CN105623684B - Pyrolysis reactor - Google Patents
Pyrolysis reactor Download PDFInfo
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- CN105623684B CN105623684B CN201610137275.9A CN201610137275A CN105623684B CN 105623684 B CN105623684 B CN 105623684B CN 201610137275 A CN201610137275 A CN 201610137275A CN 105623684 B CN105623684 B CN 105623684B
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- oil gas
- pyrolysis
- pyrolysis reactor
- radiant tube
- gas
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 125
- 238000009825 accumulation Methods 0.000 claims abstract description 35
- 239000000919 ceramic Substances 0.000 claims description 5
- 239000010813 municipal solid waste Substances 0.000 abstract description 30
- 238000000034 method Methods 0.000 abstract description 21
- 230000008901 benefit Effects 0.000 abstract description 7
- 230000004044 response Effects 0.000 abstract description 5
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000007787 solid Substances 0.000 abstract description 4
- 238000012545 processing Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 117
- 239000011269 tar Substances 0.000 description 23
- 239000000463 material Substances 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 13
- 238000002309 gasification Methods 0.000 description 10
- 238000002386 leaching Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 238000004458 analytical method Methods 0.000 description 6
- 239000000470 constituent Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000003610 charcoal Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000010791 domestic waste Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 150000003384 small molecules Chemical group 0.000 description 3
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 2
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 2
- 240000002853 Nelumbo nucifera Species 0.000 description 2
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 2
- 239000000149 chemical water pollutant Substances 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
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 239000002920 hazardous waste Substances 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
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- 229910052751 metal Inorganic materials 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000002510 pyrogen Substances 0.000 description 2
- 230000005855 radiation 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
- 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
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 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
- 238000003776 cleavage reaction Methods 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
- 230000007423 decrease Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 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
- 238000000605 extraction Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000010806 kitchen waste Substances 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 235000019353 potassium silicate Nutrition 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
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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
Abstract
Method the invention discloses pyrolysis reactor and using pyrolysis reactor processing rubbish.Pyrolysis reactor includes：It is pyrolyzed oil gas vent；Heat accumulation type radiant tube, short transverse multi-tier arrangement of the heat accumulation type radiant tube along the pyrolysis reactor, every layer has more heat accumulation type radiant tubes parallel to each other in the horizontal direction；Oil gas exports pipeline, and short transverse multi-tier arrangement of the oil gas export pipeline along the pyrolysis reactor, every layer has more oil gas export pipelines parallel to each other in the horizontal direction, and through-hole is provided on the surface of the oil gas export pipeline；And gas collecting tube, the gas collecting tube exports pipeline with the oil gas and the pyrolysis oil gas vent is connected.The pyrolysis reactor can effectively inhibit the secondary response of oil gas, improve tar yield, and employ heat accumulating type without heat carrier radiant tube heating technique, without gas, solid heat carrier, the calorific value of pyrolysis gas is improved, while to have taken into account equipment few for pyrolysis reactor, it is easy to operate, the advantages such as failure rate is low.
Description
Technical field
The present invention relates to pyrolysis reactors.
Background technology
With the acceleration of China's modernization, domestic waste, which has become, restricts the one of green city's fast development
A key factor.At present, treatment of urban garbage mode in countries in the world mainly includes sanitary landfills, burning, compost, pyrolysis and rubbish
Rubbish integrated treatment etc..And the relevant garbage classification in China, rubbish comprehensive utilization technique lag, at present main processing ways of rubbish
Based on sanitary landfills, supplemented by the modes such as burning, compost.Also, with scientific and technological progress and the enhancing of environmental consciousness, " burning method "
The destruction and the health of the mankind is threatened increasingly to be recognized that " landfill method " is brought to environment.It is a kind of new
The technology of type is to substitute " burning method " and " landfill method ", to reduce greenhouse gas emission and eliminate bioxin pollution problem, just quilt
There is an urgent need to
Refuse pyrolysis treatment technology refer to by rubbish anaerobic or anoxic in the state of heat, be allowed to decompose.It is being pyrolyzed
In the process, in-between product is intended to the variation that polarises：A kind of is from cracking process, the another kind that macromolecular cleavage is small molecule
It is the polycondensation process that small molecule is polymerized to macromolecular.With the raising of pyrolysis temperature, refuse pyrolysis mainly undergo it is dry (room temperature~
200 DEG C), destructive distillation (~500 DEG C) and gas generation (~1200 DEG C) three phases.In the low temperature drying stage, contained by rubbish
Outer water and the moisture of capillary structure absorption are initially heated evaporation, and secondly the constitution water in substance is thermally decomposed.With moisture
Evaporation and the raising of pyrogenation and carbonization temperature, refuse pyrolysis enter the destructive distillation stage.As long as internal water and CO occur for the destructive distillation stage2Analysis
Go out, deoxidation, the reactions such as desulfurization.Continue to increase with temperature, second pyrolysis, rubbish occur for the small-molecule substance that the destructive distillation stage generates
Rubbish pyrolysis enters gas generation phase, generates second pyrolysis product.Secondary response mainly has cracking, dehydrogenation, polycondensation, hydrogenation instead
Should, bridged bond reaction, water carbon reaction etc..Second pyrolysis reaction primary product includes：H2、CH4, CO etc..
