CN106281371A - Pyrolysis reactor - Google Patents
Pyrolysis reactor Download PDFInfo
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- CN106281371A CN106281371A CN201610708706.2A CN201610708706A CN106281371A CN 106281371 A CN106281371 A CN 106281371A CN 201610708706 A CN201610708706 A CN 201610708706A CN 106281371 A CN106281371 A CN 106281371A
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- catalyst
- pyrolysis reactor
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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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
-
- 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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of pyrolysis reactor.This pyrolysis reactor includes: charging aperture, oil gas vent, semicoke export, and heat accumulation type radiant tube, catalyst transport assembly and mixing component.This pyrolysis reactor can realize uniformly spraying in pyrolysis reactor raw material fast pyrogenation and catalyst simultaneously.
Description
Technical field
The present invention relates to pyrolysis reactor.
Background technology
Pyrolysis reactor is the reactor that chemical field is conventional.The most conventional pyrolysis reactor mainly includes the three of China
Jiang Fanglu, the hot solid carrier devolatilization technique stove of big work Dalian University of Science & Engineering and multistage rotary furnace pyrolytic process device, such as, external
Wood stove, the strange three sections of stoves in Shandong, Kao Baisi stove and LFC retorting technique stove etc..Some dry distilling type of furnaces are high to the Particle size requirements of raw material,
Can only be pyrolyzed lumped coal, cause small particles material to make full use of, resource utilization is the highest and bulk deposition pollutes environment
Problem；The oily yield of some type of furnaces is relatively low, and with gas as heating carrier, causes condensate recovery system huge, and pyrolysis is dry
Evaporating gas and rushed dilute, gas heating value is low, it is difficult to the problems such as further comprehensive utilization；Some use the pyrolysis type of furnace of solid thermal carriers,
Then there is raw material to mix with heat carrier, and heat carrier reheats the operations such as back-mixing, technique is complex, equipment is more, manufactures
Cost and operating cost are high.Additionally, in existing industry pyrolytic process all for the purpose of producing a large amount of tar, pyrolysis gas yield
Less, or pyrolysis gas burnt utilization by following cycle technique, What is more to the pyrolytic gas making of coal and liquefaction degree the most not
Enough.Thus, pyrolysis reactor is further improved.
Summary of the invention
It is contemplated that at least solve one of technical problem present in prior art.To this end, one object of the present invention
It is that proposing a kind of can simultaneously realization uniformly sprays into the pyrolysis reactor in pyrolysis oven by raw material fast pyrogenation and catalyst, should
Pyrolysis reactor utilizes catalyst transport assembly to carry catalyst to pyrolysis inside reactor, and utilizes mixing component by catalyst
Stir in pyrolysis reactor with raw material, and then, fast pyrogenation is blended by this pyrolysis reactor with catalytic pyrolysis technology,
The pyrolysis oil preparation being capable of small particles material is gentle, significantly improves the yield of pyrolysis gas and obtains a certain amount of pyrolysis oil.This
Outward, this pyrolysis reactor have employed heat accumulation type radiant tube heating technique, it is not necessary to gas, solid heat carrier heating, improves reactor
Consersion unit is simplified while the thermal efficiency.
Thus, according to an aspect of the present invention, the invention provides a kind of pyrolysis reactor.Enforcement according to the present invention
Example, this pyrolysis reactor includes: charging aperture, oil gas vent, semicoke export, and wherein, the outlet of described semicoke is positioned at reactor bottom；
Heat accumulation type radiant tube, described heat accumulation type radiant tube inside described pyrolysis reactor along the height of described pyrolysis reactor
Degree direction multi-tier arrangement, every layer has many heat accumulation type radiant tubes the most parallel to each other；Catalyst transport assembly,
Described catalyst transport assembly includes: catalyst hooper；Catalyst is responsible for, and described catalyst supervisor is vertically situated at described heat
Outside solution reactor；Described catalyst supervisor be connected with described catalyst hooper；Catalyst arm, described catalyst arm is worn
Cross the sidewall of described pyrolysis reactor and extend to the inside of described pyrolysis reactor, described catalyst arm and described catalyst
Supervisor is connected；One or more catalyst ejector parts, described catalyst ejector part is arranged on described catalyst arm, and position
Inside described pyrolysis reactor, carrier gas delivers part, and described carrier gas delivers part and is connected with described catalyst supervisor, described carrier gas
Deliver the inside that part is configured to be suitable to that catalyst is blown into described pyrolysis reactor；Mixing component, described mixing component includes:
Rotatable shaft, described shaft is extend into the inside of described pyrolysis reactor by the outlet of described semicoke；Multiple puddlers,
Described puddler is connected on described shaft along the length of described shaft, and described puddler is positioned at described heat accumulating type spoke
Penetrate the interlayer of pipe.
