CN105623684A - Pyrolysis reactor - Google Patents
Pyrolysis reactor Download PDFInfo
- Publication number
- CN105623684A CN105623684A CN201610137275.9A CN201610137275A CN105623684A CN 105623684 A CN105623684 A CN 105623684A CN 201610137275 A CN201610137275 A CN 201610137275A CN 105623684 A CN105623684 A CN 105623684A
- Authority
- CN
- China
- Prior art keywords
- oil gas
- pyrolysis
- pyrolysis reactor
- pipeline
- type radiant
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 147
- 238000009825 accumulation Methods 0.000 claims description 37
- 238000009795 derivation Methods 0.000 claims description 7
- 239000010813 municipal solid waste Substances 0.000 abstract description 26
- 238000000034 method Methods 0.000 abstract description 22
- 230000008901 benefit Effects 0.000 abstract description 7
- 238000010438 heat treatment Methods 0.000 abstract description 6
- 238000010517 secondary reaction Methods 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 5
- 239000007787 solid Substances 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 105
- 239000011269 tar Substances 0.000 description 24
- 239000000463 material Substances 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 10
- 230000008569 process Effects 0.000 description 10
- 230000001988 toxicity Effects 0.000 description 9
- 231100000419 toxicity Toxicity 0.000 description 9
- 238000002309 gasification Methods 0.000 description 8
- 238000007599 discharging Methods 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 230000004888 barrier function Effects 0.000 description 6
- 239000003245 coal Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000003610 charcoal Substances 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 239000010791 domestic waste Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 150000003384 small molecules Chemical class 0.000 description 3
- 240000002853 Nelumbo nucifera Species 0.000 description 2
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 2
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 2
- 239000000567 combustion gas Substances 0.000 description 2
- 239000002361 compost Substances 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000011812 mixed powder Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 239000010970 precious metal Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 239000011285 coke tar Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- DNJIEGIFACGWOD-UHFFFAOYSA-N ethanethiol Chemical compound CCS DNJIEGIFACGWOD-UHFFFAOYSA-N 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 235000019353 potassium silicate Nutrition 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002296 pyrolytic carbon Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a pyrolysis reactor and a method for treating rubbish with the pyrolysis reactor. The pyrolysis reactor comprises a pyrolysis oil gas outlet, heat accumulating type radiant tubes, oil gas guiding-out pipelines and a gas collecting tube. The heat accumulating type radiant tubes are arranged in multiple layers in the height direction of the pyrolysis reactor, and each layer includes multiple heat accumulating type radiant tubes which are parallel to one another in the horizontal direction. The oil gas guiding-out pipelines are arranged in multiple layers in the height direction of the pyrolysis reactor, each layer includes multiple oil gas guiding-out pipelines which are parallel to one another in the horizontal direction, and the surfaces of the oil gas guiding-out pipelines are provided with through holes. The gas collecting tube is communicated with the oil gas guiding-out pipelines and the pyrolysis oil gas outlet. The pyrolysis reactor can effectively restrain a secondary reaction of oil gas and increase the tar yield; in addition, the heat accumulating type heat-carrier-free radiant tube heating technology is adopted, no gas or solid heat carrier is needed, and the heat value of pyrolysis gas is increased; meanwhile, the pyrolysis reactor has the advantages that few devices are used, operation is easy, and the fault rate is low.
Description
Technical field
The present invention relates to pyrolysis reactor.
