CN205653404U - Coal pyrolytic reaction ware - circulating fluidized bed combined system - Google Patents

Abstract

The utility model provides a coal pyrolytic reaction ware circulating fluidized bed combined system, it includes coal pyrolytic reaction ware and circulating fluidized bed. The utility model discloses a combined system can directly ally oneself with usefulness with current circulating fluidized bed with coal pyrolytic reaction ware, and need not to reform transform current circulating fluidized bed, coal pyrolytic reaction ware and circulating fluidized bed can move relatively independently, the two mutual interference is less relatively, and this combined system can effectively be used for producing combustible gas and pyrolysis oil and coproduction electric power, and the current circulating fluidized bed's of utilization conveying system, it send to realize semicoke heat, the burning of guarantee semicoke, and reduce the coal and pull out first technology cost, and can greatly reduced the produce coal oil -gas mixture's of pyrolytic reaction ware dustiness of the built -in cyclone of this coal pyrolytic reaction ware, and then thermal insulation is reduced to probably reaching of plug the pipe in effectively reducing the subsequent handling.

Description

Pyrolysis of coal reactor-recirculating fluidized bed combined system

Technical field

This utility model relates to coal sublevel cascade utilization technical field, in particular it relates to pyrolysis of coal reactor-recirculating fluidized bed combined system.

Background technology

The semicoke produced after pyrolysis of coal can be as fuel-fired power generation, and existing pyrolysis of coal plug technique is mainly for recirculating fluidized bed generating set, as Chinese Academy of Sciences's process and Zhejiang University utilize the heat that CFBB produces grey as heat carrier, and utilize down-flow fluidized bed using ECT technique to achieve pyrolysis of coal, and petroleum vapor recovery.Existing system is owing to taking the pyrolysis of coal plug technique of more complicated solid or gas heat carrier, and pyrolytic process of coal produces petroleum resources, for electricity generation system, needs to be equipped with corresponding oil vapor treatment system, and therefore existing system configuration is various, and cost is high.

Fig. 1 is a kind of furnace front coal head-drawing process structure schematic diagram, (diagram A entrance) is sent in solid thermal carriers gasification installation 1 by this technique, by coal plug pyrolysis gas and tar after cyclone separator 6, extract petroleum resources (diagram B outlet), the semicoke separated sends into recirculating fluidized bed 7 (diagram F outlet), the bottom that semicoke sends into recirculating fluidized bed 7 through material returning device 2 rear portion (diagram G outlet) uses as fuel, a part is sent in adiabatic coal plug combustor 3, joins air burning.The flue gas that combustor 3 produces enters cyclone separator 4, and the semicoke separated is in material returning device 5 enters gasification installation 1 together with coal, and heat smoke (diagram E) is also fed in recirculating fluidized bed 7.But, this technological process is complicated, be primarily due to this technique take semicoke as heat carrier, therefore technological process include semicoke heating, promote, separate, the technique such as mixing, cause system flow to increase, substantially increase system failure rate；Meanwhile, the semicoke that this technique produces can only be for fluidized-bed combustion boiler, it is impossible to utilize on recirculating fluidized bed.

But, in China's electricity generation system, recirculating fluidized bed accounting is the highest, and owing to CFBC is higher to coal volatile matter and Particle size requirements, coal plug is the most little for the technique of recirculating fluidized bed.

Thus, current pyrolysis of coal plug technique still haves much room for improvement.

Utility model content

One of technical problem that this utility model is intended to solve in correlation technique the most to a certain extent.To this end, one of the purpose of this utility model is propose a kind of pyrolysis of coal reactor-recirculating fluidized bed combined system and utilize its method processing coal.

Concrete, this utility model is provided with a kind of New type coal plug technique for recirculating fluidized bed, produces combustible gas and pyrolysis oil co-production electric power, and utilize the induction system of existing recirculating fluidized bed, realize semicoke heat to send, ensure the burning of semicoke, and reduce coal plug process costs.Combined system of the present utility model solves the problem that coal plug leading portion pyrolytic process is complicated, and thermal decomposition product Appropriate application, reduces cost of electricity-generating.