The present inventor devises one for existing pyrolysis reactor and can realize raw material fast pyrogenation simultaneously and urge
Agent uniformly sprays into the pyrolysis reactor in pyrolysis oven, and this pyrolysis reactor utilizes catalyst transport assembly in pyrolysis reactor
Portion's conveying catalyst, and utilize mixing component catalyst and raw material to be stirred in pyrolysis reactor, effectively loosen thing
Material, makes the oil gas of generation discharge as early as possible, reduces second pyrolysis, improves oil yield, adds the mixing of powerful catalyst and coal charge, further
Improve catalytic efficiency.Thus, fast pyrogenation is blended by this pyrolysis reactor with catalytic pyrolysis technology, it is possible to realize small particle
The pyrolysis oil preparation of material is gentle, significantly improves the yield of pyrolysis gas and obtains a certain amount of pyrolysis oil.Additionally, this pyrolysis reactor is adopted
By heat accumulation type radiant tube heating technique, it is not necessary to gas, solid heat carrier heating, simplify while improve the thermal efficiency of reactor
Consersion unit, has important social benefit, economic benefit and environmental benefit.
Wherein it is desired to explanation, in the present invention, " pyrolysis reactor " and " heat accumulating type descending-bed reactor " can be mutual
Change use.
In one embodiment of the invention, described pyrolysis reactor specific reactor body, described reacting body has
There are charging aperture and discharging opening, in described reactor body, limit reaction compartment.
In one embodiment of the invention, catalyst supervisor is arranged on the outside of described reactor body.
In one embodiment of the invention, the sidewall of reactor body described in the plurality of catalyst Zhi Jing enters institute
State in reaction compartment.
In one embodiment of the invention, during described mixing component is arranged on described reaction compartment.
In one embodiment of the invention, described pyrolysis reactor includes charging aperture, fuel gas inlet, air intake and
Pyrolysis oil gas vent, exhanst gas outlet, semicoke outlet, catalyst ejector part entrance and the outlet of catalyst ejector part.An enforcement
In scheme, charging aperture is arranged on the top of pyrolysis reactor.
In one embodiment of the invention, described shaft utilizes motor-driven.
In one embodiment of the invention, described catalyst arm is multiple, and be responsible for along described catalyst
Length direction is arranged parallel to each other.
In one embodiment of the invention, described catalyst arm is perpendicular to described catalyst supervisor.
In one embodiment of the invention, described catalyst arm extends to the whole of described heat accumulation type radiant tube layer
Slice width degree.
In one embodiment of the invention, described catalyst arm is arranged on the interlayer of described heat accumulation type radiant tube.
In a preferred embodiment of the invention, described catalyst arm is parallel with heat accumulation type radiant tube every layer described.
In one embodiment of the invention, described catalyst ejector part is arranged in the layer of described heat accumulation type radiant tube
Between.
In one embodiment of the invention, described catalyst ejector part includes catalyst jet pipe and urges described in being arranged on
Nozzle on agent jet pipe, described nozzle is provided with regulation valve.
In one embodiment of the invention, described catalyst jet pipe is U-shaped, S type or W type jet pipe.
In one embodiment of the invention, described catalyst ejector part includes catalyst jet pipe, and described catalyst sprays
It is provided with through hole on the tube wall of pipe.
In one embodiment of the invention, described catalyst arm is arranged on the interlayer of described heat accumulation type radiant tube,
And described catalyst ejector part is arranged in the interlayer of described heat accumulation type radiant tube.
