and mixture, and described smoke inlet is connected with the exhanst gas outlet on described heat accumulation type radiant tube, and described fine coal opening for feed is connected with described second discharge port; First cyclonic separator, described first cyclonic separator has mixture entrance, offgas outlet and dry discharge, and described mixture entrance exports with described mixture and is connected; 3rd conveyor screw, described 3rd conveyor screw has the 3rd opening for feed and the 3rd discharge port, and described 3rd opening for feed is connected with described dry discharge, and described 3rd discharge port is connected with described coal charge entrance; 4th conveyor screw, the below and exporting with described semicoke that described 4th conveyor screw is arranged on described moving bed pyrolysis reactor is connected.Thus, when making fine coal enter stove, moisture is little, and heat dissipation is few, thus can improve the pyrolysis efficiency of fine coal further.
In some embodiments of the invention, the system of described pyrolyzing coal comprises further: the second cyclonic separator, and described second cyclonic separator has oil and gas import, solid particulate outlet and purification oil gas vent, and described oil and gas import is connected with described gas gathering manifold; Cleaning apparatus, described cleaning apparatus has oil gas vent after dedusting oil gas entrance and dedusting, and described dedusting oil gas entrance is connected with described purification oil gas vent, and after described dedusting, oil gas vent is connected with described spray column.Thus, tar and combustion gas quality can be significantly improved.
In some embodiments of the invention, the system of described pyrolyzing coal comprises further: tar groove, and described tar groove has tar entrance, light oil outlet, heavy oil outlet and coke tar refuse outlet, and described tar entrance is connected with described spray column; Blower fan, described blower fan has fuel gas inlet and gas outlet, and described fuel gas inlet is connected with described spray column; And gas-holder, described gas-holder is connected with described gas outlet.
In another aspect of the present invention, the present invention proposes a kind of method of pyrolyzing coal.According to embodiments of the invention, the method for this pyrolyzing coal adopts the system of described pyrolyzing coal to carry out.According to a particular embodiment of the invention, the method comprises:
Coal is delivered in described moving bed pyrolysis reactor and carries out pyrolysis processing, to obtain semicoke and pyrolysis oil gas;
Described pyrolysis oil gas is delivered in described spray column and carries out spray process, to obtain tar and combustion gas.
Thus, method according to the pyrolyzing coal of the embodiment of the present invention effectively can process fine coal, and processing efficiency is high, the hydrocarbon resources that pyrolysis simultaneously produces can be derived rapidly, and secondary reaction is few, tar quality is high, in tar, light component content is high, and pyrolysis reactor adopts heat accumulation type radiant tube in addition, and inside arranges rotation inner member, add between particle and conduct heat between particular radiation pipe, heat transfer efficiency is high.
In one embodiment of the invention, the method of described pyrolyzing coal comprises further: described pyrolysis oil gas is supplied in described spray column carry out spray process before, described pyrolysis oil gas is supplied in described second cyclonic separator and described cleaning apparatus carries out cyclonic separation and dust removal process successively in advance.Thus, the quality of tar and combustion gas can be significantly improved.
Additional aspect of the present invention and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage will become obvious and easy understand from accompanying drawing below combining to the description of embodiment, wherein:
Fig. 1 is the system architecture schematic diagram of pyrolyzing coal according to an embodiment of the invention;
Fig. 2 is the vertical view of the whipping appts in the system of pyrolyzing coal according to an embodiment of the invention;
Fig. 3 is the system architecture schematic diagram of the pyrolyzing coal according to another embodiment of the present invention;
Fig. 4 is the system architecture schematic diagram of the pyrolyzing coal according to another embodiment of the present invention;
Fig. 5 is the system architecture schematic diagram of the pyrolyzing coal according to another embodiment of the present invention;
Fig. 6 is the method flow schematic diagram of pyrolyzing coal according to an embodiment of the invention;
Fig. 7 is the method flow schematic diagram of the pyrolyzing coal according to another embodiment of the present invention;
Fig. 8 is the method flow schematic diagram of the pyrolyzing coal according to another embodiment of the present invention.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the present invention, and can not limitation of the present invention be interpreted as.
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 ", " axis ", " radial direction ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, only the present invention for convenience of description and simplified characterization, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore limitation of the present invention can not be interpreted as.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise at least one this feature.In describing the invention, the implication of " multiple " is at least two, such as two, three etc., unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements, unless otherwise clear and definite restriction.For the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood 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 indirect contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " below " and " below " can be fisrt feature immediately below second feature or tiltedly below, or only represent that fisrt feature level height is less than second feature.
