CN105482833A - Pyrolysis reactor - Google Patents
Pyrolysis reactor Download PDFInfo
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- CN105482833A CN105482833A CN201610022364.9A CN201610022364A CN105482833A CN 105482833 A CN105482833 A CN 105482833A CN 201610022364 A CN201610022364 A CN 201610022364A CN 105482833 A CN105482833 A CN 105482833A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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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
- C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
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- 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
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a pyrolysis reactor which comprises a feed inlet, oil gas outlets and a carbocoal outlet, as well as heat accumulating type radiant tubes, a catalyst conveying assembly and a stirring assembly. According to the pyrolysis reactor, raw materials can be quickly pyrolyzed, and a catalyst can be uniformly injected into the pyrolysis reactor.
Description
Technical field
The present invention relates to pyrolysis reactor.
Background technology
Pyrolysis reactor is the reactor that chemical field is conventional.Pyrolysis reactor conventional at present mainly comprises three river side's stoves of China, the hot solid carrier devolatilization technique stove of large work Dalian University of Science & Engineering and multistage rotary kiln 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.The Particle size requirements of some destructive distillation type of furnaces to raw material is high, can only pyrolysis lumped coal, causes small particles material to make full use of, the not high and problem of bulk deposition contaminate environment of resource utilization; The oily yield of some type of furnaces is lower, and is heating carrier with gas, and cause condensate recovery system huge, pyrogenation and carbonization gas is rushed rare, and gas heating value is low, is difficult to the problems such as comprehensive utilization further; Some adopt the pyrolysis type of furnace of solid thermal carriers, then there is raw material and mix with thermal barrier, and thermal barrier reheats the operations such as back-mixing, and technique comparatively complexity, equipment is more, manufacturing cost and working cost high.In addition, all to produce for the purpose of a large amount of tar in existing industrial pyrolytic process, pyrolysis gas output is less, or pyrolysis gas by following cycle technique utilization of burning, What is more to the pyrolytic gas making of coal and liquefaction degree all inadequate.Thus, pyrolysis reactor is further improved.
Summary of the invention
The present invention is intended at least to solve one of technical problem existed in prior art.For this reason, one object of the present invention is to propose a kind of pyrolysis reactor that simultaneously can realize raw material fast pyrogenation and catalyzer evenly being sprayed in pyrolysis oven, this pyrolysis reactor utilizes catalyst transport assembly to pyrolysis inside reactor conveying catalyzer, and utilize mixing component catalyzer and raw material to be stirred in pyrolysis reactor, and then, fast pyrogenation and catalytic pyrolysis technology merge by this pyrolysis reactor mutually, the pyrolysis oil preparation that can realize small particles material is gentle, significantly improves the yield of pyrolysis gas and obtains a certain amount of pyrolysis oil.In addition, this pyrolysis reactor have employed heat accumulation type radiant tube heating technique, without the need to gas, solid thermal barrier heating, simplifies conversion unit while improve the thermo-efficiency of reactor.
Thus, according to an aspect of the present invention, the invention provides a kind of pyrolysis reactor.According to embodiments of the invention, this pyrolysis reactor comprises: opening for feed, oil gas vent, semicoke export, and wherein, described semicoke outlet is positioned at reactor bottom;
Heat accumulation type radiant tube, described heat accumulation type radiant tube is arranged along the short transverse multilayer of described pyrolysis reactor in described pyrolysis reactor inside, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction; Catalyst transport assembly, described catalyst transport assembly comprises: catalyst hooper; Catalyzer is responsible for, and it is outside that described catalyzer supervisor is arranged on described pyrolysis reactor vertically; Described catalyzer supervisor is connected with described catalyst hooper; Catalyzer arm, described catalyzer arm through described pyrolysis reactor sidewall and extend to the inside of described pyrolysis reactor, described catalyzer arm is responsible for described catalyzer and is connected; One or more catalyst ejector part, described catalyst ejector part is arranged on described catalyzer arm, and it is inner to be positioned at described pyrolysis reactor, part is sent in carrier gas, described carrier gas is sent part and is responsible for described catalyzer and is connected, and the inside that part is configured to be suitable for catalyzer being blown into described pyrolysis reactor is sent in described carrier gas; Mixing component, described mixing component comprises: rotatable stir shaft, and described stir shaft is exported the inside extending into described pyrolysis reactor by described semicoke; Multiple agitator arm, described agitator arm is connected on described stir shaft along the length of described stir shaft, and described agitator arm is positioned at the interlayer of described heat accumulation type radiant tube.