In one embodiment of the invention, described carrier gas delivers part and is connected to the end of described catalyst supervisor, excellent
Selection of land, described carrier gas delivery part is detachably connected or is soldered to described catalyst supervisor.
In one embodiment of the invention, the number of plies of described catalyst arm is 10-25 layer, every layer of described catalyst
There is on arm 4-15 catalyst ejector part.
In one embodiment of the invention, it is respectively provided with between the described heat accumulation type radiant tube that any level is adjacent
State catalyst ejector part.
In one embodiment of the invention, described puddler is perpendicular to described shaft, and along described shaft
Length separation distribution.
In one embodiment of the invention, the projection on the same cross section of described shaft of the described puddler in
Certain angle.It is preferably carried out in scheme of the present invention, the angle ranging from 0-90 degree.At one of the present invention more preferably
In ground embodiment, the angle ranging from 30～90 degree.
In one embodiment of the invention, multiple described puddlers divide at the spaced apart lengths of described shaft
Cloth.
In one embodiment of the invention, described heat accumulation type radiant tube is the round tube of a diameter of 200-300 millimeter.
In one embodiment of the invention, the level interval between the described heat accumulation type radiant tube of arbitrary neighborhood is
200-500mm, vertical interval is 200-700mm.
In one embodiment of the invention, the number of plies of described multilamellar heat accumulation type radiant tube is 10-25 layer.
The additional aspect of the present invention and advantage will part be given in the following description, and part will become from the following description
Obtain substantially, or recognized by the practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or the additional aspect of the present invention and advantage are from combining the accompanying drawings below description to embodiment and will become
Substantially with easy to understand, wherein:
Fig. 1 shows the structural representation of pyrolysis reactor according to an embodiment of the invention；
Fig. 2 shows the structural representation of pyrolysis reactor according to an embodiment of the invention；
Fig. 3 shows the structural representation of the catalyst ejector part in pyrolysis reactor according to an embodiment of the invention
Figure；
Fig. 4 shows the top view of the mixing component in pyrolysis reactor according to an embodiment of the invention.
Detailed description of the invention
Embodiments of the invention are described below in detail, and the example of described embodiment is shown in the drawings, the most from start to finish
Same or similar label represents same or similar element or has the element of same or like function.Below with reference to attached
The embodiment that figure describes is exemplary, is only used for explaining the present invention, and is not considered as limiting the invention.
In describing the invention, term " longitudinally ", " laterally ", " on ", D score, "front", "rear", "left", "right", " perpendicular
Directly ", " level ", " top ", the orientation of the instruction such as " end " or position relationship be based on orientation shown in the drawings or position relationship, be only
For the ease of describing the present invention rather than requiring that the present invention must be with specific azimuth configuration and operation, therefore it is not intended that right
The restriction of the present invention.
It should be noted that term " first ", " second " are only used for describing purpose, and it is not intended that instruction or hint phase
To importance or the implicit quantity indicating indicated technical characteristic.Thus, define " first ", " second " feature permissible
Express or implicitly include one or more this feature.Further, in describing the invention, unless otherwise saying
Bright, " multiple " are meant that two or more.
According to an aspect of the present invention, the invention provides a kind of pyrolysis reactor.
Surprisingly, it was found that the pyrolysis reactor in embodiments of the invention can realize raw material simultaneously quick
Pyrolysis and catalyst uniformly spray in pyrolysis oven, utilize catalyst transport assembly to carry catalyst to pyrolysis inside reactor, and
Utilize mixing component catalyst and raw material to be stirred in pyrolysis reactor, effectively loosen material, make the oil gas of generation
Discharge as early as possible, reduce second pyrolysis, improve oil yield, add the mixing of powerful catalyst and coal charge, improve catalytic efficiency further.By
This, fast pyrogenation is blended by this pyrolysis reactor with catalytic pyrolysis technology, it is possible to realize small particles material pyrolysis oil preparation and
Gas, significantly improves the yield of pyrolysis gas and obtains a certain amount of pyrolysis oil.
Additionally, this pyrolysis reactor also has the further advantage that.Such as, this pyrolysis reactor have employed heat accumulation type radiant tube and adds
Thermal technology, it is not necessary to gas, solid heat carrier heating, simplifies consersion unit while improve the thermal efficiency of reactor, has important
Social benefit, economic benefit and environmental benefit.