In one aspect of the invention, the present invention proposes a kind of system of pyrolyzing coal.System below with reference to the pyrolyzing coal of Fig. 1-5 pairs of embodiment of the present invention is described in detail.According to embodiments of the invention, this system comprises: moving bed pyrolysis reactor 100 and spray column 200.
According to embodiments of the invention, moving bed pyrolysis reactor 100 comprises: coal charge entrance 101, heat accumulation type radiant tube 11, oil gas derive pipeline 12, semicoke outlet 102, whipping appts 13 and effuser 14.
According to embodiments of the invention, coal charge entrance 101 is positioned at the top of reactor, and is suitable for coal charge to be supplied in reactor.
According to embodiments of the invention, semicoke outlet 102 can be arranged on the bottom of reactor, and is suitable for pyrogenous origin semicoke to discharge reactor.
According to embodiments of the invention, heat accumulation type radiant tube 11 is arranged along the short transverse multilayer of reactor in the inside of moving bed pyrolysis reactor, 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, heat accumulation type radiant tube parallel to each other is in the horizontal direction uniformly distributed, preferably, the heat accumulation type radiant tube arranged along the short transverse of reactor is parallel to each other and be staggeredly arranged.According to concrete example of the present invention, the caliber of heat accumulation type radiant tube can be 100 ~ 300mm.According to embodiments of the invention, the horizontal throw between adjacent heat accumulation type radiant tube outer wall is 200 ~ 500mm, and the vertical distance between adjacent heat accumulation type radiant tube outer wall is 200 ~ 700mm.It should be explained that, horizontal throw between adjacent heat accumulation type radiant tube outer wall can be understood as the distance on same layer between heat accumulation type radiant tube outer wall, and the vertical distance between adjacent heat accumulation type radiant tube outer wall can be understood as adjacent upper and lower two interlayers adjacent heat accumulation type radiant tube outer wall between distance.
According to embodiments of the invention, the number of plies of multilayer heat accumulation type radiant tube can be 10-25 layer.Contriver finds, this kind of structural arrangement can make reactor temperature field distribution even, thus can significantly improve the pyrolysis efficiency of coal charge.
According to embodiments of the invention, heat accumulation type radiant tube can be unidirectional regenerative gas heat accumulation type radiant tube, and the heat namely produced by combustion gas by heat accumulation type radiant tube body carries out heat supply in the mode 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, the flow passing into the combustion gas of heat accumulation type radiant tube can be regulated to wait the accurate temperature controlling realized pyrolytic process by adjustment gas control valve, thus the pyrolysis efficiency of coal charge can be significantly improved, and then improve the yield of pyrolytic tar.
Concrete, heat accumulation type radiant tube to extend into from the side of sidewall of reactor in the horizontal direction reactor and runs through reactor, namely heat accumulation type radiant tube to stretch into from the side of sidewall of reactor in the horizontal direction reactor and passes another sidewall of reactor, and sidewall of reactor is all stretched out in the two ends of heat accumulation type radiant tube, wherein, fuel inlet on heat accumulation type radiant tube is positioned at the one end of heat accumulation type radiant tube stretching out reactor, exhanst gas outlet on heat accumulation type radiant tube is positioned at the other end heat accumulation type radiant tube stretching out reactor, or the fuel inlet on heat accumulation type radiant tube and exhanst gas outlet are positioned at the same one end on heat accumulation type radiant tube.The accurate temperature controlling of the realizations such as the flow of the combustion gas of heat accumulation type radiant tube to pyrolytic process is passed into by adjustment, and heat accumulation type radiant tube adopts the combustion system of regularly commutation, the temperature field of single heat accumulation type radiant tube is made to be more or less the same in 30 DEG C, thus ensure the homogeneity of reactor temperature field, such as the adjustment temperature range of the heat accumulation type radiant tube in epimere region in reactor is made to be 500 ~ 800 DEG C by adjusting the flow passing into the combustion gas of heat accumulation type radiant tube, ensure the abundant pyrolysis of coal charge, the flow being passed into the combustion gas of heat accumulation type radiant tube by adjustment makes the adjustment temperature range of the heat accumulation type radiant tube in hypomere region in reactor be 450 ~ 650 DEG C, thus a heating part does not further have the coal charge of complete pyrolysis.
According to embodiments of the invention, the tube wall of oil gas derivation pipeline 12 is provided with through hole, according to a particular embodiment of the invention, oil gas is derived pipeline 12 and is arranged along the short transverse multilayer of reactor, and every layer has many oil gas derivation pipelines parallel to each other in the horizontal direction.
