CN205501185U - Remove bed pyrolytic reaction ware - Google Patents
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- CN205501185U CN205501185U CN201620077598.9U CN201620077598U CN205501185U CN 205501185 U CN205501185 U CN 205501185U CN 201620077598 U CN201620077598 U CN 201620077598U CN 205501185 U CN205501185 U CN 205501185U
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Abstract
The utility model discloses a remove bed pyrolytic reaction ware, include: matter entrance and semi -coke outlet, matter entrance is located the reactor top, semi -coke outlet is located the reactor bottom, regenerative radiant tube, regenerative radiant tube arrange along reactor height direction multilayer in that remove bed pyrolytic reaction ware is inside, and every layer has many parallel regenerative radiant tube each other on the horizontal direction, oil gas export pipeline is provided with the through -hole on oil gas export pipeline's the pipe wall, agitating unit, agitating unit include the (mixing) shaft and connect at the epaxial a plurality of puddlers of stirring that the (mixing) shaft is stretched into the inside of reactor and is set to by semi -coke outlet can be rotatory at reactor, discharge, discharge include gas collecting main and the gas collecting branch tubes who is linked together with gas collecting main, and gas collecting main sets up at the reactor outsidely vertically, and gas collecting branch tubes extends the lateral wall that passes the reactor and stretches into reactor and oil gas export pipeline intercommunication. This reactor can effectively suppress the secondary pyrolysis of oil gas, improves pyrolysis tar yield.
Description
Technical field
This utility model belongs to chemical field, and specifically, this utility model relates to a kind of moving bed pyrolysis reactor.
Background technology
The energy resource structure present situation of China is rich coal, gas oil-poor, few, and world today's petroleum resources gradually decreases, and day by day deficient, China's petroleum resources shortage is particularly acute, substantial amounts of petroleum resources dependence on import.Petroleum resources scarcity seriously governs China's economy and social development, the burning of the most a large amount of Fossil fuels, brings again serious environmental problem, such as dust, PM2.5, acid rain, greenhouse gases etc..Open up energetically coal liquifaction, coal gas technology, be pyrolyzed, gasify, liquefaction technology etc., on the one hand can effectively alleviate China's petroleum resources shortage, the poverty-stricken situation of heavy dependence import；On the other hand reduce the utilization of the Fossil fuels such as coal, can effectively solve, at present, the environmental problem that China's rapid economic development faces.According to incompletely statistics, there are the brown coal of more than 90% in China for station boiler and various Industrial Boiler.The low-order coal such as brown coal are directly burnt as power fuel, not only waste the hydrocarbon rich resource contained in coal, and efficiency is low, pollute weight.By middle low temperature pyrogenation technology and coal-char combustion, gasification decoupling, it is achieved low-order coal classification high-efficiency cleaning trans-utilization, is the Main way of present large-scale Coal Chemical Industry.Meanwhile, for China's high-sulfur, the IGCC technology of high ash, the biggest business efficiency, social benefit and environmental benefit will be realized.
Modern Coal-based Chemical is the high-efficiency cleaning trans-utilization realizing the carbon-containing fuels such as low-order coal, develop multiple comprehensive coal chemical technology, pyrolysis-burning decoupling, the decoupling of pyrolysis-chemicals, pyrolysis-gasification decoupling etc., but really realize industrialized few, during pilot scale is amplified to industrialization, encounter various technical barrier.The most especially with pyrolysis reactor design, subsequent purification process technique especially prominent.At present, the main type of furnace that carbon-containing fuel (coal, oil shale, biomass etc.) is pyrolyzed has Fushun stove, three river side's stoves, the solid heat carrier retort of Dalian University of Science & Engineering, loves the Galoter stove of husky Leah and the ATP stove of Australia etc..Some gas retorts can only be used for being pyrolyzed block oil shale and coal, and small particle material cannot utilize, and resource utilization is low, and granular material is because utilizing and bulk deposition；The type of furnace with gas as heat carrier, because condensate recovery system is huge, the problems such as pyrolysis gas calorific value is low, and tar yield is low, it is difficult to further genralrlization is demonstrated；The type of furnace with solid as heat carrier, then the problem such as there is raw material and heat carrier uniformly mixes, separation, and limit it and develop further.