Background technology
Along with the acceleration of China's modernization, domestic waste has become an important factor of restriction green city fast development. At present, treatment of urban garbage mode in countries in the world mainly comprises sanitary landfill, burning, compost, pyrolysis and comprehensive garbage disposal etc. And the relevant refuse classification of China, rubbish comprehensive utilization technique are delayed, the main processing ways of current rubbish is sanitary landfill is main, and the modes such as burning, compost are auxiliary. Further, along with the enhancing of scientific-technical progress and environmental consciousness, the destruction that " burning method " and " landfill method " brings to environment and threaten the healthy more and more recognized of the mankind to arrive. A kind of novel technology, to substitute " burning method " and " landfill method ", to reduce greenhouse gas emission and to eliminate two English pollution problems, is just urgently needed
Refuse pyrolysis process technology refer to by rubbish when anaerobic or heating when anoxic, make it to decompose. In pyrolytic process, its intermediate product trends towards two polarization changes: a kind of be cracked into the cracking process of small molecules from macromole, another kind be the polycondensation process that small molecules is polymerized to macromole. Along with the rising of pyrolysis temperature, refuse pyrolysis mainly experiences drying (room temperature��200 DEG C), destructive distillation (��500 DEG C) and gas and generates (��1200 DEG C) three phases. In the cryodrying stage, the water of constitution decomposes of the moisture of outer water contained in rubbish and capillary structure absorption first by heating evaporation, in next material. Along with the evaporation of moisture and the rising of pyrogenation and carbonization temperature, refuse pyrolysis enters the destructive distillation stage. As long as there is internal water and CO in the destructive distillation stage2Precipitation, deoxidation, the reaction such as desulfurization. Along with the continuation of temperature raises, the small-molecule substance generation second pyrolysis that the destructive distillation stage produces, refuse pyrolysis enters gas generation phase, generates second pyrolysis product. Secondary reaction mainly contains cracking, dehydrogenation, polycondensation, hydrogenation, bridged bond reaction, water carbon reaction etc. Second pyrolysis reaction primary product comprises: H2��CH4, CO etc.
Owing to China's Waste sorting method is imperfect, cause the composition of rubbish own abnormal complicated, normal containing thing, plastics, old and useless battery, circuit card etc. more than kitchen. Find that the tar ingredients that refuse pyrolysis produces is also abnormal complicated simultaneously, composition analysis finds in tar containing material in hundreds of, comprise various organic acid, phenols, ketone class, aldehyde class, PAHs etc., wherein chlorine element and heavy metal element are generally higher, water content about 20%, calorific value is 13��18MJ/Kg about, causes stench because of sulfide content height simultaneously, and comprehensive utilization difficulty is big. All multifactor cause China's refuse pyrolysis, rubbish comprehensive utilization technique be difficult to obtain important breakthrough.
Summary of the invention
The present invention is intended to one of technical problem at least solving existence in prior art. For this reason, it is an object of the present invention to propose a kind of pyrolysis reactor, this pyrolysis reactor can effectively suppress the secondary reaction of oil gas, improve tar yield, and have employed heat accumulating type without thermal barrier radiator tube heating technique, it is not necessary to gas, solid thermal barrier, improve the calorific value of pyrolysis gas, simultaneously to have taken into account equipment few for pyrolysis reactor, easily operates, the advantages such as failure rate is low.
According to an aspect of the present invention, the present invention provides a kind of pyrolysis reactor. According to embodiments of the invention, pyrolysis reactor comprises: pyrolysis oil gas vent; Heat accumulation type radiant tube, described heat accumulation type radiant tube is along the height direction multi-tier arrangement of described pyrolysis reactor, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction; Oil gas derives pipeline, and described oil gas derives the height direction multi-tier arrangement of pipeline along described pyrolysis reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline, and described oil gas is derived and is provided with through hole on the surface of pipeline; And effuser, described effuser is derived pipeline with described oil gas and is connected with described pyrolysis oil gas vent.
Pyrolysis reactor according to embodiments of the present invention, oil gas derives pipeline and the pyrolysis oil gas of generation can be derived pyrolysis reactor by effuser fast, thus reduce the residence time of pyrolysis oil gas, suppress the secondary reaction of pyrolysis oil gas, and have employed heat accumulating type without thermal barrier radiator tube heating technique, it is not necessary to gas, solid thermal barrier, improve the calorific value of pyrolysis gas, simultaneously to have taken into account equipment few for pyrolysis reactor, easily operates, the advantages such as failure rate is low.
In one embodiment of the invention, described pyrolysis reactor has reactor body, and described reacting body has opening for feed, discharge port and pyrolysis oil gas vent, limits reaction compartment in described reactor body.