According to a particular embodiment of the invention, oil gas is derived pipeline 12 and is arranged in parallel with heat accumulation type radiant tube 11, and the left and right sides of heat accumulation type radiant tube 11 is symmetrically arranged with two oil gas derivation pipelines 12.Contriver finds, derive pipeline by installing oil gas in every root heat accumulation type radiant tube both sides, the oil gas that pyrolysis produces is derived pipeline by oil gas and is derived rapidly, thus restrained effectively the second pyrolysis of oil gas, and then improve the yield of pyrolytic tar, good in economic efficiency.According to concrete example of the present invention, the caliber that oil gas derives pipeline can be 30 ~ 80mm.
According to a particular embodiment of the invention, oil gas derives pipeline with the spacing of the tube wall of contiguous heat accumulation type radiant tube is that oil gas derives the 1/2-3 of pipe diameter d doubly.The pyrolytic tar of generation can be derived thus at once, avoid pyrolytic tar cracking, improve pyrolytic tar productive rate.
According to a particular embodiment of the invention, the tube wall of oil gas derivation pipeline 12 is provided with multiple through hole, preferably, multiple through hole is derived on the length direction of pipeline 12 at oil gas and is uniformly distributed.Thus can so that pyrolytic tar be derived fast.
According to embodiments of the invention, multiple agitator arms 16 that whipping appts 13 comprises stir shaft 15 and is connected on stir shaft 15, thus stir shaft 15 drives agitator arm 16 to rotate under the driving of drive-motor, according to a particular embodiment of the invention, stir shaft 15 rotatably extend into inside reactor from semicoke outlet 102.Invention finds, by arranging whipping appts in reactor, agitator arm, in the process carrying out back rotation, effectively can avoid the coking on radiator tube surface, and then avoids reducing heat transfer efficiency because of radiator tube coking, thus can enhance heat transfer effect.
According to a particular embodiment of the invention, all there is one or more agitator arm the top of every layer of radiator tube, and the vertical range of agitator arm and radiator tube is 20 ~ 300mm.Can avoid the upper coking of radiator tube thus, guarantee equipment normally runs.Such as, agitator arm can between radiation tube layer and oil gas delivery line channel layer.
According to a particular embodiment of the invention, agitator arm 16 is perpendicular to stir shaft 15, and spaced apart along the length direction of stir shaft 15.
According to a particular embodiment of the invention, the adjacent projections of agitator arm 16 on the same cross section of stir shaft 15 at an angle.Such as, as shown in Figure 2, described angle θ can be 0 ~ 90 degree (not containing end value), preferably 30 ~ 90 degree (not containing 90 degree).Thus, agitator arm can be made effectively to loosen inside reactor coal charge, thus oil gas pyrolytic tar can be derived fast.Concrete, the length of central stirring shaft can be 1-18m, and detachable agitator arm vertical spacing can be 0.4-1m, and the number of plies can be 11-26 layer.
According to embodiments of the invention, the gas-collecting branch pipe 18 that effuser 14 comprises gas gathering manifold 17 and is communicated with gas gathering manifold 17, according to a particular embodiment of the invention, gas gathering manifold 17 is arranged on reactor outside vertically, and the sidewall that gas-collecting branch pipe 18 extends through reactor to extend in reactor and derives pipeline 12 with oil gas and is connected.Thus, enter oil gas derivation pipeline pyrolytic tar gas and be collected to gas gathering manifold through gas-collecting branch pipe.
According to a particular embodiment of the invention, gas-collecting branch pipe 18 is multiple, and multiple gas-collecting branch pipe 18 can be arranged parallel to each other along the length direction of gas gathering manifold 17, and according to concrete example of the present invention, gas-collecting branch pipe 18 is perpendicular to gas collecting main pipe 17.Thus, multiple gas-collecting branch pipe can ensure that oil gas derives the quick derivation of pyrolytic tar gas in pipeline, thus significantly improves the yield of pyrolytic tar.
According to concrete example of the present invention, as shown in Figure 1, same layer oil gas is derived pipeline 12 and is communicated to same gas-collecting branch pipe 18.
According to embodiments of the invention, reactor head can spherically type or taper.
According to embodiments of the invention, the bottom of reactor can be back taper.Thus, pyrogenous origin semicoke can be made to discharge reactor smoothly.
According to embodiments of the invention, spray column 200 has pyrolysis oil gas entrance 201, spray liquid entrance 202, tar outlet 203 and fuel gas outlet 204, pyrolysis oil gas entrance 201 is connected with gas gathering manifold 17, and be suitable for adopting spray liquid to carry out spray to pyrolysis oil gas and process, thus can be separated and obtain tar and combustion gas.It should be noted that, those skilled in the art can select the particular type of spray liquid according to actual needs, such as, can be the combination of one or more forms in ammoniacal liquor, water, washing oil or pyrolytic tar.Concrete, pyrolysis oil gas is entered in spray column by top or bottom, and spray liquid following current or the heat exchange of counter current contact mass transfer.