In view of this, at an aspect of the present utility model, this utility model provides a kind of pyrolysis of coal reactor-recirculating fluidized bed combined system.According to embodiment of the present utility model, this pyrolysis of coal reactor-recirculating fluidized bed combined system includes:

Pyrolysis of coal reactor, described pyrolysis of coal reactor has coal entrance, semicoke outlet and gas mixture outlet, wherein, described coal entrance is arranged at the top of described pyrolysis of coal reactor, the outlet of described gas mixture is arranged on roof and/or the sidewall of described pyrolysis of coal reactor, and the outlet of described semicoke is arranged at the bottom of described pyrolysis of coal reactor；

It is provided with many oil gas in described pyrolysis reactor and derives pipelines, gas gathering manifold, many gas-collecting branch pipes, heat accumulation type radiant tube and cyclone separator,

Wherein, described gas gathering manifold is adjacent to the internal perisporium of described pyrolysis of coal reactor and is vertically arranged,

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 cyclone separator has gas-solid mixture entrance, gas outlet and solid outlet, and wherein, described gas outlet is connected with the outlet of described gas mixture, and one end of described gas gathering manifold extends the gas-solid mixture entrance being communicated to described 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 the most parallel to each other；

Recirculating fluidized bed, described recirculating fluidized bed is provided with semicoke entrance, bunker coal entrance and air intake, and described semicoke entrance is connected with the outlet of described semicoke.

Inventor finds, pyrolysis of coal reactor of the present utility model directly can be combined with existing recirculating fluidized bed, and without existing recirculating fluidized bed is transformed, with existing pyrolysis of coal plug technique-recirculating fluidized bed generating set associated with compared with system, in pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model, pyrolysis of coal reactor and recirculating fluidized bed can run relatively independently, and the two interferes with each other relatively small.nullAdditionally，Owing to pyrolysis of coal reactor using heat accumulation type radiant tube provide thermal source for pyrolytic process，The accurate temperature controlling to pyrolytic process can be realized by the flow of the combustion gas that adjustment is passed through heat accumulation type radiant tube，And this heat accumulation type radiant tube can be by realizing quickly commutation and heat storage type combustion at two ends，Can ensure that the uniformity in temperature field in pyrolysis of coal reactor，Such that it is able to significantly improve the fast pyrogenation efficiency of coal charge，Use gas heat carrier or solid thermal carriers as compared with the pyrolytic reaction device of pyrolysis thermal source with more traditional，Pyrolysis of coal reaction unit of the present utility model need not arrange preheating unit and carrier separative element，Fast pyrogenation reaction process flow process can be greatly simplified，Thus it is relatively low to significantly reduce dust content in the fault rate of device and gained tar，And then it is complicated to solve existing coal plug leading portion pyrolytic process，And the problem of fluctuation of service that existing pyrolysis reactor causes with CFBB coupling height.Pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model can be effective to produce combustible gas and pyrolysis oil co-production electric power, and utilize the induction system of existing recirculating fluidized bed, realize semicoke heat to send, ensure the burning of semicoke, and reduce coal plug process costs.When pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model is used for generating electricity, it can be ensured that the stability of electricity generation system.Special needs to be pointed out is, pyrolysis of coal inside reactor is provided with cyclone separator, greatly reduces whirlwind insulation cost and the possibility of tar condensing blocking pipeline.

Alternatively, every layer of described heat accumulation type radiant tube includes multiple parallel and equally distributed heat accumulation type radiant tube, and each described heat accumulation type radiant tube is parallel with each heat accumulation type radiant tube in adjacent upper and lower two-layer heat accumulation type radiant tube and is in staggered distribution in the short transverse of described pyrolysis of coal reactor.Thus, it is possible to significantly improve the fast pyrogenation efficiency of coal charge, and then improve the productivity of tar.

Alternatively, described gas-collecting branch pipe is arranged parallel to each other along the length direction of described gas gathering manifold.

Alternatively, described gas-collecting branch pipe is perpendicular to described gas collecting main pipe.

Alternatively, described oil gas derives the pipeline short transverse multi-tier arrangement along described pyrolysis reactor, and every layer has many oil gas the most parallel to each other and derives pipeline.

Alternatively, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.

Alternatively, 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.

Alternatively, the spacing of the tube wall that described oil gas derives pipeline and neighbouring described heat accumulation type radiant tube be that described oil gas derives pipe diameter d 1/2-3 times.

Alternatively, described oil gas is derived and is provided with multiple through hole on the tube wall of pipeline.

Alternatively, the plurality of through hole is uniformly distributed on the length direction that described oil gas derives pipeline.

Alternatively, it is welded with support bar between outer wall and the described heat accumulation type radiant tube being adjacent of described cyclone separator.

Alternatively, described pyrolysis of coal reactor-recirculating fluidized bed combined system farther includes: gas mixture after-treatment device, and described gas mixture after-treatment device is connected with the outlet of described gas mixture.

Alternatively, described gas mixture after-treatment device includes: Oil-gas Separation assembly, and described Oil-gas Separation assembly has gas mixture import, pyrolysis gas outlet and tar outlet, and described gas mixture import is connected with the outlet of described gas mixture；Pyrolysis gas purification assembly, described pyrolysis gas purification assembly has pyrolysis gas import and combustible gas outlet, and described pyrolysis gas import is connected with described pyrolysis gas outlet, tar refining assembly, described tar refining assembly has tar entrance and oil product outlet, and described tar entrance is connected with described tar outlet.