Since China's Waste sorting method is not perfect, cause rubbish ingredient complex itself, often containing kitchen waste material, modeling
Material, old and useless battery, circuit board etc..The tar ingredients also complex that refuse pyrolysis generates is found simultaneously, and constituent analysis is found
Containing substance in hundreds of in tar, including various organic acids, phenols, ketone, aldehydes, PAHs etc., wherein chlorine element and a huge sum of money
It is generally higher to belong to element, water content about 20%, calorific value about 13~18MJ/Kg, while lead to stench due to sulfide content height,
It is big to comprehensively utilize difficulty.Factors cause China's refuse pyrolysis, rubbish comprehensive utilization technique to be difficult to obtain important breakthrough.
Invention content
The present invention is directed at least solve one of technical problem in the prior art.For this purpose, one object of the present invention
It is to propose a kind of pyrolysis reactor, which can effectively inhibit the secondary response of oil gas, improve tar yield, and
Heat accumulating type is employed without heat carrier radiant tube heating technique, without gas, solid heat carrier, improves the calorific value of pyrolysis gas, while heat
The advantages such as it is few that solution reactor has taken into account equipment, easy to operate, and failure rate is low.
According to an aspect of the present invention, the present invention provides a kind of pyrolysis reactors.According to an embodiment of the invention, it is hot
Solution reactor includes：It is pyrolyzed oil gas vent；Heat accumulation type radiant tube, height of the heat accumulation type radiant tube along the pyrolysis reactor
Direction multi-tier arrangement, every layer has more heat accumulation type radiant tubes parallel to each other in the horizontal direction；Oil gas exports pipeline, described
Oil gas exports short transverse multi-tier arrangement of the pipeline along the pyrolysis reactor, and every layer has more and puts down each other in the horizontal direction
Capable oil gas export pipeline, the oil gas export and are provided with through-hole on the surface of pipeline；And gas collecting tube, the gas collecting tube and institute
Oil gas export pipeline is stated with the pyrolysis oil gas vent to be connected.
Pyrolysis reactor according to embodiments of the present invention, oil gas export pipeline sum aggregate tracheae can be fast by the pyrolysis oil gas of generation
Speed export pyrolysis reactor, so as to reduce the residence time of pyrolysis oil gas, inhibits the secondary response of pyrolysis oil gas, and employ
Heat accumulating type, without gas, solid heat carrier, improves the calorific value of pyrolysis gas, while pyrolytic reaction without heat carrier radiant tube heating technique
The advantages such as it is few that device has taken into account equipment, easy to operate, and failure rate is low.
In one embodiment of the invention, the pyrolysis reactor has reactor body, the reacting body tool
There are feed inlet, discharge port and pyrolysis oil gas vent, reaction compartment is limited in the reactor body.
In one embodiment of the invention, baffle is respectively arranged on the both sides tube wall of the heat accumulation type radiant tube,
The baffle is located at the top of oil gas export pipeline, and covers whole vertical projections of the oil gas export pipeline.
In one embodiment of the invention, the baffle is from the vertical section of the tube wall of the heat accumulation type radiant tube
Phase tangent line is starting point, extends downward into the vertical section of the oil gas export pipeline at an angle, the angle ranging from 40-90
Degree, and without 90 degree.
In one embodiment of the invention, between the oil gas export pipeline and the neighbouring heat accumulation type radiant tube
Tube wall distance 1/2-3 times of pipe diameter d is exported for the oil gas.