System according to the pyrolyzing coal of the embodiment of the present invention effectively can process coal dust, and processing efficiency is high, simultaneously by using many group heat accumulation type radiant tubes to provide thermal source for pyrolytic process, the flow that can pass into the combustion gas of heat accumulation type radiant tube by adjustment realizes the accurate temperature controlling to pyrolytic process, and heat accumulation type radiant tube passes through heat storage type combustion, ensure that the homogeneity in temperature field, thus the pyrolysis efficiency of coal charge can be significantly improved, and then improve the yield of pyrolytic tar, more traditional use gaseous heat-carrier or solid thermal carriers are compared as the pyrolytic reaction device of pyrolysis thermal source simultaneously, moving bed pyrolysis reactor of the present invention does not need to arrange preheating unit and carrier separating unit, thus can greatly simplify pyrolytic reaction technical process, and then significantly reduce device failure rate and in gained pyrolytic tar dust content lower, and funnel temperature is low, secondly the present invention is by arranging that in the bottom of heat accumulation type radiant tube oil gas derives pipeline, the oil gas that pyrolysis produces can be derived rapidly, thus restrained effectively the second pyrolysis of oil gas, and then improve the yield of pyrolytic tar, and pyrolysis gas is not diluted by gaseous heat-carrier, pyrolysis gas calorific value is high, good in economic efficiency, secondly heat accumulation type radiant tube is coordinated by arranging whipping appts in reactor, agitator arm is in the process carrying out back rotation, make to pile up coal charge to be loosened, increase the voidage of piling up between coal charge, reduce the pressure drop of pyrolytic tar gas through coal charge layer, make the pyrolytic tar gas produced can pass rapidly through coal charge layer and arrive oil gas delivery line, the pyrolytic tar gas produced can be derived by oil gas delivery line in time, and the coking of radiator tube upper end can be avoided, thus avoid affecting heat transfer efficiency, additionally by employing spray column, spray process is carried out to pyrolysis oil gas, can be separated and obtain tar and combustible gas, increase economic efficiency.
With reference to figure 3, the method for pyrolyzing coal comprises further according to an embodiment of the invention: crusher 300, first conveyor screw 400, coal bunker 500, second conveyor screw 600, dry riser tube 700, first cyclonic separator 800, the 3rd conveyor screw 900 and the 4th conveyor screw 1000.
According to embodiments of the invention, crusher 300 has lump coal entrance 301 and broken coal export 302, and is suitable for carrying out break process to lump coal (middle low-rank coal), thus can obtain broken coal.According to a particular embodiment of the invention, the particle diameter of broken coal can be below 3mm.
According to embodiments of the invention, the first conveyor screw 400 has the first opening for feed 401 and the first discharge port 402, first opening for feed 401 is connected with broken coal export 302, and is suitable for transporting broken coal in follow-up coal bunker.
According to embodiments of the invention, coal bunker 500 has coal bunker import 501 and coal bunker outlet 502, and coal bunker import 501 is connected with the first discharge port 402, and is suitable for storing the broken coal obtained through the first conveyor screw.
According to embodiments of the invention, the second conveyor screw 600 has the second opening for feed 601 and the second discharge port 602, second opening for feed 601 and exports 502 with coal bunker and be connected, and is suitable for the broken coal in coal bunker to be supplied in follow-up dry riser tube.
According to embodiments of the invention, dry riser tube 700 has smoke inlet 701, fine coal opening for feed 702 and mixture outlet 703, smoke inlet 701 is connected with the exhanst gas outlet (not shown) on heat accumulation type radiant tube, fine coal opening for feed 702 is connected with the second discharge port 602, and the heat smoke being suitable for adopting heat accumulation type radiant tube to produce promotes and drying treatment broken coal, to obtain the mixture containing dry fine coal and flue gas.Thus, not only can realize the efficiency utilization of waste heat, and when making fine coal enter stove, moisture is little, heat dissipation is few, thus can improve the pyrolysis efficiency of fine coal further.Concrete, the heat smoke temperature produced in heat accumulation type radiant tube is about 200 DEG C, and it contacts realization with broken coal and dehydrates, the heat smoke temperature after heat exchange about about 100 DEG C, through the dried fine coal water content control of heat smoke at below 10wt%.
According to embodiments of the invention, first cyclonic separator 800 has mixture entrance 801, offgas outlet 802 and dry discharge 803, mixture entrance 801 and mixture export 703 and are connected, and be suitable for the mixture containing dry fine coal and flue gas obtained in dry riser tube to carry out cyclonic separation process, thus obtain tail gas and dry fine coal respectively.It should be noted that, those skilled in the art can need to adopt secondary cyclone according to substantial sepn.