Therefore, existing pyrolytic technique is further improved.
Utility model content
One of technical problem that this utility model is intended to solve in correlation technique the most to a certain extent.For this, a purpose of the present utility model is to propose a kind of moving bed pyrolysis reactor, this reactor can effectively suppress the second pyrolysis of oil gas, improve pyrolytic tar productivity, and have employed heat accumulating type without heat carrier heat accumulation type radiant tube heating technique, it is not necessary to gas, solid heat carrier, improve the calorific value of pyrolysis gas, to have taken into account equipment few for moving bed pyrolysis reactor simultaneously, easily operates, the advantage such as failure rate is low.
At an aspect of the present utility model, the utility model proposes a kind of moving bed pyrolysis reactor, according to embodiment of the present utility model, this reactor includes:
Material inlet and semicoke outlet；
Described material inlet is positioned at the top of described reactor；
The outlet of described semicoke is positioned at the bottom of described reactor；
Heat accumulation type radiant tube, described heat accumulation type radiant tube is in the inside of described moving bed pyrolysis reactor along the short transverse multi-tier arrangement of described reactor, and every layer has many heat accumulation type radiant tubes the most parallel to each other；
Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline；
Agitating device, described agitating device includes shaft and the multiple puddlers being connected on described shaft, and described shaft is extend into the inside of described reactor by the outlet of described semicoke and is configured to rotate in described reactor；
Discharge, described discharge includes gas gathering manifold and the gas-collecting branch pipe being connected with described gas gathering manifold,
Wherein, described gas gathering manifold is vertically situated at outside described reactor,
Described gas-collecting branch pipe extends through in the sidewall of described reactor extend into described reactor and derives pipeline with described oil gas and is connected.
Thus, moving bed pyrolysis reactor according to this utility model embodiment can effectively suppress the second pyrolysis of oil gas, improve pyrolytic tar productivity, and have employed heat accumulating type without heat carrier heat accumulation type radiant tube heating technique, it is not necessary to gas, solid heat carrier, improve the calorific value of pyrolysis gas, to have taken into account equipment few for moving bed pyrolysis reactor simultaneously, easily operates, the advantage such as failure rate is low, additionally by arranging agitating device in pyrolysis reactor, it is possible to augmentation of heat transfer effect.
Optional, described gas-collecting branch pipe is multiple, and arranged parallel to each other along the length direction of described gas gathering manifold.Thus, it is possible to the oil gas significantly improved in reactor derives efficiency.
Optional, described gas-collecting branch pipe is perpendicular to described gas collecting main pipe.
Optional, described oil gas derives the pipeline short transverse multi-tier arrangement along described reactor, and every layer has many oil gas the most parallel to each other and derives pipeline.Thus, it is possible to the oil gas improved further in reactor derives efficiency.
Optional, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and the respective left and right sides of described heat accumulation type radiant tube is symmetrically arranged with two oil gas and derives pipeline.Thus, it is possible to the oil gas improved further in reactor derives efficiency.
Optional, described oil gas derives 1/2-3 times that spacing is described oil gas derivation pipe diameter d of pipeline and the tube wall of neighbouring described heat accumulation type radiant tube.In embodiments more of the present utility model, described oil gas is derived and is provided with multiple through hole on the tube wall of pipeline.Thus, it is possible to the oil gas improved further in reactor derives efficiency.
Optional, described through hole is derived at described oil gas and is uniformly distributed on the length direction of pipeline.In embodiments more of the present utility model, oil gas described in same layer is derived pipeline and is communicated to same described gas-collecting branch pipe.
Optional, all there is one or more puddler the top of every layer of radial canal, and the vertical dimension of puddler and radial canal is 20～300mm.Thereby, it is possible to augmentation of heat transfer effect.Such as, puddler can be between radiation tube layer and oil gas delivery line channel layer for pyrolytic tar.
Optional, described puddler is perpendicular to described shaft, and spaced apart along the length direction of described shaft.Thus, it is possible to improve the yield of pyrolytic tar further.