In one embodiment of the invention, the both sides tube wall of described heat accumulation type radiant tube is respectively arranged with baffle plate, described baffle plate be positioned at described oil gas derive pipeline top, and cover described oil gas derive the whole of pipeline erect to projection.
In one embodiment of the invention, described baffle plate is starting point from the phase tangent line of the vertical tangent plane of the tube wall of described heat accumulation type radiant tube, extends downward the vertical tangent plane that described oil gas derives pipeline at an angle, the angle ranging from 40-90 degree, and not containing 90 degree.
In one embodiment of the invention, described oil gas derives 1/2-3 times that the distance of the tube wall between pipeline and contiguous described heat accumulation type radiant tube is described oil gas derivation pipe diameter d.
In one embodiment of the invention, described oil gas derives pipeline and described heat accumulation type radiant tube is arranged in parallel, and the left and right sides of described heat accumulation type radiant tube is symmetrically arranged with two oil gas derivation pipelines.
In one embodiment of the invention, the oil gas delivery line of same layer is connected to same pyrolysis oil gas vent.
In one embodiment of the invention, described heat accumulation type radiant tube is made up of heat accumulating type honeycomb and radiator tube.
Pyrolysis reactor according to embodiments of the present invention, at least has one of following advantage:
1) utilizing pyrolysis reactor to carry out pyrolysis, the pyrolysis gas calorific value height that pyrolysis produces, without gaseous heat-carrier dilution, follow-up pyrolysis gas condensation cold is few, and the equipment pipe volumes such as purification and dedusting are little.
2) heat accumulation type radiant tube adopts heat accumulating type honeycomb, will enter fuel and the preheating of air of combustion chamber, and reduce funnel temperature, thermo-efficiency height.
3) pyrolysis reactor can modular combination, be applicable to different garbage treatment quantity, be easy to industrialization promotion.
4) septate heat transfer technique is adopted, the component variation of rubbish is insensitive.
5) this pyrolysis reactor only needs rubbish to carry out simple pre-treatment.
The 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 the practice of the present invention.
Accompanying drawing explanation
Above-mentioned and/or the additional aspect of the present invention and advantage from accompanying drawing below combining to the description of embodiment becoming obviously and it should be readily understood that wherein:
Fig. 1 shows the structural representation of pyrolysis reactor according to an embodiment of the invention;
Fig. 2 shows the structural representation of heat accumulation type radiant tube, baffle plate and oil gas delivery line in pyrolysis reactor according to an embodiment of the invention;
Fig. 3 shows the structural representation of pyrolysis reactor according to an embodiment of the invention.
Embodiment
Being 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. It is exemplary below by the embodiment being described with reference to the drawings, only for explaining the present invention, and limitation of the present invention can not be 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 are closed is based on orientation shown in the drawings or position relation, be only the present invention for convenience of description instead of require the present invention must with specific orientation structure and operation, therefore can not be interpreted as limitation of the present invention.
It should be noted that, term " first ", " the 2nd " are only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technology feature. Thus, be limited with " first ", the feature of " the 2nd " can express or implicit comprise one or more these features. Further, in describing the invention, unless otherwise explanation, the implication of " multiple " is two or more.
According to an aspect of the present invention, the present invention provides a kind of pyrolysis reactor. With reference to figure 1, according to embodiments of the invention, this pyrolysis reactor is explained, this pyrolysis reactor comprises: pyrolysis oil gas vent 110, heat accumulation type radiant tube 200, oil gas derive pipeline 300 and effuser 400, wherein, heat accumulation type radiant tube 200 (herein also referred to as " radiator tube ") is along the height direction multi-tier arrangement of pyrolysis reactor, and every layer has many heat accumulation type radiant tubes 200 parallel to each other in the horizontal direction; Oil gas derives the height direction multi-tier arrangement of pipeline 300 along pyrolysis reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline, and oil gas is derived and is provided with through hole on the surface of pipeline; Effuser 400 is derived pipeline 300 with oil gas and is connected with pyrolysis oil gas vent 110.