This utility model at least has the advantages that

1) radial canal heats downstriker pyrolysis of coal reactor be combined with recirculating fluidized bed, pyrolysis reactor of the present utility model have employed heat accumulation type radiant tube and combines descending reactor, belong to heating indirectly, such pyrolysis reactor allows directly to be combined with existing recirculating fluidized bed, and without existing recirculating fluidized bed is transformed on a large scale.

2) hot semicoke is sent into recirculating fluidized bed, it is possible to increase the capacity usage ratio of electricity generation system.

3) in pyrolysis of coal reactor, cyclone separator is set, greatly reduce the dustiness of the gas mixture of the pyrolysis reactor that produces coal and pyrolysis of coal reactor to the lagging facility of pipeline between pyrolysis oil gas mixture rapid condensation device, the thermal insulation area of minimizing equipment and reduction system heat tracing energy consumption, greatly reduce the possibility of tar condensing blocking pipeline simultaneously, reduce the processing cost of follow-up tar.

Additional aspect of the present utility model and advantage will part be given in the following description, and part will become apparent from the description below, or is recognized by practice of the present utility model.

Accompanying drawing explanation

Fig. 1 existing furnace front coal head-drawing process structure schematic diagram.

Fig. 2 is the pyrolysis of coal reactor according to one embodiment of this utility model-recirculating fluidized bed combined system structural representation.

Fig. 3 is the pyrolysis of coal reactor according to another embodiment of this utility model-recirculating fluidized bed combined system part-structure schematic diagram.

Fig. 4 is the pyrolysis of coal reactor according to this utility model further embodiment-recirculating fluidized bed combined system structural representation.

Fig. 5 is the schematic flow sheet of the method utilizing pyrolysis of coal reactor-recirculating fluidized bed combined system process coal according to one embodiment of this utility model.

Fig. 6 is the schematic flow sheet of the method utilizing pyrolysis of coal reactor-recirculating fluidized bed combined system process coal according to another embodiment of this utility model.

Detailed description of the invention

Embodiment of the present utility model is described below in detail.The embodiments described below is exemplary, is only used for explaining this utility model, and it is not intended that to restriction of the present utility model.In embodiment, unreceipted concrete technology or condition, according to the technology described by the document in this area or condition or carried out according to product description.Agents useful for same or instrument unreceipted production firm person, be can by city available from conventional products.

In description of the present utility model, it will be appreciated that, term " " center ", " longitudinally ", " laterally ", " length ", " width ", " thickness ", on " ", D score, " front ", " afterwards ", " left ", " right ", " vertically ", " level ", " push up ", " end ", " interior ", " outward ", " clockwise ", " counterclockwise ", " axially ", " radially ", orientation or the position relationship of the instruction such as " circumferential " are based on orientation shown in the drawings or position relationship, it is for only for ease of description this utility model and simplifies description, rather than indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore it is not intended that to restriction of the present utility model.

Additionally, term " first ", " second " are only used for describing purpose, 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 at least one this feature.In description of the present utility model, " multiple " are meant that at least two, such as two, three etc., unless otherwise expressly limited specifically.

In this utility model, unless otherwise clearly defined and limited, term " is installed ", " being connected ", " connection ", the term such as " fixing " should be interpreted broadly, and connects for example, it may be fixing, it is also possible to be to removably connect, or integral；Can be to be mechanically connected, it is also possible to be electrical connection；Can be to be joined directly together, it is also possible to be indirectly connected to by intermediary, can 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, above-mentioned term concrete meaning in this utility model can be understood as the case may be.

In this utility model, 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.

At an aspect of the present utility model, this utility model provides a kind of pyrolysis of coal reactor-recirculating fluidized bed combined system.According to embodiment of the present utility model, with reference to Fig. 2, this pyrolysis of coal reactor-recirculating fluidized bed combined system includes pyrolysis of coal reactor 100 and recirculating fluidized bed 200.

According to embodiment of the present utility model, pyrolysis of coal reactor 100 has coal entrance 110, semicoke outlet 120 and gas mixture outlet 130.Wherein, coal entrance 110 is arranged at the top of pyrolysis of coal reactor 100, is suitable in fine coal supply to pyrolysis of coal reactor 100；Gas mixture outlet 130 is arranged on roof and/or the sidewall of pyrolysis of coal reactor 100, and the gas mixture being suitable to produce pyrolysis of coal discharges pyrolysis of coal reactor 100；Semicoke outlet 120 is arranged at the bottom of pyrolysis of coal reactor 100, and the semicoke being suitable to produce pyrolysis of coal discharges pyrolysis of coal reactor 100.

According to embodiment of the present utility model, it is provided with many oil gas in pyrolysis of coal reactor 100 and derives pipelines 140, gas gathering manifold 150, many gas-collecting branch pipes 160, heat accumulation type radiant tube 170 and cyclone separator 180.