Additionally, the pyrolysis reactor of the embodiment of the present invention takes heat accumulation type radiant tube down-flow fluidized bed using ECT technique, response system structure
Simply, easy to operate, uniformity of temperature profile, heats is good.
Additionally, the pyrolysis reactor of the embodiment of the present invention can process the fine coal of below 2mm, raw material availability is high, is suitable to
Promote.
Additionally, compared with traditional aluminum rice steamer method carbonization gas productivity, the pyrolysis reactor of the embodiment of the present invention uses catalyst
Coal is carried out be catalyzed fast pyrogenation, the gas production of the highest carbonization gas improve 50%.
Additionally, the pyrolysis reactor of the embodiment of the present invention uses heat accumulation type radiant tube to be pyrolyzed, system can not only be improved
The thermal efficiency, and ensure that the uniformity in temperature field.The combustion system that heat accumulation type radiant tube periodically commutates so that single storage
The surface temperature difference of hot type radial canal only has about 30 DEG C, does not has district of localized hyperthermia.
Additionally, the pyrolysis reactor of the embodiment of the present invention uses heat accumulation type radiant tube combustion heat supplying technology, surface temperature difference is little,
Exhaust gas temperature is low, and the thermal efficiency is high.
Fig. 1 shows the pyrolysis reactor of another embodiment of the present invention.As it is shown in figure 1, pyrolysis reactor includes: reaction
Device body 100, multilamellar heat accumulation type radiant tube 200, catalyst transport assembly 300 and mixing component 400.
Wherein, reacting body 100 has charging aperture and discharging opening, limits reaction compartment 110 in this reactor body.
Multilamellar heat accumulation type radiant tube 200 is spaced apart along reactor body 100 short transverse in described reaction compartment, and
And every layer of heat accumulation type radiant tube includes the heat accumulation type radiant tube of multiple horizontally spaced distribution, heat accumulation type radiant tube has heat
Solving oil gas vent, multilamellar heat accumulation type radiant tube 200 is for being pyrolyzed reaction raw materials.
Catalyst transport assembly 300 includes: catalyst hooper 340, catalyst supervisor 310, multiple catalyst arm 320,
Many catalyst ejector parts 330 and carrier gas deliver part (not shown), and wherein, catalyst hooper 340 is used for depositing catalyst,
Catalyst supervisor 310 has catalyst feeds and multiple first catalyst outlet, and catalyst supervisor is arranged on described reactor
The outside of body, catalyst supervisor 310 is connected with catalyst hooper 340；Multiple catalyst arms 320 and multiple first catalysis
Agent outlet one_to_one corresponding also connects, and in the sidewall described reaction compartment of entrance of described reactor body, each catalyst props up
Pipe 320 be all set in parallel in two-layer heat accumulation type radiant tube adjacent in horizontal direction in described multilamellar heat accumulation type radiant tube 200 it
Between space in；Many catalyst ejector parts, described many catalyst ejector parts are arranged on the plurality of catalyst arm, and
Being positioned at reaction compartment, each catalyst ejector part is respectively provided with nozzle；Carrier gas delivers part, and described carrier gas delivers part and described catalysis
Agent supervisor be connected, and described carrier gas delivers the inside that part is configured to be suitable to that catalyst is blown into described pyrolysis reactor.Utilize
Catalyst transport assembly, by catalyst transport to reaction compartment, arranges many catalyst ejector parts at catalyst arm, makes every
Being furnished with catalyst ejector part around heat accumulation type radiant tube, catalyst is sprayed in coal charge layer equably by catalyst ejector part.
Mixing component 400 is arranged in reaction compartment, and this mixing component 400 includes: rotatable shaft 410 and multiple
Puddler 420, wherein, described shaft is extend into the inside of described pyrolysis reactor, multiple puddlers by the outlet of described semicoke
420 are interspersed on described shaft, and each puddler is arranged at horizontal direction in described multilamellar heat accumulation type radiant tube
In space between upper adjacent two-layer heat accumulation type radiant tube.Utilize agitating device effectively to loosen material, make catalyst and coal
The mixing that material is more uniformly distributed, improves catalytic efficiency, the oil gas of generation can be made to discharge as early as possible simultaneously, reduces second pyrolysis, improves
Oil yield.