The present inventor devises a kind of pyrolysis reactor that simultaneously can realize raw material fast pyrogenation and catalyzer evenly being sprayed in pyrolysis oven for existing pyrolysis reactor, this pyrolysis reactor utilizes catalyst transport assembly to pyrolysis inside reactor conveying catalyzer, and utilize mixing component catalyzer and raw material to be stirred in pyrolysis reactor, effectively loosen material, the oil gas of generation is discharged as early as possible, reduce second pyrolysis, improve oily yield, add the mixing of powerful catalyst and coal charge, improve catalytic efficiency further.Thus, fast pyrogenation and catalytic pyrolysis technology merge by this pyrolysis reactor mutually, and the pyrolysis oil preparation that can realize small particles material is gentle, significantly improve the yield of pyrolysis gas and obtain a certain amount of pyrolysis oil.In addition, this pyrolysis reactor have employed heat accumulation type radiant tube heating technique, without the need to gas, solid thermal barrier heating, simplifies conversion unit, have important social benefit, economic benefit and environmental benefit while improve the thermo-efficiency of reactor.
Wherein, it should be noted that, in the present invention, " pyrolysis reactor " and " heat accumulating type descending-bed reactor " can exchange use.
In one embodiment of the invention, described pyrolysis reactor specific reactor body, described reacting body has opening for feed and discharge port, limits reaction compartment in described reactor body.
In one embodiment of the invention, catalyzer supervisor is arranged on the outside of described reactor body.
In one embodiment of the invention, described in described multiple catalyzer Zhi Jing, the sidewall of reactor body enters in described reaction compartment.
In one embodiment of the invention, described mixing component is arranged in described reaction compartment.
In one embodiment of the invention, described pyrolysis reactor comprises opening for feed, fuel gas inlet, gas inlet and pyrolysis oil gas vent, exhanst gas outlet, semicoke outlet, catalyst ejector part entrance and the outlet of catalyst ejector part.In one embodiment, opening for feed is arranged on the top of pyrolysis reactor.
In one embodiment of the invention, described stir shaft utilizes motor drive.
In one embodiment of the invention, described catalyzer arm is multiple, and the length direction be responsible for along described catalyzer is arranged parallel to each other.
In one embodiment of the invention, described catalyzer arm is responsible for perpendicular to described catalyzer.
In one embodiment of the invention, described catalyzer arm extends to the whole layer width of described heat accumulation type radiant tube layer.
In one embodiment of the invention, described catalyzer arm is arranged on the interlayer of described heat accumulation type radiant tube.In a preferred embodiment of the invention, described catalyzer 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 interlayer of described heat accumulation type radiant tube.
In one embodiment of the invention, described catalyst ejector part comprises catalyzer jet pipe and is arranged on the nozzle on described catalyzer jet pipe, and described nozzle is provided with variable valve.
In one embodiment of the invention, described catalyzer jet pipe is U-shaped, S type or W type jet pipe.
In one embodiment of the invention, described catalyst ejector part comprises catalyzer jet pipe, and the tube wall of described catalyzer jet pipe is provided with through hole.
In one embodiment of the invention, described catalyzer 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, the end that part is connected to described catalyzer supervisor is sent in described carrier gas, and preferably, described carrier gas is sent part and removably connected or be soldered to described catalyzer supervisor.