With reference to figure 1, in some embodiments of the invention, this pyrolysis reactor can also be provided by following form, and this pyrolysis reactor comprises:
Reactor body 100, described reactor body has opening for feed, discharge port and pyrolysis oil gas vent, limits reaction compartment in described reactor body;
Multilayer heat accumulation type radiant tube 200, described multilayer heat accumulation type radiant tube is spaced apart along described reactor body height direction in described pyrolysis reaction region, every layer of described heat accumulation type radiant tube comprises multiple heat accumulation type radiant tube spaced apart in the horizontal direction, and described at least one in described multilayer heat accumulation type radiant tube, the bottom of heat accumulation type radiant tube is provided with at least one pyrolysis oil gas vent;
Oil gas derives pipeline 300, and described oil gas derives the height direction multi-tier arrangement of pipeline along described pyrolysis reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline, and oil gas described in every root is derived pipeline and is connected with described pyrolysis oil gas vent;
Effuser 400, described effuser is derived pipeline with described oil gas and is connected.
Thus, pyrolysis reactor according to embodiments of the present invention can effectively suppress the secondary reaction of oil gas, improve tar yield, and have employed heat accumulating type without thermal barrier radiator tube heating technique, without the need to gas, solid thermal barrier, it is to increase the calorific value of pyrolysis gas, to have taken into account equipment few for pyrolysis reactor simultaneously, easily operation, the advantages such as failure rate is low.
Furthermore, it may be desirable to utilize rubbish is carried out pyrolysis by this pyrolysis reactor, refuse pyrolysis temperature is low, pyrolysis efficiency height, and can realize two English zero releases.
In addition, this pyrolysis reactor can modular combination, be applicable to different garbage treatment quantity, be easy to industrial applications.
According to a particular embodiment of the invention, reactor body 100 comprises gas inlet 120, fuel gas inlet 130 and exhanst gas outlet 140 further.
According to a particular embodiment of the invention, every layer of radiator tube comprise multiple parallel and equally distributed radiator tubes and each radiator tube parallel with each radiator tube in adjacent upper and lower two layers of radiator tube and be in staggered distribution along reactor body height direction. Thus, it is possible to significantly improve the pyrolysis efficiency of material, so improve pyrolysis oil product rate.
According to a particular embodiment of the invention, oil gas derives the height direction multi-tier arrangement of pipeline 300 along pyrolysis reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline, and oil gas is derived and is provided with through hole on the surface of pipeline; Oil gas is derived pipeline 300 and is connected with effuser 400, and effuser 40 is connected with oil gas vent 12. Thus, arrange that oil gas is derived pipeline 30 and reduced the residence time of tar in burner hearth by end under radiator tube, avoid the second pyrolysis of tar, it is to increase tar yield. According to a particular embodiment of the invention, oil gas is derived pipeline 300 and is arranged in parallel with radiator tube 200, and the left and right sides of radiator tube 200 is symmetrically arranged with two oil gas derivation pipelines 300. Thus, by arranging that in the both sides of radiator tube oil gas is derived pipeline 30 and decreased the residence time of tar in burner hearth, the second pyrolysis of tar is avoided, it is to increase tar yield.
According to embodiments of the invention, oil gas delivery line 300 is symmetrical set the lower section at each heat accumulation type radiant tube 200. Thus, being convenient to oil gas derives, and decreases the residence time of tar in burner hearth, avoids the second pyrolysis of tar, it is to increase tar yield.
According to embodiments of the invention, oil gas delivery line 300 is not particularly limited with the mode of connection of pyrolysis oil gas vent 110, and according to a particular embodiment of the invention, the oil gas delivery line 300 of same layer is connected to same pyrolysis oil gas vent 110. Some specific embodiments according to the present invention, the oil gas delivery line 300 of adjacent two layers or more layer is connected to same pyrolysis oil gas vent 110. Thus, it is possible to collected by oil gas, Simplified flowsheet also improves tar yield, simultaneously can so that oil gas is derived.