In one embodiment of the invention, motor-driven shaft 410 is utilized to rotate.
In one embodiment of the invention, described catalyst arm 320 is multiple, and is responsible for along described catalyst
Length direction arranged parallel to each other.Thus, in reaction compartment, the material of diverse location sprays catalyst.
In one embodiment of the invention, described catalyst arm 320 is perpendicular to described catalyst supervisor 310.
In one embodiment of the invention, described catalyst arm 320 extends to described heat accumulation type radiant tube layer
Whole slice width degree.I.e. catalyst arm 320 arrives the tail end of heat accumulation type radiant tube layer through heat accumulation type radiant tube layer.Thus, make
Catalyst sprays in reaction compartment material everywhere, it is ensured that catalyst and the full and uniform mixing of material.
In one embodiment of the invention, the number of plies of described catalyst arm is 10-25 layer, every layer of described catalyst
There is on arm 4-15 catalyst ejector part.This kind of structure is arranged so that uniform distribution of temperature field in pyrolysis reaction region,
Such that it is able to significantly improve the pyrolysis efficiency of material, and then improve the yield of pyrolysis oil.
In one embodiment of the invention, it is respectively provided with between the described heat accumulation type radiant tube that any level is adjacent
State catalyst ejector part.Thereby it is ensured that catalyst is ejected in material equably.
In one embodiment of the invention, described catalyst ejector part 330 includes catalyst jet pipe 331 and is arranged on
Nozzle 332 on described catalyst jet pipe, described nozzle is provided with regulation valve.Thus, regulation valve regulation catalyst is utilized
Straying quatity, it is ensured that catalytic reaction efficient is carried out.
In one embodiment of the invention, described catalyst ejector part 330 is U-shaped, S type or W type jet pipe.
With reference to Fig. 3, in one embodiment of the invention, catalyst ejector pipe 330 can by multiple in the horizontal direction
Multiple muonic catalysis agent jet pipes 333 that spaced apart and head and the tail are sequentially connected form, and the tube wall of each muonic catalysis agent jet pipe has
Multiple catalyst spray orifices 332.Thus, use the catalyst coil pipe of specific form, catalyst arm the catalyst come is in catalysis
Agent jet pipe is carried by noble gas and sprays in pyrolysis reactor.Catalyst can be evenly distributed in pyrolysis reactor,
Uniformly mix with raw material, and then catalysis pyrolytic reaction, improve pyrolysis efficiency.
In one embodiment of the invention, described catalyst ejector part includes catalyst jet pipe, and described catalyst sprays
It is provided with through hole on the tube wall of pipe.
In one embodiment of the invention, one end of catalyst arm is detachably connected on catalyst supervisor also
In communication, one end of catalyst jet pipe connects with the other end of catalyst arm, and the other end of catalyst jet pipe is fixed on stove
On wall, thus, catalyst jet pipe is across inside pyrolysis reactor on the width of reactor.The bottom of catalyst supervisor
Connect with gas reservoir.Noble gas is blown into catalyst supervisor by gas reservoir, thus catalyst is blown into catalyst jet pipe.Lazy
Property gas can be nitrogen etc..Catalyst jet pipe can be U-shaped, S type or W type, needs to explain, group catalyst jet pipe number is
Being U-shaped when 2, group catalyst jet pipe number is S type when being 3.
In one embodiment of the invention, described catalyst arm 320 is arranged on described heat accumulation type radiant tube 200
Interlayer, and described catalyst ejector part 330 is arranged in the interlayer of described heat accumulation type radiant tube 200.
Catalyst arm is arranged at radial canal interlayer can effectively prevent powder-material blocking catalyst jet pipe, can ensure thing simultaneously
Material manage via radiation uniform after can mix with catalyst uniform contact, it is ensured that good reaction effect, while can prevent catalyst from propping up
Pipe weares and teares, and extends its service life, reduces and changes number of times.According to the concrete example of the present invention, the number of muonic catalysis agent jet pipe can
Depending on according to the radial canal number in every layer of heat accumulation type radiant tube, and then so that join around every heat accumulation type radiant tube
There is catalyst jet pipe, and then improve the catalyst addition uniformity, and reaction degree of being heated evenly.The catalyst of particle diameter≤0.5mm
It is sprayed on equably in coal charge layer by catalyst jet pipe.Catalyst jet pipe uses the round tube of DN30-80, and catalyst is by urging
Agent is responsible in catalyst arm is blown into the catalyst jet pipe of every layer.