In one embodiment of the invention, the number of plies of described catalyzer arm is 10-25 layer, and every layer of described catalyzer arm has 4-15 catalyst ejector part.
In one embodiment of the invention, described catalyst ejector part is provided with between the described heat accumulation type radiant tube that any level is adjacent.
In one embodiment of the invention, described agitator arm perpendicular to described stir shaft, and distributes along the length separation of described stir shaft.
In one embodiment of the invention, the projection of described agitator arm on the same cross section of described stir shaft at an angle.At one preferably in embodiment of the present invention, the angle ranging from 0-90 degree.At one more preferably in embodiment of the present invention, the angle ranging from 30 ~ 90 degree.
In one embodiment of the invention, multiple described agitator arm distributes at the spaced apart lengths of described stir shaft.
In one embodiment of the invention, the round tube of described heat accumulation type radiant tube to be diameter be 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, and vertical spacing is 200-700mm.
In one embodiment of the invention, the number of plies of described multilayer heat accumulation type radiant tube is 10-25 layer.
Additional aspect of the present invention and advantage will part provide in the following description, and part will become obvious from the following description, or be recognized by practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or additional aspect of the present invention and advantage will become obvious and easy understand from accompanying drawing below combining to the description of embodiment, wherein:
Fig. 1 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;
Fig. 4 shows the vertical view of the mixing component in pyrolysis reactor according to an embodiment of the invention.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Being exemplary below by the embodiment be described with reference to the drawings, only for explaining the present invention, and can not limitation of the present invention being interpreted as.
In describing the invention, term " longitudinal direction ", " transverse direction ", " on ", D score, "front", "rear", "left", "right", " vertically ", " 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 the present invention for convenience of description instead of require that the present invention with specific azimuth configuration and operation, therefore must can not be interpreted as limitation of the present invention.
It should be noted that, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.Further, in describing the invention, except as otherwise noted, the implication of " multiple " is two or more.
According to an aspect of the present invention, the invention provides a kind of pyrolysis reactor.
The present inventor is surprised to find, pyrolysis reactor in embodiments of the invention can realize raw material fast pyrogenation and catalyzer evenly to spray in pyrolysis oven simultaneously, utilize catalyst transport assembly to pyrolysis inside reactor conveying catalyzer, and utilize mixing component catalyzer and raw material to be stirred in pyrolysis reactor, effectively loosen material, the oil gas of generation is discharged as early as possible, reduce second pyrolysis, improve oily yield, add the mixing of powerful catalyst and coal charge, improve catalytic efficiency further.Thus, fast pyrogenation and catalytic pyrolysis technology merge by this pyrolysis reactor mutually, and the pyrolysis oil preparation that can realize small particles material is gentle, significantly improve the yield of pyrolysis gas and obtain a certain amount of pyrolysis oil.
In addition, this pyrolysis reactor also has other advantage.Such as, this pyrolysis reactor have employed heat accumulation type radiant tube heating technique, without the need to gas, solid thermal barrier heating, simplifies conversion unit, have important social benefit, economic benefit and environmental benefit while improve the thermo-efficiency of reactor.
In addition, heat accumulation type radiant tube down-flow fluidized bed using ECT technique taked by the pyrolysis reactor of the embodiment of the present invention, and reactive system structure is simple, and easy to operate, uniformity of temperature profile, heats is good.
In addition, the pyrolysis reactor of the embodiment of the present invention can process the fine coal of below 2mm, and raw material availability is high, is suitable for promoting.
In addition, compared with traditional aluminium rice steamer method carbonization gas productive rate, the pyrolysis reactor of the embodiment of the present invention adopts catalyzer to carry out catalysis fast pyrogenation to coal, the gas production rate of the highest carbonization gas improve 50%.