Optional, described puddler adjacent projections on the same cross section of described shaft is at an angle.Thus, it is possible to improve the yield of pyrolytic tar further.
Optional, the angle ranging from 0～90 degree, without end value, it is preferred that the angle ranging from 30～90 degree, without 90 degree.Thus, it is possible to improve the yield of pyrolytic tar further.
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
Above-mentioned and/or additional aspect of the present utility model and advantage will be apparent from easy to understand, wherein from combining the accompanying drawings below description to embodiment:
Fig. 1 is the structural representation of the moving bed pyrolysis reactor according to one embodiment of this utility model；
Fig. 2 is the top view of the agitating device on the moving bed pyrolysis reactor according to one embodiment of this utility model；
Fig. 3 is the structural representation of the moving bed pyrolysis reactor according to this utility model further embodiment.
Detailed description of the invention
Of the present utility model embodiment is described below in detail, and the example of described embodiment is shown in the drawings, and the most same or similar label represents same or similar element or has the element of same or like function.The embodiment described below with reference to accompanying drawing is exemplary, it is intended to be used for explaining this utility model, and it is not intended that to restriction of the present utility model.
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.
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, the utility model proposes a kind of moving bed pyrolysis reactor.Moving bed pyrolysis reactor below with reference to-3 pairs of this utility model embodiments of Fig. 1 is described in detail.According to embodiment of the present utility model, moving bed pyrolysis reactor includes: material inlet 101, heat accumulation type radiant tube 11, oil gas derive pipeline 12, semicoke outlet 102, agitating device 13 and discharge 14.
According to embodiment of the present utility model, material inlet 101 is positioned at the top of reactor, and is suitable to supply the material to reactor.
According to embodiment of the present utility model, semicoke outlet 102 can be arranged on the bottom of reactor, and is suitable to pyrogenous origin semicoke is discharged reactor.
According to embodiment of the present utility model, heat accumulation type radiant tube 11 in the inside of moving bed pyrolysis reactor along the short transverse multi-tier arrangement of reactor, every layer has many heat accumulation type radiant tubes the most parallel to each other, according to specific embodiment of the utility model, heat accumulation type radiant tube the most parallel to each other is 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 utility model, the caliber of heat accumulation type radiant tube can be 100～300mm.According to embodiment of the present utility model, the horizontal range 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 range 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 the distance between the adjacent heat accumulation type radiant tube outer wall of adjacent upper and lower two interlayers.
According to embodiment of the present utility model, the number of plies of multilamellar heat accumulation type radiant tube can be 10-25 layer.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.
According to embodiment of the present utility model, heat accumulation type radiant tube can be unidirectional regenerative gas heat accumulation type radiant tube, 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 wait, by adjusting the flow of the combustion gas that gas control valve regulation is passed through heat accumulation type radiant tube, the accurate temperature controlling realized pyrolytic process, such that it is able to significantly improve the pyrolysis efficiency of material, and then improve the yield of pyrolytic tar.
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, 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 the regulation temperature range of the heat accumulation type radiant tube in epimere region in reactor be 500～800 DEG C, ensure the abundant pyrolysis of material, the flow of the combustion gas being passed through heat accumulation type radiant tube by adjustment makes the regulation temperature range of the heat accumulation type radiant tube in hypomere region in reactor be 450～650 DEG C, thus the material that a heating part further is pyrolyzed the most completely.
According to embodiment of the present utility model, oil gas is derived and is provided with through hole on the tube wall of pipeline 12, according to specific embodiment of the utility model, oil gas derives the pipeline 12 short transverse multi-tier arrangement along reactor, and every layer has many oil gas the most parallel to each other and derives pipeline.
According to specific embodiment of the utility model, 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 and derives pipeline 12.Inventor finds, derives pipeline by installing oil gas every heat accumulation type radiant tube both sides, and the oil gas that pyrolysis produces is derived pipeline by oil gas and derived rapidly, thus restrained effectively the second pyrolysis of oil gas, and then improves the yield of pyrolytic tar, good in economic efficiency.According to concrete example of the present utility model, it can be 30～80mm that oil gas derives the caliber of pipeline.