According to specific embodiment of the utility model, heat accumulation type radiant tube 160 is in the inside of pyrolysis of coal reactor 100 along the short transverse multi-tier arrangement of pyrolysis of coal reactor 100, and every layer has many heat accumulation type radiant tubes the most parallel to each other.According to specific embodiment of the utility model, every layer of heat accumulation type radiant tube 160 includes that multiple parallel and equally distributed heat accumulation type radiant tube and each heat accumulation type radiant tube are parallel with each heat accumulation type radiant tube in adjacent upper and lower two-layer heat accumulation type radiant tube.According to concrete example of the present utility model, 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 specific embodiment of the utility model, the concrete set-up mode of heat accumulation type radiant tube 160 is not particularly limited, and those skilled in the art can carry out appropriate design according to the temperature field that actual pyrolytic reaction needs.In embodiments more of the present utility model, the concrete set-up mode of heat accumulation type radiant tube 160 includes but not limited to: adjacent heat accumulation type radiant tube about 160 center distance can be 300～500mm, adjacent heat accumulation type radiant tube vertical centre spacing can be 400～800mm, and the number of plies of multilamellar heat accumulation type radiant tube can be 10-30 layer.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.Inventor finds, this kind of structure is arranged so that reactor temperature field distribution is uniform, such that it is able to significantly improve the pyrolysis efficiency of material, and then improves the yield of pyrolysis oil.

According to specific embodiment of the utility model, heat accumulation type radiant tube can be unidirectional, gas heat-accumulated type radial canal, and the heat i.e. produced by combustion gas by heat accumulation type radiant tube body is to carry out heat supply by the way of radiation.According to specific embodiment of the utility model, heat accumulation type radiant tube can be provided with gas control valve (not shown).Thus, it is possible to realize the accurate temperature controlling to pyrolytic process by adjusting the flow of the combustion gas that gas control valve regulation is passed through heat accumulation type radiant tube, 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 be passed through the combustion gas of heat accumulation type radiant tube by adjustment realizes the accurate temperature controlling to pyrolytic process, the every independent temperature control of heat accumulation type radiant tube, and heat accumulation type radiant tube uses the combustion system of periodically commutation, the temperature field making single heat accumulation type radiant tube is more or less the same in 30 DEG C, thus ensure the uniformity of reactor temperature field, the flow of the combustion gas being such as passed through 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, can be by the temperature range in the control realization drying and dehydrating district to heat accumulation type radiant tube 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 the material that a heating part further is pyrolyzed the most completely.

According to embodiment of the present utility model, gas gathering manifold 150 is adjacent to the internal perisporium of pyrolysis of coal reactor 100 and is vertically arranged, and one end of gas-collecting branch pipe 160 is connected with gas gathering manifold 150, and the other end is communicated to oil gas and derives pipeline 140.The concrete set-up mode of gas-collecting branch pipe 160 is not particularly limited, such as, include but not limited to that the length direction along gas gathering manifold 150 is arranged parallel to each other.Every gas-collecting branch pipe 160 can individually be connected with gas gathering manifold 150, it is also possible to two or many gas-collecting branch pipes 160 are communicated to gas gathering manifold 150 near one end of gas-collecting branch pipe by same connection pipeline 161.According to embodiment of the present utility model, can have certain angle between gas-collecting branch pipe 160 and gas gathering manifold 150, in some concrete examples, gas-collecting branch pipe 160 is perpendicular to gas collecting main pipe 150 and arranges.Thus, beneficially the quick of gas mixture is derived.

According to embodiment of the present utility model, oil gas is derived pipeline 140 and is connected with one end of gas-collecting branch pipe 160, and is provided with through hole on the tube wall of oil gas delivery line 140.Thus, by arranging oil gas derivation pipeline so that the pyrolysis oil gas produced in pyrolytic process is quickly derived, thus effectively suppression oil gas second pyrolysis, improve pyrolysis oil yield.According to embodiment of the present utility model, 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 140, it is preferable that the plurality of through hole is derived at oil gas and is uniformly distributed on the length direction of pipeline 140.Thus, beneficially gas mixture is quickly derived.

According to embodiment of the present utility model, oil gas derives the pipeline 140 short transverse multi-tier arrangement along pyrolysis reactor 100, and every layer has many oil gas the most parallel to each other and derives pipeline.According to specific embodiment of the utility model, same layer oil gas is derived pipeline 140 and is communicated to same gas-collecting branch pipe 160.Thereby, it is possible to gas mixture is concentrated, is derived rapidly.