According to embodiments of the invention, 3rd conveyor screw 900 has the 3rd opening for feed 901 and the 3rd discharge port 902,3rd opening for feed 901 is connected with dry discharge 803,3rd discharge port 902 is connected with coal charge entrance 101, and is suitable for the dry fine coal that separation obtains to be supplied in reactor to carry out pyrolysis processing.
According to embodiments of the invention, the 4th conveyor screw 1000 is located at the below of moving bed pyrolysis reactor 100 and exports 102 with semicoke and be connected.
With reference to figure 4, the method for pyrolyzing coal comprises further according to an embodiment of the invention: the second cyclonic separator 1100 and cleaning apparatus 1200.
According to embodiments of the invention, second cyclonic separator 1100 has oil and gas import 1101, solid particulate outlet 1102 and purification oil gas vent 1103, oil and gas import 1101 is connected with gas gathering manifold 17, and be suitable for the pyrolysis of collecting in gas gathering manifold oil gas is supplied in spray column carry out spray process before, in advance pyrolysis oil gas is supplied to the second rotary separator and carries out cyclonic separation process, thus the solid particulate being purified oil gas and containing semicoke can be separated.Thus, the quality of gained tar and combustion gas can be significantly improved.
According to embodiments of the invention, cleaning apparatus 1200 has oil gas vent 1202 after dedusting oil gas entrance 1201 and dedusting, dedusting oil gas entrance 1201 is connected with purification oil gas vent 1103, after dedusting, oil gas vent 1202 is connected with pyrolysis oil gas entrance 201, and is suitable for resupplying after the purification obtained in the second cyclonic separator oil gas is carried out dust removal process to spray column, carries out spray process.Thus, the quality of gained tar and combustion gas can be improved further.It should be noted that, those skilled in the art can select the particular type of fly-ash separator according to actual needs, and such as cleaning apparatus can be one or more forms combination in a fly-ash separator, electrostatic precipitator, metallic filter etc.
With reference to figure 5, the method for pyrolyzing coal comprises further according to an embodiment of the invention: tar groove 1300, blower fan 1400 and gas-holder 1500.
According to embodiments of the invention, tar groove 1300 has tar entrance 1301, light oil outlet 1302, heavy oil outlet 1303 and coke tar refuse outlet 1304, tar entrance 1301 is connected with tar outlet 203, and be suitable for carrying out natural subsidence by being separated the tar obtained in spray column, thus light oil, heavy oil and coke tar refuse can be obtained respectively.Thus, economic benefit can be significantly improved.
According to embodiments of the invention, blower fan 1400 has fuel gas inlet 1401 and gas outlet 1402, and fuel gas inlet 1401 and fuel gas export 204 and is connected, and is suitable for fuel gas supply in follow-up gas-holder.
According to embodiments of the invention, gas-holder 1500 is connected with gas outlet 1402, and is suitable for obtaining in storage spray column and the combustion gas of carrying through blower fan.
As mentioned above, can have according to the system of the pyrolyzing coal of the embodiment of the present invention and be selected from following advantage one of at least:
Can process the fine coal of below 3mm according to the system of the pyrolyzing coal of the embodiment of the present invention, processing efficiency is high;
Can derive rapidly according to the hydrocarbon resources that the system pyrolysis of the pyrolyzing coal of the embodiment of the present invention produces, secondary reaction is few, and tar quality is high, and in tar, light component content is high;
System pyrolysis reactor according to the pyrolyzing coal of the embodiment of the present invention adopts heat accumulation type radiant tube, and inside arranges rotation inner member, and add between particle and conduct heat between particular radiation pipe, heat transfer efficiency is high;
System pyrolysis gas according to the pyrolyzing coal of the embodiment of the present invention is not diluted, and calorific value is high.
In second of the present invention, the present invention proposes a kind of method of pyrolyzing coal.According to embodiments of the invention, the method adopts the system of the pyrolyzing coal of foregoing description to carry out.Method below with reference to the pyrolyzing coal of Fig. 6-8 pairs of embodiment of the present invention is described in detail.According to embodiments of the invention, the method comprises:
S100: coal is delivered in moving bed pyrolysis reactor and carries out pyrolysis processing
According to embodiments of the invention, coal is supplied to moving bed pyrolysis reactor from coal charge entrance, fuel and air are supplied in heat accumulation type radiant tube respectively, fuel are burnt in heat accumulation type radiant tube produce heat to carry out pyrolysis processing to coal, thus pyrolysis oil gas and semicoke can be obtained.