With reference to figure 2, according to embodiments of the invention, the both sides tube wall of heat accumulation type radiant tube 200 being respectively arranged with baffle plate 800, this baffle plate 800 is positioned at the top that oil gas derives pipeline 300, and covering oil gas derivation the whole of pipeline 300 erect to projection. In other words, every root heat accumulation type radiant tube 200 is provided with baffle plate 800, oil gas delivery line 300 is arranged near heat accumulation type radiant tube 200, baffle plate 800 is made to cover the upper surface of oil gas delivery line 300, and baffle plate 800 extends to the outside upright edge of oil gas delivery line 300 from the point contacted with heat accumulation type radiant tube 200. Contriver finds, arranges baffle plate by deriving fast at every root oil gas above pipeline, not only prevents friction in material decline process from prolonging oil gas delivery line, and then extends the life-span of oil gas delivery line; And baffle plate also plays the drainage to material, prevent material to be stuck between radiator tube and oil gas derivation pipeline, cause feed blocking; In addition, baffle plate also avoids tar to spread, and then improves the efficiency deriving tar, it is to increase tar yield.
According to a particular embodiment of the invention, oil gas delivery line 300 is positioned at below heat accumulation type radiant tube 200 horizontal diameter space and is positioned at heat accumulation type radiant tube 200 both sides, and baffle plate 800 is tangent with oil gas delivery line 300. Thus, the drainage of baffle plate is better, it is possible to better avoid tar to spread, and the life-span of oil gas delivery line is longer, and tar yield is higher. According to a particular embodiment of the invention, as shown in Figure 2, baffle plate 800 is from the vertical tangent plane A (A of the tube wall of radiator tube 8001) phase tangent line be starting point, at an angle �� extend downward oil gas derive pipeline 300 vertical tangent plane B (B1), angle [alpha] is 40-90 degree, not containing 90 degree. Thus so that the shortest length of baffle plate can block oil gas to derive pipeline.
According to a particular embodiment of the invention, oil gas derives 1/2-3 times that the spacing of the tube wall of pipeline 300 and contiguous radiator tube 200 is oil gas derivation pipeline 300 caliber d. Thus, it is possible to by deriving the tar of generation at once, avoid coke tar cracking, it is to increase tar yield.
According to embodiments of the invention, effuser 400 comprises: gas-collecting branch pipe 410 and gas gathering manifold 420, and wherein, gas gathering manifold 420 is derived pipeline 300 by multiple gas-collecting branch pipe 410 and multilayer oil gas and is connected. Thus, the pyrolysis oil gas that pyrolysis produces is derived through effuser and gas gathering manifold, thus reduces the residence time of pyrolysis oil gas in pyrolysis oven, effectively suppresses the secondary reaction of oil gas, it is to increase tar yield.
According to embodiments of the invention, described heat accumulation type radiant tube is made up of heat accumulating type honeycomb and radiator tube. Thus, utilize heat accumulating type honeycomb will enter fuel and the preheating of air of combustion chamber, reduce funnel temperature, thermo-efficiency height.
Fig. 3 shows the pyrolysis reactor of one embodiment of the invention, and as shown in Figure 3, this pyrolysis reactor comprises further: spiral discharging device 700, and this spiral discharging device 700 is connected with discharge port. Thus, while discharging, material is carried out break process, is convenient to subsequent applications.
According to embodiments of the invention, this pyrolysis reactor comprises further: feed hopper 500 and feeding screw 600, and wherein, feed hopper 500 has lower discharge port; Feeding screw 600 has material inlet and material outlet, and material inlet is connected with lower discharge port, and material outlet is connected with opening for feed, for being entered in reaction compartment by feeder 600 by the material being stored in feed hopper 500.
Below with reference to specific embodiment, the present invention will be described, it is necessary to explanation, and these embodiments are only explanation property, and can not be interpreted as limitation of the present invention.