In one embodiment of the invention, described puddler 420 is positioned at described heat accumulation type radiant tube layer 200 with described
Between catalyst arm 320.Thus can effectively loosen inside reactor material, thus improve leading of pyrolysis oil gas further
Go out rate, avoid coking on heat accumulation type radiant tube, it is ensured that equipment is properly functioning simultaneously.
In one embodiment of the invention, described puddler 420 is perpendicular to described shaft 410, and along described
The length separation distribution of shaft 410.Thus, it is possible to make puddler effectively loosen inside reactor material, such that it is able to
Significantly improve the derivation rate of pyrolysis oil gas.
According to another specific embodiment of the present invention, as shown in Figure 4, on the shaft section of shaft 410, multiple stirrings
It is evenly spaced apart distribution, according to the concrete example of the present invention, at shaft in the circumference being projected in shaft 410 of bar 420
On the shaft section of 410, in the projection of multiple puddlers 420, the adjacent angle theta between two puddlers 420 can be 0～90
Degree, preferably 30～90 degree.Thus, it is possible to make puddler effectively loosen inside reactor material, thus improve heat further
Solve the derivation rate of oil gas.According to the concrete example of the present invention, the angle between every layer of puddler 420, can be 180 degree, it is possible to
It is distributed between 0-90 degree.The length of shaft 410 can be 1-18m, and detachable puddler vertical interval can be 0.4-1m, layer
Number can be 11-26 layer.
According to embodiments of the invention, heat accumulation type radiant tube can be unidirectional regenerative gas radial canal, i.e. by radiation
The heat that combustion gas is produced by pipe body carries out heat supply in the way of radiation.According to a particular embodiment of the invention, heat accumulating type
Gas control valve (not shown) can be provided with on radial canal.Thus, it is possible to be passed through accumulation of heat by adjusting gas control valve regulation
The flow of the combustion gas of formula radial canal waits the accurate temperature controlling realized pyrolytic process, such that it is able to significantly improve the pyrolysis effect of material
Rate, and then improve the yield of pyrolysis oil.
Concrete, accurate to pyrolytic process of the realization such as flow of the combustion gas of heat accumulation type radiant tube can be passed through by adjustment
Temperature control, and heat accumulation type radiant tube uses the combustion system of periodically commutation so that the temperature field of single radial canal be more or less the same in
30 DEG C, and there is no partial insulation district, thus ensure the uniformity in temperature field in reactor body, make the temperature control in reaction compartment
System is in the range of 450-750 degree Celsius.
Wherein, the model of radial canal and adjacent can adjust according to the volume of reaction compartment, the kind of reaction mass etc.
Whole.In specific embodiments of the present invention, heat accumulation type radiant tube is the round tube of a diameter of 200-300 millimeter.In the present invention
Specific embodiments in, the level interval between the heat accumulation type radiant tube of arbitrary neighborhood is 200-500mm, and vertical interval is
200-700mm.Thus, be pyrolyzed effective.
The number of plies of multilamellar heat accumulation type radiant tube can also be adjusted according to the volume of reaction compartment, the kind of reaction mass etc.
Whole.According to some embodiments of the present invention, the number of plies of multilamellar heat accumulation type radiant tube is 10-25 layer, it is ensured that accumulation of heat in reaction compartment
The distribution density of formula radial canal is suitable, fully meets the needs of pyrolytic reaction.
The volume of reactor body can be adjusted according to the treating capacity of pyrolysis reactor.Some according to the present invention are real
Executing example, the width of reactor body is 2-6m, and height is 3-20m.
Fig. 2 shows the pyrolysis reactor of embodiments of the invention.As in figure 2 it is shown, this pyrolysis reactor farther includes:
Spiral discharging device 700, described spiral discharging device 700 is connected with described discharging opening.