According to embodiment of the present utility model, oil gas is derived pipeline 140 and is arranged in parallel with heat accumulation type radiant tube 170, and the left and right sides of heat accumulation type radiant tube 170 is symmetrically arranged with two oil gas and derives pipeline 140.Inventor finds, derives pipeline by installing oil gas every heat accumulation type radiant tube both sides, and the gas mixture that pyrolysis produces is derived rapidly by deriving pipeline, thus restrained effectively the second pyrolysis of oil gas, and then improves the yield of pyrolysis oil, good in economic efficiency.

According to embodiment of the present utility model, as it is shown on figure 3, oil gas derives 1/2-3 times that spacing L is oil gas derivation pipe diameter d of pipeline 140 and the tube wall of neighbouring heat accumulation type radiant tube 170.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 embodiment of the present utility model, cyclone separator 180 has gas-solid mixture entrance 181, gas outlet 182 and solid outlet 183, wherein, gas outlet 182 is connected with gas mixture outlet 120, and the end of gas gathering manifold 150 extends the gas-solid mixture entrance 181 being communicated to this cyclone separator 180.Inventor finds, by arranging cyclone separator at pyrolysis of coal inside reactor, thermal decomposition product is carried out gas solid separation process, can effectively reduce the dustiness of gas mixture discharging pyrolysis of coal reactor, effectively the produce coal pyrolysis oil gas of pyrolysis reactor of suppression mixes dust condensation blocking subsequent pipeline and relevant device；Meanwhile, in cyclone separator built-in pyrolysis of coal reactor, 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 embodiment of the present utility model, between outer wall and the heat accumulation type radiant tube 170 being adjacent of cyclone separator 180, it is welded with support bar 181, it is possible to be firmly fixed to inside pyrolysis reactor this cyclone separator.Generally, cyclone separator 180 is arranged at the top of pyrolysis reactor 100, therefore, it can weld support bar 181 between cyclone separator 180 outer wall and ground floor heat accumulation type radiant tube 170.

According to embodiment of the present utility model, being additionally provided with the smoke entrance (not shown) after fuel, air and the burning needed for heat accumulation type radiant tube burning on pyrolysis of coal reactor 100, fuel gas inlet is connected with heat accumulation type radiant tube 170 respectively with air intake simultaneously.The heat smoke produced that burns in heat accumulation type radiant tube may be used for treating the fine coal raw material of pyrolysis and is dried and the pre-heat treatment, thus further increases pyrolysis of coal reactor efficiency and efficiency of combustion, and achieves comprehensive utilization resource, reduces the purpose of energy consumption.

According to embodiment of the present utility model, the height of pyrolysis of coal reactor 100 and width are preferably suitable, and width can be 2-6 rice, highly can control by controlling the quantity and spacing of every layer of heat accumulation type radiant tube 170, and the height of usual pyrolysis of coal reactor can be 5～20m.Thus, it is possible to realize the pyrolysis completely to material.It will be understood by those skilled in the art that height and the width of pyrolysis of coal reactor 100 are not limited to above-mentioned scope, those skilled in the art can select the most flexibly.

According to embodiment of the present utility model, semicoke entrance 210, bunker coal entrance 220 and air intake 230 it is provided with on recirculating fluidized bed 200, wherein, semicoke entrance 210 is connected with semicoke outlet 120, be suitable to supply to recirculating fluidized bed 200 semicoke produced in pyrolysis of coal reactor, bunker coal entrance 220 and air intake 230 are respectively adapted in recirculating fluidized bed 200 supply bunker coal and air, are beneficial to coal and semicoke are carried out mixed combustion generating.Inventor finds, by the hot semicoke directly heat produced in pyrolysis of coal reactor 100 is delivered to recirculating fluidized bed 200 and coal mixed combustion, the combustion stability of recirculating fluidized bed 200 can not only be guaranteed, and capacity usage ratio can be significantly improved, and when the stability utilizing this pyrolysis of coal reactor-recirculating fluidized bed combined system to be able to ensure that electricity generation system when carrying out combustion power generation.

According to embodiment of the present utility model, with reference to Fig. 4, this pyrolysis of coal reactor-recirculating fluidized bed combined system may further include: gas mixture after-treatment device 400, and this gas mixture after-treatment device 400 exports 130 with the gas mixture of pyrolysis of coal reactor 100 and is connected.Specifically, gas mixture after-treatment device 400 may include that Oil-gas Separation assembly 410, pyrolysis gas purification assembly 420 and tar refining assembly 430.The gas mixture that gas mixture after-treatment device 400 is suitable to obtain pyrolysis carries out post processing, carries out Oil-gas Separation, pyrolysis gas purification and tar refining etc. successively and processes, to obtain purified gas and high added value oil product.