In addition, the pyrolysis reactor of the embodiment of the present invention adopts heat accumulation type radiant tube to carry out pyrolysis, can not only improve the thermo-efficiency of system, and can ensure the homogeneity in temperature field.The combustion system that heat accumulation type radiant tube regularly commutates, makes the surface temperature difference of single heat accumulation type radiant tube only have about 30 DEG C, does not have district of localized hyperthermia.
In addition, the pyrolysis reactor of the embodiment of the present invention adopts heat accumulation type radiant tube combustion heat supplying technology, and surface temperature difference is little, and funnel temperature is low, and thermo-efficiency is high.
Fig. 1 shows the pyrolysis reactor of another embodiment of the present invention.As shown in Figure 1, pyrolysis reactor comprises: reactor body 100, multilayer heat accumulation type radiant tube 200, catalyst transport assembly 300 and mixing component 400.
Wherein, reacting body 100 has opening for feed and discharge port, limits reaction compartment 110 in this reactor body.
Multilayer heat accumulation type radiant tube 200 is spaced apart along reactor body 100 short transverse in described reaction compartment, and every layer of heat accumulation type radiant tube comprises multiple heat accumulation type radiant tube spaced apart in the horizontal direction, heat accumulation type radiant tube has pyrolysis oil gas vent, and multilayer heat accumulation type radiant tube 200 is for carrying out pyrolysis to reaction raw materials.
Catalyst transport assembly 300 comprises: part (not shown) is sent in catalyst hooper 340, catalyzer supervisor 310, multiple catalyzer arm 320, many catalyst ejector parts 330 and carrier gas, wherein, catalyst hooper 340 is for depositing catalyzer, catalyzer supervisor 310 has catalyst feeds and multiple first catalyst outlet, catalyzer supervisor is arranged on the outside of described reactor body, and catalyzer supervisor 310 is connected with catalyst hooper 340; Multiple catalyzer arm 320 is with multiple first catalyst outlet one_to_one corresponding and be communicated with, and entering in described reaction compartment through the sidewall of described reactor body, each catalyzer arm 320 is all set in parallel in the space between two-layer heat accumulation type radiant tube adjacent in horizontal direction in described multilayer heat accumulation type radiant tube 200; Many catalyst ejector parts, described many catalyst ejector parts are arranged on described multiple catalyzer arm, and are positioned at reaction compartment, and each catalyst ejector part all has nozzle; Part is sent in carrier gas, and described carrier gas is sent part and is responsible for described catalyzer and is connected, and the inside that part is configured to be suitable for catalyzer being blown into described pyrolysis reactor is sent in described carrier gas.Utilize catalyst transport assembly by catalyst transport to reaction compartment, arrange many catalyst ejector parts at catalyzer arm, make to be furnished with catalyst ejector part around every root heat accumulation type radiant tube, catalyzer is sprayed in coal charge layer equably by catalyst ejector part.
Mixing component 400 is arranged in reaction compartment, this mixing component 400 comprises: rotatable stir shaft 410 and multiple agitator arm 420, wherein, described stir shaft is exported the inside extending into described pyrolysis reactor by described semicoke, multiple agitator arm 420 is interspersed on described stir shaft, and each agitator arm is all arranged in the space between two-layer heat accumulation type radiant tube adjacent in horizontal direction in described multilayer heat accumulation type radiant tube.Utilize whipping appts effectively to loosen material, catalyzer and coal charge are mixed more uniformly, improve catalytic efficiency, the oil gas of generation can be made to discharge as early as possible simultaneously, reduce second pyrolysis, improve oily yield.
In one embodiment of the invention, motor drive stir shaft 410 is utilized to rotate.
In one embodiment of the invention, described catalyzer arm 320 is multiple, and the length direction be responsible for along described catalyzer is arranged parallel to each other.Thus, the material to different positions in reaction compartment sprays catalyzer.
In one embodiment of the invention, described catalyzer arm 320 is perpendicular to described catalyzer supervisor 310.