In one embodiment of the invention, the oil gas export pipeline is arranged in parallel with the heat accumulation type radiant tube,
And two oil gas export pipelines are symmetrically arranged at left and right sides of the heat accumulation type radiant tube.
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, the heat accumulation type radiant tube is made of heat accumulating type honeycomb ceramics and radiant tube
's.
Pyrolysis reactor according to embodiments of the present invention, at least with one of following advantages：
1) it is pyrolyzed using pyrolysis reactor, the pyrolysis gas calorific value for being pyrolyzed generation is high, no gas heat carrier dilution, subsequently
Pyrolysis gas condensation cold it is few, purification and the equipment pipes such as dedusting are small.
2) heat accumulation type radiant tube uses heat accumulating type honeycomb ceramics, will be preheated into the fuel and air of combustion chamber, reduces smoke evacuation
Temperature, the thermal efficiency are high.
3) pyrolysis reactor can modular combination, be suitble to different garbage treatment quantities, be easy to industrialization promotion.
4) using septate heat transfer technique, the component of rubbish is changed insensitive.
5) pyrolysis reactor only needs rubbish to carry out simple pre-treatment.
The additional aspect and advantage of the present invention will be set forth in part in the description, and will partly become from the following description
It obtains significantly or is recognized by the practice of the present invention.
Description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will become in the description from combination accompanying drawings below to embodiment
Significantly and it is readily appreciated that, wherein：
Fig. 1 shows the structure diagram of pyrolysis reactor according to an embodiment of the invention；
Fig. 2 shows that heat accumulation type radiant tube, baffle and oil gas are led in pyrolysis reactor according to an embodiment of the invention
The structure diagram of outlet pipe；
Fig. 3 shows the structure diagram of pyrolysis reactor according to an embodiment of the invention.
Specific embodiment
The embodiment of the present invention is described below in detail, the example of the embodiment is shown in the drawings, wherein from beginning to end
Same or similar label represents same or similar element or the element with same or like function.Below with reference to attached
The embodiment of figure description is exemplary, and is only used for explaining the present invention, and is not considered as limiting the invention.
In the description of the present invention, term " longitudinal direction ", " transverse direction ", " on ", " under ", "front", "rear", "left", "right", " perpendicular
Directly ", the orientation of the instructions such as " level ", " top ", " bottom " or position relationship are based on orientation shown in the drawings or position relationship, are only
The present invention rather than require the present invention therefore it is not intended that right with specific azimuth configuration and operation for ease of description
The limitation of the present invention.
It should be noted that term " first ", " second " are only used for description purpose, and it is not intended that instruction or hint phase
To importance or the implicit quantity for indicating indicated technical characteristic.Define " first " as a result, the feature of " second " can be with
Express or implicitly include one or more this feature.Further, in the description of the present invention, unless otherwise saying
Bright, " multiple " are meant that two or more.
According to an aspect of the present invention, the present invention provides a kind of pyrolysis reactors.It is according to the present invention with reference to figure 1
The pyrolysis reactor is explained in embodiment, which includes：It is pyrolyzed oil gas vent 110, heat accumulating type radiation
Pipe 200, oil gas export pipeline 300 and gas collecting tube 400, wherein, the (also referred to as " radiation herein of heat accumulation type radiant tube 200
Pipe ") along the short transverse multi-tier arrangement of pyrolysis reactor, every layer has more heat accumulating type spokes parallel to each other in the horizontal direction
Penetrate pipe 200；Oil gas exports short transverse multi-tier arrangement of the pipeline 300 along pyrolysis reactor, and every layer has more in the horizontal direction
Upper oil gas export pipeline parallel to each other, oil gas export and are provided with through-hole on the surface of pipeline；Gas collecting tube 400 and oil gas delivery line
Road 300 is connected with pyrolysis oil gas vent 110.