Embodiment 1:
Certain domestic waste composition analysis is as shown in table 1, and rubbish water content is 43%, utilizes pyrolysis reactor this life to be processed, and wherein, as shown in Figure 3, detailed process is as follows for the structural representation of pyrolysis reactor:
Table 1
Table 2
1, march into the arena rubbish pre-treatment, Large stone dregs, glass and the metal etc. contained in the rubbish after marching into the arena not easily pyrolysis or can not the material of pyrolysis reject in advance;
2, pyrolysis reactor is delivered to after the rubbish after rejecting not easily pyrolyzate directly being delivered to sanitary fill compression dehydration;
3, control enters the combustion gas of radiator tube and air proportioning and amount, and the temperature of control pyrolysis oven, ensures that pyrolysis room temp is about 680 DEG C;
4, control discharging spiral rotating speed bottom pyrolysis reactor so that rubbish mean residence time��1.5h, discharge pyrolysis oven by bottom discharging spiral;
5, with the ratio of ratio 36.76:52.33:10.91, refuse pyrolysis charcoal, Sichuan lotus coal, Wingdale being mixed powder process, obtained compound median size��300 ��m, wherein, the composition analysis of Sichuan lotus coal is as shown in table 2;
6, compound is sent into pyrolysis reactor gasification, and vaporized chemical adopts percolate and part air, gasification and melting furnace temperature 1300 DEG C;
7, in pyrolysis reactor, rubbish charcoal, coal and the reaction of vaporized chemical generating gasification, produce gasification gas and liquid glass body lime-ash, liquid lime-ash building sand after reclaiming precious metal;
8, the pyrolysis oil gas that pyrolysis reactor pyrolysis produces is after gas-oil separation, obtain high-quality pyrolytic tar, the pyrolysis gas of��75% enters pyrolysis reactor burning for pyrolysis offer fuel, and the pyrolysis gas of��25% and the gas that gasifies generate electricity through the laggard gas turbine combustion of mixing and rough purification.
Lime-ash is analyzed: the two non-1.3ng-TEQ/kg of English content in anxious sloppy heat slag, Pb leach toxicity value be 0.2013mg/L, Cr leach toxicity value be 0.387mg/L, Cd leach toxicity value be 0.147mg/L, all the other non-detections, meet about Extraction Toxicity Identification Standard of Hazardous Waste.
Embodiment 2:
Certain domestic waste composition analysis is as shown in table 3, and rubbish water content is 51%, utilizes pyrolysis reactor this life to be processed, and wherein, as shown in Figure 3, detailed process is as follows for the structural representation of pyrolysis reactor:
Table 3
Table 4
1, march into the arena rubbish pre-treatment, Large stone dregs, glass and the metal etc. contained in the rubbish after marching into the arena not easily pyrolysis or can not the material of pyrolysis reject in advance;
2, pyrolysis reactor is delivered to after the rubbish after rejecting not easily pyrolyzate directly being delivered to sanitary fill compression dehydration;
3, control enters the combustion gas of radiator tube and air proportioning and amount, and the temperature of control pyrolysis oven, ensures that the pyrolysis room temp of pyrolysis reactor is about 700 DEG C;
4, control discharging spiral rotating speed bottom pyrolysis reactor so that rubbish mean residence time��1h, discharge pyrolysis reactor by bottom discharging spiral;
5, with the ratio of ratio 47.3:42.1:10.6, pyrolytic carbon, Yangquan Shanxi hard coal, Wingdale being mixed powder process, obtained compound median size��400um, wherein, the composition analysis of Yangquan Shanxi hard coal is as shown in table 4;
6, compound is sent into pyrolysis reactor gasification, and vaporized chemical adopts percolate and part air, gasification and melting furnace temperature 1420 DEG C;
7, in pyrolysis reactor, rubbish charcoal and the reaction of coal generating gasification, produce gasification gas and liquid lime-ash, liquid lime-ash building sand after reclaiming precious metal;
8, the pyrolysis oil gas that pyrolysis reactor pyrolysis produces is after gas-oil separation, obtain high-quality pyrolytic tar, the pyrolysis gas of��80% enters pyrolysis reactor burning for pyrolysis offer fuel, and the pyrolysis gas of��20% and the gas that gasifies generate electricity through the laggard gas turbine combustion of mixing and rough purification.