According to specific embodiment of the utility model, oil gas derives 1/2-3 times that spacing is oil gas derivation pipe diameter d of pipeline and the tube wall of neighbouring heat accumulation type radiant tube.Thus can derive the pyrolytic tar of generation at once, it is to avoid pyrolytic tar cracks, improve pyrolytic tar productivity.
According to specific embodiment of the utility model, oil gas is derived and is provided with multiple through hole on the tube wall of pipeline 12, it is preferable that multiple through holes are derived at oil gas and are uniformly distributed on the length direction of pipeline 12.Thus can be so that pyrolytic tar be quickly derived.
According to embodiment of the present utility model, agitating device 13 includes shaft 15 and the multiple puddlers 16 being connected on shaft 15, thus shaft 15 drives puddler 16 to rotate under the driving driving motor, according to specific embodiment of the utility model, shaft 15 rotatably extend into inside reactor from semicoke outlet 102.Utility model finds, by arranging agitating device in reactor, puddler, during carrying out back rotation, can be prevented effectively from the coking on radial canal surface, and then avoid reducing heat transfer efficiency because of radial canal coking such that it is able to strengthen heat-transfer effect.
According to specific embodiment of the utility model, all there is one or more puddler the top of every layer of radial canal, and the vertical dimension of puddler and radial canal is 20～300mm.Thus can avoid the upper coking of radial canal, it is ensured that equipment is properly functioning.Such as, puddler can be between radiation tube layer and oil gas delivery line channel layer.
According to specific embodiment of the utility model, puddler 16 is perpendicular to shaft 15, and spaced apart along the length direction of shaft 15.
According to specific embodiment of the utility model, the puddler 16 adjacent projections on the same cross section of shaft 15 is at an angle.Such as, as in figure 2 it is shown, described angle, θ can be 0～90 degree (without end value), preferably 30～90 degree (without 90 degree).Thus, it is possible to make puddler effectively loosen inside reactor material such that it is able to quickly derive oil gas pyrolytic tar.The length of central stirring shaft can be 1-18m, and detachable puddler vertical interval can be 0.4-1m, and the number of plies can be 11-26 layer.
According to embodiment of the present utility model, discharge 14 includes gas gathering manifold 17 and the gas-collecting branch pipe 18 connected with gas gathering manifold 17, according to specific embodiment of the utility model, gas gathering manifold 17 is vertically situated at outside reactor, and gas-collecting branch pipe 18 extends through in the sidewall of reactor extend into 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 specific embodiment of the utility model, 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 utility model, gas-collecting branch pipe 18 is perpendicular to gas collecting main pipe 17.Thus, multiple gas-collecting branch pipes 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 utility model, as it is shown in figure 1, same layer oil gas derives pipeline 12 is communicated to same gas-collecting branch pipe 18.
According to embodiment of the present utility model, reactor head can spherically type or taper.
According to embodiment of the present utility model, the bottom of reactor can be in inverted cone.Thus, it is possible to make pyrogenous origin semicoke discharge reactor smoothly.
nullMoving bed pyrolysis reactor according to this utility model embodiment provides thermal source by using many group heat accumulation type radiant tubes 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 heat accumulation type radiant tube passes through heat storage type combustion，Ensure that the uniformity in temperature field，Such that it is able to significantly improve the pyrolysis efficiency of material，And then improve the yield of pyrolytic tar，The most traditional use gas heat carrier or solid thermal carriers are compared as the pyrolytic reaction device being pyrolyzed thermal source，Moving bed pyrolysis reactor of the present utility model need not arrange preheating unit and carrier separative element，Such that it is able to greatly simplify pyrolytic reaction technological process，And then it is relatively low to significantly reduce dust content in the fault rate of device and gained pyrolytic tar，And exhaust gas temperature is low，Secondly this utility model is by arranging that in the both sides 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 gas heat carrier，Pyrolysis gas calorific value is high，Good in economic efficiency，Heat accumulation type radiant tube is coordinated additionally by arranging agitating device in reactor，Puddler is during carrying out back rotation，Stacking material is loosened，Increase the voidage between stacking material，Reduce pyrolytic tar gas through material bed pressure drop，Make the pyrolytic tar gas produced can pass rapidly through material bed arrival oil gas delivery line，The pyrolytic tar gas produced can be derived by oil gas delivery line in time，And it can be avoided that radial canal upper end coking，Thus avoid affecting heat transfer efficiency.