According to embodiment of the present utility model, Oil-gas Separation assembly 410 has gas mixture import 411, pyrolysis gas outlet 412 and tar outlet 413, gas mixture import 411 exports 130 with the gas mixture of pyrolysis of coal reactor and is connected, tar outlet 413 is connected with the tar entrance 431 of tar refining assembly 430, and this Oil-gas Separation assembly 410 is suitable to separate thermogenetic for solution gas mixture obtain pyrolysis gas and tar, Oil-gas Separation assembly 410 carries out the concrete mode of Oil-gas Separation and is not particularly limited, such as, condensation, spray etc. are included but not limited to.

According to embodiment of the present utility model, pyrolysis gas purification assembly 420 has pyrolysis gas import 421 and combustible gas outlet 422, wherein, pyrolysis gas import 421 is connected with pyrolysis gas outlet 412, and pyrolysis gas purification assembly 420 is suitable to that pyrolysis gas carries out the operation such as desulfurization, deamination and carries out purified treatment to obtain clean combustible gas.In certain embodiments, pyrolysis gas purification assembly 420 can be provided with two combustible gases and export 422 (not shown)s, one of them is connected with the heat accumulation type radiant tube in pyrolysis of coal reactor, for providing the fuel of heat accumulation type radiant tube combustion heating, realize the Appropriate application of thermal decomposition product, and another pyrolysis gas outlet 422 is as product gas outlet.

According to embodiment of the present utility model, tar refining assembly 430 has tar entrance 431 and oil product outlet 432, and wherein, tar entrance 431 is connected with tar outlet 413.The tar that this tar refining assembly 430 is suitable to separating acquisition carries out refinement treatment, to obtain high added value oil product, such as, includes but not limited to that the tar to isolated carries out hydrofinishing.

Pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model arranges coal plug technique for recirculating fluidized bed, efficiently solve the problem that coal plug leading portion pyrolytic process is complicated, in combined system of the present utility model, pyrolysis of coal reactor directly can be combined with existing recirculating fluidized bed, hot semicoke is sent by First air, without existing recirculating fluidized bed is transformed, with existing pyrolysis of coal plug technique-recirculating fluidized bed generating set associated with compared with system, in pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model, pyrolysis of coal reactor and recirculating fluidized bed can run relatively independently, the two interferes with each other relatively small, thermal decomposition product Appropriate application, cost of electricity-generating is substantially reduced.Pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model can be effective to produce combustible gas and pyrolysis oil co-production electric power, and utilize the induction system of existing recirculating fluidized bed, realize semicoke heat and deliver to recirculating fluidized bed, and retain the combustion system of original recirculating fluidized bed, realize the coal in pyrolysis char and recirculating fluidized bed mixes burning, ensure the stability of CFBC, pyrolysis gas and pyrolytic tar are processed simultaneously, produce combustible gas and prepared tar as major product, it is achieved the economic benefit of coal plug.When pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model is used for generating electricity, it can be ensured that the stability of electricity generation system.Special needs to be pointed out is, pyrolysis of coal inside reactor is provided with cyclone separator, the temperature of pyrolysis of coal gas mixture can be reduced, reduce the dustiness of the gas mixture of the pyrolysis reactor that produces coal simultaneously, reduce the dust content in subsequent high temperature coal pyrolysis gas Quench tar, with the possibility of tar condensing blocking pipeline, reduce whirlwind insulation cost simultaneously.

In order to reduce the impact on coal powder boiler combustion of the coal plug, combined system of the present utility model takes heat accumulating type descending fast pyrogenation stove, have only to be delivered to recirculating fluidized bed hot for the semicoke produced, it is effectively utilized the sensible heat that pyrolysis char is self-contained, pyrolysis gas and pyrolytic tar are processed simultaneously, produce combustible gas and high added value oil product as major product, it is achieved the economic benefit of coal plug.Pyrolysis primary dust removing system (i.e. cyclone separator) is built in pyrolysis reactor simultaneously, effectively reduces out the dustiness of the pyrolysis gas of pyrolysis reactor, it is to avoid the problem that tar condenses blocking pipeline.

In another aspect of the present utility model, this utility model provides a kind of method utilizing foregoing pyrolysis of coal reactor-recirculating fluidized bed combined system to process coal.According to embodiment of the present utility model, with reference to Fig. 5, the method comprises the following steps:

S100: coal is delivered to described pyrolysis of coal reactor and carries out pyrolysis processing, in order to obtain semicoke and gas mixture.

According to embodiment of the present utility model, the particle diameter supplying the coal to pyrolysis of coal reactor can be less than 3 millimeters, and thus, pyrolysis material is heated evenly in pyrolysis reactor, and pyrolytic reaction efficiency is higher, and pyrolytic tar yield is higher.

According to specific embodiment of the utility model, 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, in drying and dehydrating district, moisture quickly sloughed by 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 pyrolysis of coal reactor is discharged by semicoke outlet.

S200: semicoke is delivered to described recirculating fluidized bed, makes semicoke carry out with coal mixing powder process burning.