With reference to figure 1, in some embodiments of the invention, which can also be provided by following form, the heat
Solution reactor includes：
Reactor body 100, the reactor body have feed inlet, discharge port and pyrolysis oil gas vent, the reaction
Reaction compartment is limited in device ontology；
Multilayer heat accumulation type radiant tube 200, the multilayer heat accumulation type radiant tube is in the pyrolysis reaction region along the reaction
Device body height direction is spaced apart, and every layer of heat accumulation type radiant tube includes the heat accumulating type of multiple horizontally spaced distributions
Radiant tube, and the bottom of at least one of described multilayer heat accumulation type radiant tube heat accumulation type radiant tube is provided at least one
A pyrolysis oil gas vent；
Oil gas exports pipeline 300, and the oil gas exports short transverse multi-tier arrangement of the pipeline along the pyrolysis reactor, often
Layer has more oil gas export pipelines parallel to each other in the horizontal direction, the every oil gas export pipeline and the pyrolysis oil
Gas outlet；
Gas collecting tube 400, the gas collecting tube are connected with oil gas export pipeline.
Pyrolysis reactor according to embodiments of the present invention can effectively inhibit the secondary response of oil gas as a result, improve tar production
Rate, and heat accumulating type is employed without heat carrier radiant tube heating technique, without gas, solid heat carrier, the calorific value of pyrolysis gas is improved,
The advantages such as it is few to have taken into account equipment for pyrolysis reactor simultaneously, easy to operate, and failure rate is low.
In addition, being pyrolyzed using the pyrolysis reactor to rubbish, refuse pyrolysis temperature is low, and pyrolysis is efficient, and can
To realize bioxin zero-emission.
In addition, the pyrolysis reactor can modular combination, be suitble to different garbage treatment quantities, be easy to industrial applications.
According to a particular embodiment of the invention, reactor body 100 further comprises air intake 120, fuel gas inlet 130
With exhanst gas outlet 140.
According to a particular embodiment of the invention, every layer of radiant tube includes multiple parallel and equally distributed radiant tube and every
A radiant tube is parallel with each radiant tube in adjacent two layers of radiant tube up and down and is staggered along reactor body short transverse
Distribution.Thus, it is possible to significantly improve the pyrolysis efficiency of material, and then improve pyrolysis oily yield.
According to a particular embodiment of the invention, short transverse multi-tier arrangement of the oil gas export pipeline 300 along pyrolysis reactor,
Every layer has more oil gas export pipelines parallel to each other in the horizontal direction, is provided on the surface of oil gas export pipeline logical
Hole；Oil gas export pipeline 300 is connected with gas collecting tube 400, and gas collecting tube 40 is connected with oil gas vent 12.As a result, by radiating
Pipe lower end arrangement oil gas export pipeline 30 reduces residence time of the tar in burner hearth, avoids the second pyrolysis of tar, improves burnt
Oily yield.According to a particular embodiment of the invention, oil gas export pipeline 300 is arranged in parallel, and radiant tube 200 with radiant tube 200
The left and right sides be symmetrically arranged with two oil gas export pipelines 300.As a result, by arranging oil gas delivery line in the both sides of radiant tube
Road 30 reduces residence time of the tar in burner hearth, avoids the second pyrolysis of tar, improves tar yield.
According to an embodiment of the invention, oil gas delivery line 300 is symmetrical set under each heat accumulation type radiant tube 200
Side.It is exported as a result, convenient for oil gas, reduces residence time of the tar in burner hearth, avoid the second pyrolysis of tar, improve tar
Yield.
According to an embodiment of the invention, oil gas delivery line 300 is with being pyrolyzed the connection mode of oil gas vent 110 not by special
Limitation, according to a particular embodiment of the invention, the oil gas delivery line 300 of same layer are connected to same pyrolysis oil gas vent 110.
The oil gas delivery line 300 of some specific embodiment, adjacent two layers or more layers according to the present invention is connected to same pyrolysis oil
Gas outlet 110.Thus, it is possible to oil gas is collected, simplify technique and improves tar yield, while can be exported in order to oil gas.
With reference to figure 2, according to an embodiment of the invention, baffle is respectively arranged on the both sides tube wall of heat accumulation type radiant tube 200
800, which is located at the top of oil gas export pipeline 300, and covers whole vertical projections of oil gas export pipeline 300.It changes
Sentence is talked about, and baffle 800 is provided on every heat accumulation type radiant tube 200, oil gas delivery line 300 is arranged on heat accumulation type radiant tube 200
Near so that baffle 800 covers the upper surface of oil gas delivery line 300, and baffle 800 connects from heat accumulation type radiant tube 200
Tactile point extends to the outside upright edge of oil gas delivery line 300.Inventor has found, by quickly exporting pipeline in every oil gas
Top setting baffle, not only prevent material decline during friction prolong oil gas delivery line, and then extend the longevity of oil gas delivery line
Life；And baffle also acts as the drainage to material, and material is prevented to be stuck between radiant tube and oil gas export pipeline, causes object
Material blocks；In addition, baffle also avoids tar from spreading, and then improves the efficiency of export tar, tar yield is improved.