According to embodiment of the present utility model, with reference to Fig. 3, moving bed pyrolysis reactor farther includes: hopper 19, feed screw 20 and spiral discharging machine 21.
According to this utility model volume embodiment, hopper 19 is suitable to store material to be pyrolyzed.
According to embodiment of the present utility model, feed screw 20 is connected with hopper 19 and material inlet 101 respectively, and is suitable to the material to be pyrolyzed in hopper in material inlet supply to reactor.
According to embodiment of the present utility model, spiral discharging machine 21 is arranged on the lower section of reactor, and is connected with semicoke outlet 102.
nullSpecifically，The accurate temperature controlling to pyrolytic process is realized by adjusting the flow etc. of the combustion gas that the regulation valve regulation on gas pipeline is passed through unidirectional heat accumulation type radiant tube，Making reactor upper temp scope is 680～730 DEG C，The flow of the combustion gas being passed through heat accumulation type radiant tube by adjustment makes reactor middle portion temperature scope be 500～650 DEG C，The flow of the combustion gas being passed through heat accumulation type radiant tube by adjustment makes reactor lower part temperature range be 500～600 DEG C，Material enters in reactor from material inlet through feed screw from hopper，Material scatter after drying on reactor top，Material is made uniformly to be scattered in generation pyrolytic reaction in the middle part of reactor，And the agitating device in reactor is so that puddler is during carrying out back rotation，Stacking material is loosened，Increase the voidage between stacking material，Reduce pyrolytic tar gas through material bed pressure drop，Make the pyrolytic tar gas produced can pass rapidly through what material bed arrival oil gas delivery line entered，The pyrolytic tar gas generated is derived to gas gathering manifold through gas-collecting branch pipe，And the semicoke being pyrolyzed generation drains into spiral discharging machine from semicoke outlet.
As it has been described above, can have selected from least one following advantage according to the moving bed pyrolysis reactor of this utility model embodiment:
Moving bed pyrolysis reactor employing heat accumulation type radiant tube heat supply according to this utility model embodiment, response system simple in construction, easy to operate, internal temperature field uniform, controllable；
It is provided with 1～2 oil gas delivery line bottom every heat accumulation type radiant tube of moving bed pyrolysis reactor according to this utility model embodiment, for quickly deriving pyrolytic tar gas, restrained effectively the second pyrolysis of pyrolytic tar, pyrolytic tar quality better, productivity is high, meanwhile, pyrolysis coal gas is not diluted by carrier gas, and calorific value is high；
Moving bed pyrolysis temperature of reactor field according to this utility model embodiment is controlled, can be different according to different material pyrolysis characteristics, reasonably regulating and controlling temperature field and temperature field length.
Below with reference to specific embodiment, this utility model is described, it should be noted that these embodiments are the most illustrative, and limits this utility model never in any form.
Embodiment 1
The present embodiment 1 utilizes the moving bed pyrolysis reactor of Fig. 1-3 to process brown coal.The Industrial Analysis of brown coal: Mad%:6.75%, Vad%:31.59%, Aad%:5.41%, Fcad%:56.25%.
Technological parameter: heat accumulation type radiant tube reactor drying and dehydrating district temperature is 690 DEG C, and pyrolysis reaction region temperature is 625 DEG C, and semicoke maturation zone temperature is 594 DEG C, heat accumulation type radiant tube reactor internal pressure 2.51Kpa.Pyrolysis tertiary industry distribution: pyrolytic tar 17.4%, pyrolysis gas 12.8%, semicoke 69.8%.