According to one embodiment of present invention, the granularity of coal is also not particularly limited, and those skilled in the art can select according to actual needs, and according to a particular embodiment of the invention, the granularity of coal can be not higher than 3mm.Thus, the unserviceable difficult problem of fine coal in prior art can be solved.
Concrete, the accurate temperature controlling of the realizations such as the flow of the combustion gas of heat accumulation type radiant tube to pyrolytic process is passed into by adjustment, and heat accumulation type radiant tube adopts the combustion system of regularly commutation, the temperature field of single heat accumulation type radiant tube is made to be more or less the same in 30 DEG C, thus ensure the homogeneity of reactor temperature field, such as the adjustment temperature range of the heat accumulation type radiant tube in epimere region in reactor is made to be 500 ~ 800 DEG C by adjusting the flow passing into the combustion gas of heat accumulation type radiant tube, ensure the abundant pyrolysis of coal charge, the flow being passed into the combustion gas of heat accumulation type radiant tube by adjustment makes the adjustment temperature range of the heat accumulation type radiant tube in hypomere region in reactor be 450 ~ 650 DEG C, thus a heating part does not further have the coal charge of complete pyrolysis.
S200: pyrolysis oil gas is delivered in spray column and carries out spray process
According to embodiments of the invention, the pyrolysis oil gas obtained in moving bed pyrolysis reactor is delivered in spray column, adopts spray liquid to carry out spray to pyrolysis oil gas and process, thus can be separated and obtain tar and combustion gas.It should be noted that, those skilled in the art can select the particular type of spray liquid according to actual needs, such as, can be the combination of one or more forms in ammoniacal liquor, water, washing oil or pyrolytic tar.Concrete, pyrolysis oil gas is entered in spray column by top or bottom, and spray liquid following current or the heat exchange of counter current contact mass transfer.
Method according to the pyrolyzing coal of the embodiment of the present invention effectively can process coal dust, and processing efficiency is high, simultaneously by using many group heat accumulation type radiant tubes to provide thermal source for pyrolytic process, the flow that can pass into the combustion gas of heat accumulation type radiant tube by adjustment realizes the accurate temperature controlling to pyrolytic process, and heat accumulation type radiant tube passes through heat storage type combustion, ensure that the homogeneity in temperature field, thus the pyrolysis efficiency of coal charge can be significantly improved, and then improve the yield of pyrolytic tar, more traditional use gaseous heat-carrier or solid thermal carriers are compared as the pyrolytic reaction device of pyrolysis thermal source simultaneously, moving bed pyrolysis reactor of the present invention does not need to arrange preheating unit and carrier separating unit, thus can greatly simplify pyrolytic reaction technical process, and then significantly reduce device failure rate and in gained pyrolytic tar dust content lower, and funnel temperature is low, secondly the present invention is by arranging that in the bottom of heat accumulation type radiant tube oil gas derives pipeline, the oil gas that pyrolysis produces can be derived rapidly, thus restrained effectively the second pyrolysis of oil gas, and then improve the yield of pyrolytic tar, and pyrolysis gas is not diluted by gaseous heat-carrier, pyrolysis gas calorific value is high, good in economic efficiency, secondly heat accumulation type radiant tube is coordinated by arranging whipping appts in reactor, agitator arm is in the process carrying out back rotation, make to pile up coal charge to be loosened, increase the voidage of piling up between coal charge, reduce the pressure drop of pyrolytic tar gas through coal charge layer, make the pyrolytic tar gas produced can pass rapidly through coal charge layer and arrive oil gas delivery line, the pyrolytic tar gas produced can be derived by oil gas delivery line in time, and the coking of radiator tube upper end can be avoided, thus avoid affecting heat transfer efficiency, additionally by employing spray column, spray process is carried out to pyrolysis oil gas, can be separated and obtain tar and combustible gas, increase economic efficiency.
With reference to figure 7, the method according to the pyrolyzing coal of the embodiment of the present invention comprises further:
S300: lump coal is supplied in shredder assembly and carries out break process
According to embodiments of the invention, lump coal (middle low-rank coal) is supplied in shredder assembly and carries out break process, thus broken coal can be obtained.According to a particular embodiment of the invention, the particle diameter of broken coal can be below 3mm.
S400: broken coal is supplied in coal bunker through the first conveyor screw and stores
In this step, the broken coal obtained is supplied in coal bunker through the first conveyor screw stores in shredder assembly.