In one embodiment of the invention, described catalyzer arm 320 extends to the whole layer width of described heat accumulation type radiant tube layer.Namely catalyzer arm 320 arrives the tail end of heat accumulation type radiant tube layer through heat accumulation type radiant tube layer.Thus, make catalyzer spray in reaction compartment material everywhere, ensure catalyzer and the full and uniform mixing of material.
In one embodiment of the invention, the number of plies of described catalyzer arm is 10-25 layer, and every layer of described catalyzer arm has 4-15 catalyst ejector part.This kind of structural arrangement can make uniform distribution of temperature field in pyrolysis reaction region, thus can significantly improve the pyrolysis efficiency of material, and then improves the yield of pyrolysis oil.
In one embodiment of the invention, described catalyst ejector part is provided with between the described heat accumulation type radiant tube that any level is adjacent.Thus, ensure that catalyzer is ejected in material equably.
In one embodiment of the invention, the nozzle 332 that described catalyst ejector part 330 comprises catalyzer jet pipe 331 and is arranged on described catalyzer jet pipe, described nozzle is provided with variable valve.Thus, utilize variable valve to regulate the straying quatity of catalyzer, ensure that catalyzed reaction efficient the 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 figure 3, in one embodiment of the invention, catalyst ejector pipe 330 can be made up of multiple spaced apart in the horizontal direction and connected successively from beginning to end multiple muonic catalysis agent jet pipes 333, and the tube wall of each muonic catalysis agent jet pipe has multiple catalyzer spray orifice 332.Thus, adopt the catalyzer coil pipe of special shape, the catalyzer come by catalyzer arm is carried by rare gas element and sprays in pyrolysis reactor in catalyzer jet pipe.Can catalyzer be evenly distributed in pyrolysis reactor, with raw material Homogeneous phase mixing, and then catalyse pyrolysis reaction, improve pyrolysis efficiency.
In one embodiment of the invention, described catalyst ejector part comprises catalyzer jet pipe, and the tube wall of described catalyzer jet pipe is provided with through hole.
In one embodiment of the invention, one end of catalyzer arm is removably connected to catalyzer supervisor and is above also communicated with it, one end of catalyzer jet pipe is communicated with the other end of catalyzer arm, the other end of catalyzer jet pipe is fixed on furnace wall, thus, catalyzer jet pipe is across pyrolysis reactor inside on the width of reactor.The bottom of catalyzer supervisor is communicated with gas reservoir.Rare gas element is blown into catalyzer supervisor by gas reservoir, thus catalyzer is blown into catalyzer jet pipe.Rare gas element can be nitrogen etc.Catalyzer jet pipe can be U-shaped, S type or W type, needs to explain, being U-shaped when group catalyzer jet pipe number is 2, is S type when group catalyzer jet pipe number is 3.
In one embodiment of the invention, described catalyzer arm 320 is arranged on the interlayer of described heat accumulation type radiant tube 200, and described catalyst ejector part 330 is arranged in the interlayer of described heat accumulation type radiant tube 200.
Catalyzer arm is arranged at radiator tube interlayer effectively can prevent powder-material blocking catalyst jet pipe, can ensure that material can mix with catalyzer uniform contact after radiator tube is uniform simultaneously, ensure good reaction effect, can prevent catalyzer arm from wearing and tearing simultaneously, extend its work-ing life, reduce and change number of times.According to concrete example of the present invention, the number of muonic catalysis agent jet pipe can be determined according to the radiator tube number in every layer of heat accumulation type radiant tube, and then can make to be furnished with catalyzer jet pipe around every root heat accumulation type radiant tube, and then raising catalyzer adds uniformity coefficient, and reaction degree of being heated evenly.The catalyzer of particle diameter≤0.5mm is sprayed in coal charge layer equably by catalyzer jet pipe.Catalyzer jet pipe adopts the round tube of DN30-80, and catalyzer is blown in the catalyzer jet pipe of every layer through catalyzer arm by catalyzer supervisor.