Embodiment 2
The present embodiment 2 utilizes the moving bed pyrolysis reactor of Fig. 1-3 to process rice husk.The Industrial Analysis of rice husk: Mad%:6.56%, Vad%:65.17%, Aad%:11.52%, Fcad%:16.75%.Elementary analysis: Cad%:40.69%, Had%:4.96%, Nad%:0.05%, Oad%；35.13%.
Technological parameter: heat accumulation type radiant tube reactor drying and dehydrating district temperature is 680 DEG C, and pyrolysis reaction region temperature is 560 DEG C, and semicoke maturation zone temperature is 520 DEG C, heat accumulation type radiant tube reactor internal pressure 4.77Kpa.Pyrolysis tertiary industry distribution: pyrolytic tar 43.3%, pyrolysis gas 17.1%, semicoke 39.6%.
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. a moving bed pyrolysis reactor, it is characterised in that including:
Material inlet and semicoke outlet；
Described material inlet is positioned at the top of described reactor；
The outlet of described semicoke is positioned at the bottom of described reactor；
Heat accumulation type radiant tube, described heat accumulation type radiant tube in the inside of described moving bed pyrolysis reactor along described reactor
Short transverse multi-tier arrangement, every layer has many heat accumulation type radiant tubes the most parallel to each other；
Oil gas derives pipeline, and described oil gas is derived and is provided with through hole on the tube wall of pipeline；
Agitating device, described agitating device includes shaft and the multiple puddlers being connected on described shaft, described stirring
Axle is extend into the inside of described reactor by the outlet of described semicoke and is configured to rotate in described reactor；
Discharge, described discharge includes gas gathering manifold and the gas-collecting branch pipe being connected with described gas gathering manifold,
Wherein, described gas gathering manifold is vertically situated at outside described reactor,
Described gas-collecting branch pipe extends through in the sidewall of described reactor extend into described reactor and derives pipeline with described oil gas
It is connected.
Moving bed pyrolysis reactor the most according to claim 1, it is characterised in that described gas-collecting branch pipe is multiple, and
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.
Moving bed pyrolysis reactor the most according to claim 1, it is characterised in that described oil gas derives pipeline along described
The short transverse multi-tier arrangement of reactor, every layer has many oil gas the most parallel to each other and derives pipeline,
Optional, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and described heat accumulation type radiant tube is each
The left and right sides be symmetrically arranged with two oil gas and derive pipelines.
Moving bed pyrolysis reactor the most according to claim 3, it is characterised in that described oil gas derives pipeline with neighbouring
The spacing of tube wall of described heat accumulation type radiant tube be that described oil gas derives pipe diameter d 1/2-3 times.
Moving bed pyrolysis reactor the most according to claim 3, it is characterised in that described oil gas derives the tube wall of pipeline
On be provided with multiple through hole.
Moving bed pyrolysis reactor the most according to claim 5, it is characterised in that oil gas described in same layer derives pipeline
It is communicated to same described gas-collecting branch pipe.
Moving bed pyrolysis reactor the most according to claim 1, it is characterised in that described puddler is between heat accumulating type spoke
Penetrate between tube layer and oil gas delivery line channel layer.
Moving bed pyrolysis reactor the most according to claim 7, it is characterised in that described puddler be perpendicular to described in stir
Mix axle, and spaced apart along the length direction of described shaft.
Moving bed pyrolysis reactor the most according to claim 8, it is characterised in that described puddler is at described shaft
Same cross section on adjacent projections at an angle.
Moving bed pyrolysis reactor the most according to claim 9, it is characterised in that the angle ranging from 0～90 degree, no
Containing end value.
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| CN201620077598.9U CN205501185U (en) | 2016-01-27 | 2016-01-27 | Remove bed pyrolytic reaction ware |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105505412A (en) * | 2016-01-27 | 2016-04-20 | 北京神雾环境能源科技集团股份有限公司 | Moving bed pyrolysis reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105505412A (en) * | 2016-01-27 | 2016-04-20 | 北京神雾环境能源科技集团股份有限公司 | Moving bed pyrolysis reactor |
| CN105505412B (en) * | 2016-01-27 | 2017-12-08 | 神雾科技集团股份有限公司 | Moving bed pyrolysis reactor |
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