S500: by the broken coal in coal bunker in the dry riser tube of the second conveyor screw, and the heat smoke adopting heat accumulation type radiant tube to produce carries out drying to broken coal and promotes process
According to embodiments of the invention, by the broken coal that is stored in coal bunker in the dry riser tube of the second conveyor screw, the heat smoke adopting heat accumulation type radiant tube to produce carries out drying to broken coal and promotes process, thus can obtain the mixture containing dry fine coal and flue gas.Thus, not only can realize the efficiency utilization of waste heat, and when making fine coal enter stove, moisture is little, heat dissipation is few, thus can improve the pyrolysis efficiency of fine coal further.Concrete, the heat smoke temperature produced in heat accumulation type radiant tube is about 200 DEG C, and it contacts realization with broken coal and dehydrates, the heat smoke temperature after heat exchange about about 100 DEG C, through the dried fine coal water content control of heat smoke at below 10wt%.
S600: the mixture containing dry fine coal and flue gas is supplied in the first cyclonic separator and carries out cyclonic separation process, and be supplied to being separated the dry fine coal obtained in pyrolysis reactor through the 3rd conveyor screw
According to embodiments of the invention, the mixture containing dry fine coal and flue gas obtained in dry riser tube is supplied in the first cyclonic separator and carries out cyclonic separation process, thus obtain tail gas and dry fine coal respectively, and be supplied to being separated the dry fine coal obtained in pyrolysis reactor through the 3rd conveyor screw.It should be noted that, those skilled in the art can need to adopt secondary cyclone according to substantial sepn.
With reference to figure 8, the method according to the pyrolyzing coal of the embodiment of the present invention comprises further:
S700: pyrolysis oil gas is delivered in spray column carry out spray process before, pyrolysis oil gas is supplied in the second cyclonic separator and cleaning apparatus respectively carries out cyclonic separation and dust removal process successively in advance
According to embodiments of the invention, the pyrolysis of collecting in gas gathering manifold oil gas is supplied in spray column carry out spray process before, in advance pyrolysis oil gas is supplied in the second cyclonic separator and cleaning apparatus respectively and carries out cyclonic separation and dust removal process successively, thus the solid particulate being purified oil gas and containing semicoke can be separated.Thus, the quality of gained tar and combustion gas can be significantly improved.It should be noted that, those skilled in the art can select the particular type of cleaning apparatus according to actual needs, and such as cleaning apparatus can be can for one or more forms combination in bed fly-ash separator, electrostatic precipitator, metallic filter etc.
S800: tar is delivered in tar groove and carries out sedimentation
According to embodiments of the invention, carry out natural subsidence by being separated the tar obtained in spray column, thus light oil, heavy oil and coke tar refuse can be obtained respectively.Thus, economic benefit can be significantly improved.
S900: combustion gas is supplied to gas-holder through blower fan
According to embodiments of the invention, to be supplied in gas-holder through blower fan to store being separated the combustion gas that obtains in spray column.
It should be noted that, the feature and advantage described by the above-mentioned system for pyrolyzing coal are suitable for the method for this pyrolyzing coal equally, repeat no more herein.
Below with reference to specific embodiment, present invention is described, it should be noted that, these embodiments are only descriptive, and do not limit the present invention in any way.
Embodiment
The system of the pyrolyzing coal of Fig. 1-5 is adopted to process brown coal, the technical analysis of brown coal: Mad%:6.75%, Vad%:31.59%, Aad%:5.41%, Fcad%:56.25%.
Processing parameter: moving bed pyrolysis reactor inner drying drying zone temperature is 580 DEG C, pyrolysis reaction region temperature is 605 DEG C, semicoke maturation zone temperature is 594 DEG C, the second cyclonic separator 1100 temperature out 565 DEG C, heat accumulation type radiant tube reactor internal pressure 2.51Kpa.
Pyrolysis tertiary industry distributes: tar 17.4%, pyrolysis gas 12.8%, semicoke 69.8%.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term not must for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and describe embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, and those of ordinary skill in the art can change above-described embodiment within the scope of the invention, revises, replace and modification.
Claims (10)
1. a system for pyrolyzing coal, is characterized in that, comprising: moving bed pyrolysis reactor and spray column,
Wherein, described moving bed pyrolysis reactor comprises:
Coal charge entrance and semicoke outlet;
Described coal charge entrance is positioned at the top of described reactor;
Described semicoke outlet is positioned at the bottom of described reactor;
Heat accumulation type radiant tube, the short transverse multilayer of described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along described reactor is arranged, every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Oil gas derives pipeline, and the tube wall of described oil gas derivation pipeline is provided with through hole;
Whipping appts, described whipping appts comprises stir shaft and is connected to the multiple agitator arms on described stir shaft, and described stir shaft is extend into the inside of described reactor by described semicoke outlet and is configured to rotate in described reactor;
Effuser, the gas-collecting branch pipe that described effuser comprises gas gathering manifold and is connected with described gas gathering manifold,
Wherein, it is outside that described gas gathering manifold is arranged on described reactor vertically, and described gas gathering manifold is connected with described spray column,
The sidewall that described gas-collecting branch pipe extends through described reactor to extend in described reactor and derives pipeline with described oil gas and is connected.