In one embodiment of the invention, described agitator arm 420 is between described heat accumulation type radiant tube layer 200 and described catalyzer arm 320.Effectively can loosen inside reactor material thus, thus improve the derivation rate of pyrolysis oil gas further, avoid coking on heat accumulation type radiant tube, guarantee equipment normally runs simultaneously.
In one embodiment of the invention, described agitator arm 420 perpendicular to described stir shaft 410, and distributes along the length separation of described stir shaft 410.Thus, agitator arm can be made effectively to loosen inside reactor material, thus the derivation rate of pyrolysis oil gas can be significantly improved.
According to another specific embodiment of the present invention, as shown in Figure 4, on the shaft section of stir shaft 410, the circumference being projected in stir shaft 410 of multiple agitator arm 420 is evenly spaced apart distribution, according to concrete example of the present invention, on the shaft section of stir shaft 410, in the projection of multiple agitator arm 420, angle theta between two adjacent agitator arms 420 can be 0 ~ 90 degree, preferably 30 ~ 90 degree.Thus, agitator arm can be made effectively to loosen inside reactor material, thus improve the derivation rate of pyrolysis oil gas further.According to concrete example of the present invention, the angle between every layer of agitator arm 420 can be 180 degree, also can be to distribute between 0-90 degree.The length of stir shaft 410 can be 1-18m, and detachable agitator arm vertical spacing can be 0.4-1m, and the number of plies can be 11-26 layer.
According to embodiments of the invention, heat accumulation type radiant tube can be unidirectional regenerative gas radiator tube, and the heat namely produced by combustion gas by radiator tube body carries out heat supply in the mode of radiation.According to a particular embodiment of the invention, heat accumulation type radiant tube can be provided with gas control valve (not shown).Thus, the flow passing into the combustion gas of heat accumulation type radiant tube can be regulated to wait the accurate temperature controlling realized pyrolytic process by adjustment gas control valve, thus the pyrolysis efficiency of material can be significantly improved, and then improve the yield of pyrolysis oil.
Concrete, the accurate temperature controlling of the realizations such as the flow of the combustion gas of heat accumulation type radiant tube to pyrolytic process can be passed into by adjustment, and heat accumulation type radiant tube adopts the combustion system of regularly commutation, the temperature field of single radiator tube is made to be more or less the same in 30 DEG C, and there is no partial insulation district, thus the homogeneity in temperature field in guarantee reactor body, make the temperature in reaction compartment control in the scope of 450-750 degree Celsius.
Wherein, the model of radiator tube and adjacent can according to the volume of reaction compartment, the kinds of reaction mass etc. adjust.In specific embodiment of the invention scheme, the round tube of heat accumulation type radiant tube to be diameter be 200-300 millimeter.In specific embodiment of the invention scheme, the level interval between the heat accumulation type radiant tube of arbitrary neighborhood is 200-500mm, and vertical spacing is 200-700mm.Thus, pyrolysis is effective.
The number of plies of multilayer heat accumulation type radiant tube also can according to the volume of reaction compartment, and the kind of reaction mass etc. adjust.According to some embodiments of the present invention, the number of plies of multilayer heat accumulation type radiant tube is 10-25 layer, ensures that the distribution density of heat accumulation type radiant tube in reaction compartment is suitable, fully meets the needs of pyrolytic reaction.
The volume of reactor body can adjust according to the treatment capacity of pyrolysis reactor.According to some embodiments of the present invention, the width of reactor body is 2-6m, is highly 3-20m.
Fig. 2 shows the pyrolysis reactor of embodiments of the invention.As shown in Figure 2, this pyrolysis reactor comprises further: spiral discharging device 700, and described spiral discharging device 700 is connected with described discharge port.
As shown in Figure 2, this pyrolysis reactor comprises further: hopper 500 and feeding screw 600, described feeding screw 600 is connected with described opening for feed with described hopper 500, is given in reactor body by the question response thing in hopper through feeding screw fragmentation processing rear feeding confession.