Lime-ash is analyzed: the two non-1.1ng-TEQ/kg of English content in anxious sloppy heat slag, it is 0.2375mg/L that Pb leaches toxicity value, it is 0.409mg/L that Cr leaches toxicity value, it is 0.185mg/L that Cd leaches toxicity value, it is 0.024mg/L that Hg leaches toxicity value, all the other non-detections, meet about Extraction Toxicity Identification Standard of Hazardous Waste.
In the description of this specification sheets, at least one embodiment that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to be contained in the present invention in conjunction with concrete feature, structure, material or feature that this embodiment or example describe or example. In this manual, the schematic representation of above-mentioned term is not necessarily referred to identical embodiment or example. And, the concrete feature of description, structure, material or feature can combine in an appropriate manner in any one or more embodiment or example.
Although it has been shown and described that embodiments of the invention, it will be understood by those skilled in the art that: these embodiments can be carried out multiple change, amendment, replacement and modification when not departing from principle and the objective of the present invention, the scope of the present invention by claim and etc. jljl limit.
Claims (7)
1. a pyrolysis reactor, it is characterised in that, comprising:
Pyrolysis oil gas vent;
Heat accumulation type radiant tube, described heat accumulation type radiant tube is along the height direction multi-tier arrangement of described pyrolysis reactor, and every layer has many heat accumulation type radiant tubes parallel to each other in the horizontal direction;
Oil gas derives pipeline, and described oil gas derives the height direction multi-tier arrangement of pipeline along described pyrolysis reactor, and every layer has many oil gas parallel to each other in the horizontal direction and derives pipeline, and described oil gas is derived and is provided with through hole on the surface of pipeline; And
Effuser, described effuser is derived pipeline with described oil gas and is connected with described pyrolysis oil gas vent.
2. pyrolysis reactor according to claim 1, it is characterised in that, the both sides tube wall of described heat accumulation type radiant tube is respectively arranged with baffle plate, described baffle plate be positioned at described oil gas derive pipeline top, and cover described oil gas derive the whole of pipeline erect to projection.
3. pyrolysis reactor according to claim 1 and 2, it is characterized in that, described baffle plate is starting point from the phase tangent line of the vertical tangent plane of the tube wall of described heat accumulation type radiant tube, extend downward the vertical tangent plane that described oil gas derives pipeline at an angle, the angle ranging from 40-90 degree, and not containing 90 degree.
4. pyrolysis reactor according to any one of claim 1-3, it is characterised in that, described oil gas derives 1/2-3 times that the distance of the tube wall between pipeline and contiguous described heat accumulation type radiant tube be that described oil gas derives pipe diameter d.
5. pyrolysis reactor according to any one of claim 1-4, it is characterised in that, described oil gas is derived pipeline and is arranged in parallel with described heat accumulation type radiant tube, and the left and right sides of described heat accumulation type radiant tube is symmetrically arranged with two oil gas derivation pipelines.
6. pyrolysis reactor according to any one of claim 1-5, it is characterised in that, the oil gas of same layer is derived pipeline and is connected to same pyrolysis oil gas vent.