According to a particular embodiment of the invention, oil gas delivery line 300 is located at below 200 horizontal diameter of heat accumulation type radiant tube empty
Between and positioned at 200 both sides of heat accumulation type radiant tube, baffle 800 and oil gas delivery line 300 are tangent.The drainage of baffle is more as a result,
It is good, more preferably tar can be avoided to spread, the longer life expectancy of oil gas delivery line, tar yield higher.Specific reality according to the present invention
Example is applied, as shown in Fig. 2, vertical section A (A of the baffle 800 from the tube wall of radiant tube 8001) phase tangent line for starting point, in certain angle
Degree α extends downward into the vertical section B (B of oil gas export pipeline 3001), angle [alpha] is 40-90 degree, without 90 degree.As a result,
The shortest length of baffle is can to block oil gas export pipeline.
According to a particular embodiment of the invention, distance between oil gas export pipeline 300 and the tube wall of neighbouring radiant tube 200
1/2-3 times of 300 caliber d of pipeline is exported for oil gas.Thus, it is possible to which the tar that will export generation at once, avoids coke tar cracking, carry
High tar yield.
According to an embodiment of the invention, gas collecting tube 400 includes：Gas-collecting branch pipe 410 and gas gathering manifold 420, wherein, gas collection is total
Pipe 420 exports pipeline 300 with multilayer oil gas by multiple gas-collecting branch pipes 410 and is connected.It is pyrolyzed the pyrolysis oil gas of generation as a result, through collection
Tracheae and gas gathering manifold export so as to reduce residence time of the pyrolysis oil gas in pyrolysis oven, effectively inhibit the secondary counter of oil gas
Should, improve tar yield.
According to an embodiment of the invention, the heat accumulation type radiant tube is made of heat accumulating type honeycomb ceramics and radiant tube.By
This will be preheated into the fuel and air of combustion chamber using heat accumulating type honeycomb ceramics, reduces exhaust gas temperature, and the thermal efficiency is high.
Fig. 3 shows the pyrolysis reactor of one embodiment of the invention, as shown in figure 3, the pyrolysis reactor further wraps
It includes：Spiral discharging device 700, the spiral discharging device 700 are connected with discharge port.As a result, while discharging, material is crushed
Processing, convenient for subsequent applications.
According to an embodiment of the invention, which further comprises：Feed hopper 500 and feeding screw 600,
Wherein, feed hopper 500 has lower discharge port；Feeding screw 600 has material inlet and material outlet, and material inlet is under
Discharge port is connected, and material outlet is connected with feed inlet, passes through feeder 600 for that will be stored in the material in feed hopper 500
Into in reaction compartment.
Below with reference to specific embodiment, the present invention will be described, it should be noted that these embodiments are only explanation
Property, and be not considered as limiting the invention.
Embodiment 1：
Certain domestic waste constituent analysis is as shown in table 1, and rubbish water content is 43%, using pyrolysis reactor to the life
Work is handled, wherein, the structure diagram of pyrolysis reactor is as shown in figure 3, detailed process is as follows：
Table 1
Table 2
1st, rubbish of marching into the arena pre-processes, and big grain size dregs, glass and metal contained in the rubbish after marching into the arena etc. is not easy heat
Solution or the substance that cannot be pyrolyzed are rejected in advance；
2nd, it is sent after the rubbish rejected after being not easy pyrogen being fed directly to sanitary fill compression dehydration to pyrolysis reactor；
3rd, combustion gas and air stoichiometry and amount of the control into radiant tube controls the temperature of pyrolysis oven, ensures pyrolysis Indoor Temperature
Spend is 680 DEG C or so；
4th, pyrolysis reactor bottom discharge revolution speed of screw is controlled so that rubbish mean residence time~1.5h, by bottom
The spiral that discharges discharge pyrolysis oven；
5th, by refuse pyrolysis charcoal, Sichuan lotus coal, lime stone with ratio 36.76:52.33:10.91 ratio mixing system
Powder, mixture average grain diameter~300 μm obtained, wherein, the constituent analysis of Sichuan lotus coal is as shown in table 2；
6th, pyrolysis reactor gasification is fed the mixture into, gasifying agent uses landfill leachate and partial air, gasification and melting
1300 DEG C of furnace temperature；
7th, in pyrolysis reactor, gasification reaction, production gasification gas and liquid glass body occur for rubbish charcoal, coal and gasifying agent
Lime-ash, building sand after the recovered noble metal of liquid lime-ash；
8th, the pyrolysis oil gas that pyrolysis reactor pyrolysis generates obtains high-quality pyrolytic tar after Oil-gas Separation ,~75%
Pyrolysis gas enters pyrolysis reactor burning and provides fuel for pyrolysis, and~25% pyrolysis gas and gasification gas is through mixing and preliminary purification
Laggard gas turbine combustion power generation.