Below with reference to specific embodiment, the present invention will be described, it should be noted that, these embodiments are only illustrative, and can not be interpreted as limitation of the present invention.
Embodiment 1
Table 1 shows the basic data of raw material From Shenmu Coal.Table 2 shows process operation parameter when utilizing the pyrolysis reactor shown in Fig. 2 to process From Shenmu Coal.
Table 1: From Shenmu Coal basic data
Table 2: process operation parameter
| Sequence number | Parameter name | Parameter value | Sequence number | Parameter name | Parameter value |
| 1 | Top radiator tube wall surface temperature | 625℃ | Reactor lower part temperature | 545℃ | |
| 2 | Middle part radiator tube wall surface temperature | 625℃ | Reactor outlet temperature | 506℃ | |
| 3 | Lower radiant tube wall surface temperature | 580℃ | Whirlwind temperature out | 485℃ | |
| 4 | Reactor upper temp | 505℃ | Reactor pressure | 1.7Kpa | |
| 5 | Reactor middle portion temperature | 540℃ |
From Shenmu Coal (3 tons/hour) is crushed to the granule materials of granularity≤2mm, enters in heat accumulating type descending-bed reactor in hopper through feeding screw.In heat accumulating type descending-bed reactor, be evenly arranged unidirectional heat accumulation type radiant tube, pipe surface temperature utilizes gas control valve to control 450 ~ 750 DEG C of scopes, and concrete technology parameter is in table 2.
Around every root radiator tube, be furnished with catalyzer arm, the catalyzer of particle diameter≤0.5mm is entered by catalyst ejector part and is sprayed on equably in coal charge layer by catalyzer arm.Be provided with whipping appts in pyrolysis reactor, effectively can loosen material, the oil gas of generation is discharged as early as possible, reduce second pyrolysis, improve oily yield, and catalyzer and coal charge can be made to mix more uniformly, improve catalytic efficiency further.The coal charge of Homogeneous phase mixing catalyzer stops 10 minutes from top to bottom in heat accumulating type descending-bed reactor, is rapidly heated to 500 ~ 600 DEG C, completes retort process.
With this reactor, From Shenmu Coal is processed, factor of created gase is 13.15%, up to 150% of aluminium rice steamer factor of created gase, pyrolysis gas output significantly improves, and owing to decreasing the second pyrolysis of tar, oil yield rate reaches 10.18%, up to 115% of aluminium rice steamer oil yield rate, hydrocarbon yield significantly improves, good in economic efficiency.
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, identical embodiment or example are not necessarily referred to the schematic representation of above-mentioned term.And the specific features of description, structure, material or feature can combine in an appropriate manner in any one or more embodiment or example.
Although illustrate and describe embodiments of the invention, those having ordinary skill in the art will appreciate that: can carry out multiple change, amendment, replacement and modification to these embodiments when not departing from principle of the present invention and aim, scope of the present invention is by claim and equivalents thereof.
Claims (9)
1. a pyrolysis reactor, is characterized in that, comprising:
Opening for feed, oil gas vent, semicoke export, and wherein, described semicoke outlet is positioned at reactor bottom;
Heat accumulation type radiant tube, described heat accumulation type radiant tube is arranged along the short transverse multilayer of described pyrolysis reactor in described pyrolysis reactor inside, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Catalyst transport assembly, described catalyst transport assembly comprises:
Catalyst hooper;
Catalyzer is responsible for, and it is outside that described catalyzer supervisor is arranged on described pyrolysis reactor vertically, and described catalyzer supervisor is connected with described catalyst hooper;
Catalyzer arm, described catalyzer arm through described pyrolysis reactor sidewall and extend to the inside of described pyrolysis reactor, described catalyzer arm is responsible for described catalyzer and is connected;
One or more catalyst ejector part, described catalyst ejector part is arranged on described catalyzer arm, and it is inner to be positioned at described pyrolysis reactor;
Part is sent in carrier gas, and described carrier gas is sent part and is responsible for described catalyzer and is connected, and the inside that part is configured to be suitable for catalyzer being blown into described pyrolysis reactor is sent in described carrier gas;
Mixing component, described mixing component comprises:
Rotatable stir shaft, described stir shaft is exported the inside extending into described pyrolysis reactor by described semicoke;
Multiple agitator arm, described agitator arm is connected on described stir shaft along the length of described stir shaft, and described agitator arm is positioned at the interlayer of described heat accumulation type radiant tube.