2. system according to claim 1, is characterized in that, described gas-collecting branch pipe is multiple, and 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. system according to claim 1 and 2, is characterized in that, described oil gas is derived pipeline and arranged along the short transverse multilayer of described reactor, and every layer has many oil gas derivation pipelines parallel to each other in the horizontal direction,
Optional, described oil gas derives pipeline and described heat accumulation type radiant tube is arranged in parallel, and the described heat accumulation type radiant tube left and right sides is separately symmetrically arranged with two oil gas derivation pipelines.
4. the system according to any one of claim 1-3, is characterized in that, it is that described oil gas derives the 1/2-3 of pipe diameter d doubly that described oil gas derives pipeline with the spacing of the tube wall of contiguous described heat accumulation type radiant tube,
Optional, the tube wall of described oil gas derivation pipeline is provided with multiple through hole, and preferably, described through hole is derived on the length direction of pipeline at described oil gas and is uniformly distributed,
Optional, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
5. the system according to any one of claim 1-4, is characterized in that, described agitator arm between described heat accumulation type radiant tube layer and described oil gas delivery line channel layer,
Optional, described agitator arm is perpendicular to described stir shaft, and spaced apart along the length direction of described stir shaft,
Optional, the adjacent projections of described agitator arm on the same cross section of described stir shaft at an angle,
Optional, the angle ranging from 0 ~ 90 degree, not containing end value,
Preferably, the angle ranging from 30 ~ 90 degree, not containing 90 degree.
6. the system according to any one of claim 1-5, is characterized in that, comprises further:
Crusher, described crusher has lump coal entrance and broken coal export;
First conveyor screw, described first conveyor screw has the first opening for feed and the first discharge port, and described first opening for feed is connected with described broken coal export;
Coal bunker, described coal bunker has coal bunker import and coal bunker outlet, and described coal bunker import is connected with described first discharge port;
Second conveyor screw, described second conveyor screw has the second opening for feed and the second discharge port, and described second opening for feed exports with described coal bunker and is connected;
Dry riser tube, described dry riser tube has the outlet of smoke inlet, fine coal opening for feed and mixture, and described smoke inlet is connected with the exhanst gas outlet on described heat accumulation type radiant tube, and described fine coal opening for feed is connected with described second discharge port;
First cyclonic separator, described first cyclonic separator has mixture entrance, offgas outlet and dry discharge, and described mixture entrance exports with described mixture and is connected;
3rd conveyor screw, described 3rd conveyor screw has the 3rd opening for feed and the 3rd discharge port, and described 3rd opening for feed is connected with described dry discharge, and described 3rd discharge port is connected with described coal charge entrance;
4th conveyor screw, the below and exporting with described semicoke that described 4th conveyor screw is arranged on described moving bed pyrolysis reactor is connected.
7. the system according to any one of claim 1-6, is characterized in that, comprises further:
Second cyclonic separator, described second cyclonic separator has oil and gas import, solid particulate outlet and purification oil gas vent, and described oil and gas import is connected with described gas gathering manifold;
Cleaning apparatus, described cleaning apparatus has oil gas vent after dedusting oil gas entrance and dedusting, and described dedusting oil gas entrance is connected with described purification oil gas vent, and after described dedusting, oil gas vent is connected with described spray column.
8. the system according to any one of claim 1-7, is characterized in that, comprises further:
Tar groove, described tar groove has tar entrance, light oil outlet, heavy oil outlet and coke tar refuse outlet, and described tar entrance is connected with described spray column;
Blower fan, described blower fan has fuel gas inlet and gas outlet, and described fuel gas inlet is connected with described spray column; And
Gas-holder, described gas-holder is connected with described gas outlet.
9. utilize a method for the system pyrolyzing coal of the pyrolyzing coal described in any one of claim 1-8, it is characterized in that, comprising:
Coal is delivered in described moving bed pyrolysis reactor and carries out pyrolysis processing, to obtain semicoke and pyrolysis oil gas;
Described pyrolysis oil gas is delivered in described spray column and carries out spray process, to obtain tar and combustion gas.
10. method according to claim 8 or claim 9, is characterized in that, comprise further:
Described pyrolysis oil gas is supplied in described spray column carry out spray process before, described pyrolysis oil gas is supplied in described second cyclonic separator and described cleaning apparatus carries out cyclonic separation and dust removal process successively in advance.
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