7. pyrolysis reactor according to any one of claim 1-6, it is characterised in that, described heat accumulation type radiant tube is made up of heat accumulating type honeycomb and radiator tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610137275.9A CN105623684B (en) | 2016-03-10 | 2016-03-10 | Pyrolysis reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610137275.9A CN105623684B (en) | 2016-03-10 | 2016-03-10 | Pyrolysis reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105623684A true CN105623684A (en) | 2016-06-01 |
| CN105623684B CN105623684B (en) | 2018-06-08 |
Family
ID=56039043
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610137275.9A Active CN105623684B (en) | 2016-03-10 | 2016-03-10 | Pyrolysis reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105623684B (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5831576B2 (en) * | 2013-03-22 | 2015-12-09 | Ｊｆｅスチール株式会社 | Coke production equipment |
| CN105176563A (en) * | 2015-09-25 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Rapid biomass pyrogenation system and method |
| CN205045974U (en) * | 2015-09-25 | 2016-02-24 | 北京神雾环境能源科技集团股份有限公司 | System for mud rapid pyrolysis |
| CN105482834A (en) * | 2016-01-27 | 2016-04-13 | 北京神雾环境能源科技集团股份有限公司 | Moving bed pyrolysis reactor |
| CN205501187U (en) * | 2016-03-10 | 2016-08-24 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis reactor |
-
2016
- 2016-03-10 CN CN201610137275.9A patent/CN105623684B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5831576B2 (en) * | 2013-03-22 | 2015-12-09 | Ｊｆｅスチール株式会社 | Coke production equipment |
| CN105176563A (en) * | 2015-09-25 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Rapid biomass pyrogenation system and method |
| CN205045974U (en) * | 2015-09-25 | 2016-02-24 | 北京神雾环境能源科技集团股份有限公司 | System for mud rapid pyrolysis |
| CN105482834A (en) * | 2016-01-27 | 2016-04-13 | 北京神雾环境能源科技集团股份有限公司 | Moving bed pyrolysis reactor |
| CN205501187U (en) * | 2016-03-10 | 2016-08-24 | 北京神雾环境能源科技集团股份有限公司 | Pyrolysis reactor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105623684B (en) | 2018-06-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104685033A (en) | Hybrid thermal process to separate and transform contaminated or uncontaminated hydrocarbon materials into useful products, uses of the process, manufacturing of the corresponding system and plant | |
| CN102503055A (en) | Treatment method and treatment apparatus of oily sludge | |
| CN106947509B (en) | A kind of system and method that plastics pyrolytic gasification prepares oil product | |
| CN106635079A (en) | Solid waste RDF treating method | |
| CN202576344U (en) | Equipment for extracting oil fuel from sandy oil sludge or/and organic waste | |
| EP3311969A1 (en) | Device for thermally decomposing polyethylene and polypropylene waste | |
| CN103666505A (en) | Equipment for reducing and transforming household garbage or organic waste into energy resources | |
| CN101402869B (en) | Liquefaction state dry distillation oil refining process for shale and produced shale oil thereof | |
| CN101602953A (en) | The purification system of straw quick thermal cracking products | |
| CN203781995U (en) | Sludge treatment system | |
| CN107674691A (en) | A kind of system and method for domestic garbage resource | |
| US9982197B2 (en) | Dry distillation reactor and method for raw material of hydrocarbon with solid heat carrier | |
| CN105694925B (en) | Organic waste pyrolysis system and its application | |
| CN105885884A (en) | Organic waste pyrolysis system and application thereof | |
| CN205635472U (en) | Organic garbage pyrolytic system | |
| CN205635475U (en) | Organic garbage pyrolytic system | |
| CN107513392A (en) | It is a kind of to handle house refuse and the system and method for sewage sludge | |
| CN102504850B (en) | Oil sand solid hot carrier low-temperature dry distillation process | |
| CN205635474U (en) | Organic garbage pyrolytic system | |
| CN205528591U (en) | A reaction unit for pyrolysis and carbonization that gives up admittedly organically | |
| CN205501187U (en) | Pyrolysis reactor | |
| EP3312223B1 (en) | Method for thermally decomposing polyethylene and polypropylene waste | |
| CN105157033B (en) | A kind of refuse pyrolysis processing system and method | |
| CN105754622A (en) | Organic garbage pyrolysis system and application thereof | |
| CN102776016A (en) | Organic waste cracking and fractionating device and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 102200 Beijing city Changping District Machi Town cow Road No. 18 Applicant after: Shenwu Technology Group Co.,Ltd. Address before: 102200 Beijing city Changping District Machi Town cow Road No. 18 Applicant before: BEIJING SHENWU ENVIRONMENT AND ENERGY TECHNOLOGY Co.,Ltd. |
|
| CB02 | Change of applicant information | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20190121 Granted publication date: 20180608 |
|
| PP01 | Preservation of patent right | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20220921 Granted publication date: 20180608 |
|
| PD01 | Discharge of preservation of patent | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20220921 Granted publication date: 20180608 |
|
| PP01 | Preservation of patent right |