As in figure 2 it is shown, this pyrolysis reactor farther includes: feed hopper 500 and feeding screw 600, described spiral enters
Glassware 600 is connected with described feed hopper 500 and described charging aperture, is crushed through feeding screw by the question response thing in feed hopper and adds
Work rear feeding mouth supplies to reactor body.
Claims (9)
1. a pyrolysis reactor, it is characterised in that including:
Charging aperture, oil gas vent, semicoke export, and wherein, the outlet of described semicoke is positioned at reactor bottom；
Heat accumulation type radiant tube, described heat accumulation type radiant tube inside described pyrolysis reactor along the height side of described pyrolysis reactor
To multi-tier arrangement, every layer has many heat accumulation type radiant tubes the most parallel to each other；
Catalyst transport assembly, described catalyst transport assembly includes:
Catalyst hooper；
Catalyst be responsible for, described catalyst supervisor be vertically situated at outside described pyrolysis reactor, described catalyst supervisor with
Described catalyst hooper is connected；
Catalyst arm, described catalyst arm passes the sidewall of described pyrolysis reactor and extends to described pyrolysis reactor
Inside, described catalyst arm is connected with described catalyst supervisor；
One or more catalyst ejector parts, described catalyst ejector part is arranged on described catalyst arm, and is positioned at described
Inside pyrolysis reactor；
Carrier gas delivers part, and described carrier gas delivers part and is connected with described catalyst supervisor, and described carrier gas delivers part and is configured to fit
In the inside that catalyst is blown into described pyrolysis reactor；
Mixing component, described mixing component includes:
Rotatable shaft, described shaft is extend into the inside of described pyrolysis reactor by the outlet of described semicoke；Multiple stir
Mixing bar, described puddler is connected on described shaft along the length of described shaft, and described puddler is positioned at described storage
The interlayer of hot type radial canal.
Pyrolysis reactor the most according to claim 1, it is characterised in that described catalyst arm is multiple, and along institute
The length direction stating catalyst supervisor is arranged parallel to each other, and optionally, described catalyst arm is perpendicular to described catalyst supervisor,
Optionally, described catalyst arm extends to the whole slice width degree of described heat accumulation type radiant tube layer.
Pyrolysis reactor the most according to claim 1 and 2, it is characterised in that described catalyst arm is arranged on described storage
The interlayer of hot type radial canal, described catalyst ejector part is arranged in the interlayer of described heat accumulation type radiant tube.
4. according to the pyrolysis reactor described in any one of claim 1-3, it is characterised in that described catalyst ejector part includes urging
Agent jet pipe and the nozzle being arranged on described catalyst jet pipe, described nozzle is provided with regulation valve, optionally, described catalysis
Agent jet pipe is U-shaped, S type or W type jet pipe.
5. according to the pyrolysis reactor described in any one of claim 1-4, it is characterised in that described catalyst ejector part includes urging
Agent jet pipe, the tube wall of described catalyst jet pipe is provided with through hole, and optionally, described catalyst jet pipe is U-shaped, S type or W type
Jet pipe.
6. according to the pyrolysis reactor according to any one of claim 1-5, it is characterised in that described carrier gas delivers part and is connected to
The end of described catalyst supervisor, it is preferable that described carrier gas delivery part is detachably connected or is soldered to described catalyst supervisor.
7. according to the pyrolysis reactor described in any one of claim 1-6, it is characterised in that described puddler be perpendicular to described in stir
Mix axle, and along the length separation distribution of described shaft.
8. according to the pyrolysis reactor described in any one of claim 1-7, it is characterised in that described puddler is at described shaft
Same cross section on projection at an angle, it is preferable that the angle ranging from 0-90 degree, it is highly preferred that the angle ranging from 30
～90 degree.
9. according to the pyrolysis reactor according to any one of claim 1-8, it is characterised in that described puddler is positioned at described storage
Between hot type radiation tube layer and described catalyst arm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610708706.2A CN106281371A (en) | 2016-08-23 | 2016-08-23 | Pyrolysis reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610708706.2A CN106281371A (en) | 2016-08-23 | 2016-08-23 | Pyrolysis reactor |
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