According to embodiment of the present utility model, in this step, the pyrolysis high-temperature semi-coke of 400-600 degree Celsius is discharged from semicoke outlet, delivers to recirculating fluidized bed through First air, carry out combustion power generation.

S300: described gas mixture is delivered to described gas mixture after-treatment device and carries out post processing, thus obtain combustible gas and oil product.

According to embodiment of the present utility model, with reference to Fig. 6, step S300 may further include following steps: S310: gas mixture is carried out Oil-gas Separation process, obtains tar and pyrolysis gas；S320: pyrolysis gas is carried out purified treatment, obtains combustible gas；And S330: tar is carried out refinement treatment, obtains oil product.Thus, it is possible to effectively thermal decomposition product is carried out suitable post processing, obtain combustible gas and the high added value oil product of cleaning.

Inventor finds, in the method, it is possible to use pyrolysis of coal reactor is directly combined with existing recirculating fluidized bed, and without existing recirculating fluidized bed is transformed, pyrolysis of coal reactor and recirculating fluidized bed can run relatively independently, and the two interferes with each other relatively small.The method can be effective to produce combustible gas and pyrolysis oil co-production electric power, and utilizes the induction system of existing recirculating fluidized bed, it is achieved semicoke heat is sent, and ensures the burning of semicoke, and reduces coal plug process costs.And, in the method, the gas mixture that pyrolysis of coal produces is before discharging pyrolysis of coal reactor, dedusting is carried out through cyclone separator, pyrolysis of coal reactor can be greatly reduced to the lagging facility of pipeline between pyrolysis oil gas mixture rapid condensation device, the thermal insulation area of minimizing equipment and reduction system heat tracing energy consumption, greatly reduce the possibility of tar condensing blocking pipeline simultaneously.

Referring to Fig. 4 and Fig. 6, describe pyrolysis of coal of the present utility model reactor-recirculating fluidized bed combined system in detail and utilize its duty processing the method for coal to be described.

Specifically, by coal entrance 110, the fine coal that particle diameter is crushed to less than 3 millimeters in advance is supplied to pyrolysis of coal reactor 100, fine coal from top to bottom moves in pyrolysis of coal reactor 100, carries out pyrolytic reaction under the temperature field that heat accumulation type radiant tube provides, and produces gas mixture and semicoke.nullOn the one hand，The through hole that the gas mixture obtained derives pipeline 140 by oil gas enters oil gas derivation pipeline 140，Derive pipeline 140 by oil gas and be directed into gas-collecting branch pipe 160，Then gas gathering manifold 150 it is collected to，And be supplied to cyclone separator 180 carry out gas solid separation process by gas-solid mixture entrance 181，The solid of isolated is discharged through solid outlet 183，Enter in pyrolysis of coal reactor 100，The gas mixture of isolated is through gas outlet 182、Gas mixture outlet 130、And enter by gas mixture entrance 411 Oil-gas Separation assembly 410 carries out Oil-gas Separation process，The pyrolysis gas of isolated is discharged through pyrolysis gas outlet 412，Then pyrolysis gas purification assembly 420 is entered through pyrolysis gas import 421，In pyrolysis gas purification assembly 420，Pyrolysis gas carries out desulfurization、The operations such as deamination carry out purified treatment，The purified gas part obtained is through combustible gas outlet 422 discharge，Obtain combustible gas product，A part can be by the heat accumulation type radiant tube in another combustible gas outlet 422 supply to pyrolysis of coal reactor，For combustion heating，In Oil-gas Separation assembly 410, the tar of isolated enters tar refining assembly 430 through tar outlet 413 and tar import 431 successively，In tar refining assembly 430, tar is carried out hydrotreating，The high added value oil product obtained is through oil product outlet 432 discharge.On the other hand, the semicoke that pyrolysis produces is through semicoke outlet 120 discharge pyrolysis of coal reactor 100, then recirculating fluidized bed 200 is entered through semicoke entrance 210, supplying bunker coal and air in recirculating fluidized bed 200 by bunker coal entrance 220 and air intake 230, in recirculating fluidized bed 200, semicoke and coal carry out mixing burning generating simultaneously.

Embodiment

Pyrolyzing coal is crushed to below particle diameter 3mm, sends in pyrolysis of coal of the present utility model reactor-recirculating fluidized bed combined system and processes, and obtains purified gas and high-quality oil product.Concrete steps are with reference to the above-mentioned description to pyrolysis of coal reactor-recirculating fluidized bed combined system of the present utility model with the duty utilizing its method processing coal.Wherein, pyrolysis gas composition is as shown in the table, and the pyrolysis char temperature of generation is 515 DEG C, generates electricity by being mixed into CFBC with generating coal.