2. pyrolysis reactor according to claim 1, is characterized in that, described catalyzer arm is multiple, and the length direction be responsible for along described catalyzer is arranged parallel to each other,
Optionally, described catalyzer arm is responsible for perpendicular to described catalyzer,
Optionally, described catalyzer arm extends to the whole layer width of described heat accumulation type radiant tube layer.
3. pyrolysis reactor according to claim 1 and 2, is characterized in that, described catalyzer 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.
4. the pyrolysis reactor according to any one of claim 1-3, it is characterized in that, described catalyst ejector part comprises catalyzer jet pipe and is arranged on the nozzle on described catalyzer jet pipe, and described nozzle is provided with variable valve, optionally, described catalyzer jet pipe is U-shaped, S type or W type jet pipe.
5. the pyrolysis reactor according to any one of claim 1-4, is characterized in that, described catalyst ejector part comprises catalyzer jet pipe, and the tube wall of described catalyzer jet pipe is provided with through hole, and optionally, described catalyzer jet pipe is U-shaped, S type or W type jet pipe.
6. the pyrolysis reactor according to any one of claim 1-5, is characterized in that, the end that part is connected to described catalyzer supervisor is sent in described carrier gas, and preferably, described carrier gas is sent part and removably connected or be soldered to described catalyzer supervisor.
7. the pyrolysis reactor according to any one of claim 1-6, is characterized in that, described agitator arm perpendicular to described stir shaft, and distributes along the length separation of described stir shaft.
8. the pyrolysis reactor according to any one of claim 1-7, is characterized in that, the projection of described agitator arm on the same cross section of described stir shaft at an angle, preferably, the angle ranging from 0-90 degree, more preferably, the angle ranging from 30 ~ 90 degree.
9. the pyrolysis reactor according to any one of claim 1-8, is characterized in that, described agitator arm is between described heat accumulation type radiant tube layer and described catalyzer arm.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106281371A (en) * | 2016-08-23 | 2017-01-04 | 郭继安 | Pyrolysis reactor |
| CN118437740A (en) * | 2024-05-11 | 2024-08-06 | 北京华能长江环保科技研究院有限公司 | Pyrolysis device for photovoltaic modules |
| WO2024198217A1 (en) * | 2023-03-28 | 2024-10-03 | 常州大学 | Pyrolysis mechanism and biomass pyrolysis device |
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| CN104059681A (en) * | 2014-06-24 | 2014-09-24 | 北京神雾环境能源科技集团股份有限公司 | Regenerative type combustion gas radiant tube revolving bed oil shale dry distillation method and shale slag utilization technology |
| CN205528590U (en) * | 2016-01-13 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis reactor |
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| CN104059681A (en) * | 2014-06-24 | 2014-09-24 | 北京神雾环境能源科技集团股份有限公司 | Regenerative type combustion gas radiant tube revolving bed oil shale dry distillation method and shale slag utilization technology |
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| CN106281371A (en) * | 2016-08-23 | 2017-01-04 | 郭继安 | Pyrolysis reactor |
| WO2024198217A1 (en) * | 2023-03-28 | 2024-10-03 | 常州大学 | Pyrolysis mechanism and biomass pyrolysis device |
| CN118437740A (en) * | 2024-05-11 | 2024-08-06 | 北京华能长江环保科技研究院有限公司 | Pyrolysis device for photovoltaic modules |
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