Compared with the situation of generating feed coal all with the fuel of recirculating fluidized bed, when the pyrolysis char that pyrolysis of coal reactor is discharged accounts for the 50% of ciculation fluidized bed material gross weight, whole system energy utilization efficiency improves 3.83%, the income of purified gas and coal tar is converted in cost of electricity-generating, and cost of electricity-generating reduces about 5.61%.

In description of the present utility model, term " first ", " second " are only used for describing purpose, and it is not intended that indicate or imply 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 this feature.In description of the present utility model, " multiple " are meant that two or more, unless otherwise expressly limited specifically.

In the description of this specification, the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means that the specific features, structure, material or the feature that combine this embodiment or example description are contained at least one embodiment of the present utility model or example.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 be to combine in one or more embodiments in office or example in an appropriate manner.Additionally, in the case of the most conflicting, the feature of the different embodiments described in this specification or example and different embodiment or example can be combined and combine by those skilled in the art.

Although above it has been shown and described that embodiment of the present utility model, it is understandable that, above-described embodiment is exemplary, it is not intended that to restriction of the present utility model, above-described embodiment can be changed in the range of this utility model, revises, replace and modification by those of ordinary skill in the art.

Claims (10)

1. pyrolysis of coal reactor-recirculating fluidized bed combined system, it is characterised in that including:

Pyrolysis of coal reactor, described pyrolysis of coal reactor has coal entrance, semicoke outlet and gas mixture and exports, wherein, Described coal entrance is arranged at the top of described pyrolysis of coal reactor, and the outlet of described gas mixture is arranged at described pyrolysis of coal reaction On the roof of device and/or sidewall, the outlet of described semicoke is arranged at the bottom of described pyrolysis of coal reactor；

It is provided with many oil gas in described pyrolysis reactor and derives pipeline, gas gathering manifold, many gas-collecting branch pipes, heat accumulating type radiation Pipe and cyclone separator,

Wherein, described gas gathering manifold is adjacent to the internal perisporium of described pyrolysis of coal reactor and is vertically arranged,

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 cyclone separator has gas-solid mixture entrance, gas outlet and a solid outlet, wherein, described gas outlet with The outlet of described gas mixture is connected, and one end of described gas gathering manifold extends the gas-solid mixing being communicated to described cyclone separator Thing entrance；

Described heat accumulation type radiant tube is along the short transverse multi-tier arrangement of described pyrolysis reactor, and every layer has many in level side Heat accumulation type radiant tube the most parallel to each other；

Recirculating fluidized bed, described recirculating fluidized bed is provided with semicoke entrance, bunker coal entrance and air intake, described semicoke Entrance is connected with the outlet of described semicoke.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 1, it is characterised in that every layer of institute State heat accumulation type radiant tube and include multiple parallel and equally distributed heat accumulation type radiant tube, and each described heat accumulation type radiant tube with Each heat accumulation type radiant tube in adjacent upper and lower two-layer heat accumulation type radiant tube is parallel and height along described pyrolysis of coal reactor It is in staggered distribution on direction.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 1, it is characterised in that described collection Gas branch pipe is arranged parallel to each other along the length direction of described gas gathering manifold,

Optionally, described gas-collecting branch pipe is perpendicular to described gas collecting main pipe.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 1, it is characterised in that described oil Gas delivery line road along the short transverse multi-tier arrangement of described pyrolysis reactor, every layer have much the most parallel to each other Oil gas derive pipeline,

Optionally, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 1, it is characterised in that described oil Gas delivery line road 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 symmetrical arranged Two oil gas are had to derive pipeline.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 5, it is characterised in that described oil Gas delivery line road is the 1/2-3 that described oil gas derives pipe diameter d with the spacing of the tube wall of neighbouring described heat accumulation type radiant tube Times.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 1, it is characterised in that described oil Multiple through hole it is provided with on the tube wall in gas delivery line road,

Optionally, the plurality of through hole is uniformly distributed on the length direction that described oil gas derives pipeline.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 1, it is characterised in that described rotation It is welded with support bar between outer wall and the described heat accumulation type radiant tube being adjacent of wind separator.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 1, it is characterised in that further Including:

Gas mixture after-treatment device, described gas mixture after-treatment device is connected with the outlet of described gas mixture.

Pyrolysis of coal reactor-recirculating fluidized bed combined system the most according to claim 9, it is characterised in that described oil Gas mixture after-treatment device includes:

Oil-gas Separation assembly, described Oil-gas Separation assembly has gas mixture import, pyrolysis gas outlet and tar outlet, institute State gas mixture import to be connected with the outlet of described gas mixture；

Pyrolysis gas purification assembly, described pyrolysis gas purification assembly has pyrolysis gas import and combustible gas outlet, and described pyrolysis gas enters Mouth is connected with described pyrolysis gas outlet,

Tar refining assembly, described tar refining assembly has tar entrance and oil product outlet, and described tar entrance is with described Tar outlet is connected.