Lime-ash is analyzed：The chilling slag Zhong non-1.3ng-TEQ/kg of content of dioxin, Pb Leachings value are 0.2013mg/
L, Cr Leaching value are 0.387mg/L, and Cd Leachings value is 0.147mg/L, remaining is not detected, is met about hazardous waste
Leaching characteristic identification standard.
Embodiment 2：
Certain domestic waste constituent analysis is as shown in table 3, and rubbish water content is 51%, using pyrolysis reactor to the life
Work is handled, wherein, the structure diagram of pyrolysis reactor is as shown in figure 3, detailed process is as follows：
Table 3
Table 4
1st, rubbish of marching into the arena pre-processes, and big grain size dregs, glass and metal contained in the rubbish after marching into the arena etc. is not easy heat
Solution or the substance that cannot be pyrolyzed are rejected in advance；
2nd, it is sent after the rubbish rejected after being not easy pyrogen being fed directly to sanitary fill compression dehydration to pyrolysis reactor；
3rd, combustion gas and air stoichiometry and amount of the control into radiant tube, controls the temperature of pyrolysis oven, ensures pyrolysis reactor
Pyrolysis indoor temperature be 700 DEG C or so；
4th, pyrolysis reactor bottom discharge revolution speed of screw is controlled so that rubbish mean residence time~1h goes out by bottom
Expect spiral discharge pyrolysis reactor；
5th, by pyrolytic carbon, Yangquan Shanxi anthracite, lime stone with ratio 47.3:42.1:10.6 ratio mixes powder processed, system
Mixture average grain diameter~the 400um obtained, wherein, the anthracitic constituent analysis of Yangquan Shanxi is as shown in table 4；
6th, pyrolysis reactor gasification is fed the mixture into, gasifying agent uses landfill leachate and partial air, gasification and melting
1420 DEG C of furnace temperature；
7th, in pyrolysis reactor, gasification reaction, production gasification gas and liquid lime-ash, liquid lime-ash occur for rubbish charcoal and coal
Building sand after recovered noble metal；
8th, the pyrolysis oil gas that pyrolysis reactor pyrolysis generates obtains high-quality pyrolytic tar after Oil-gas Separation ,~80%
Pyrolysis gas enters pyrolysis reactor burning and provides fuel for pyrolysis, and~20% pyrolysis gas and gasification gas is through mixing and preliminary purification
Laggard gas turbine combustion power generation.
Lime-ash is analyzed：The chilling slag Zhong non-1.1ng-TEQ/kg of content of dioxin, Pb Leachings value are 0.2375mg/
L, Cr Leaching value are 0.409mg/L, and Cd Leachings value is 0.185mg/L, and Hg Leachings value is 0.024mg/L,
Yu Wei is detected, and is met about Extraction Toxicity Identification Standard of Hazardous Waste.
In the description of this specification, reference term " one embodiment ", " example ", " is specifically shown " some embodiments "
The description of example " or " some examples " etc. means specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment of the present invention or example.In the present specification, schematic expression of the above terms are not
Centainly refer to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be any
One or more embodiments or example in combine in an appropriate manner.
Although an embodiment of the present invention has been shown and described, it will be understood by those skilled in the art that：Not
In the case of being detached from the principle of the present invention and objective a variety of change, modification, replacement and modification can be carried out to these embodiments, this
The range of invention is limited by claim and its equivalent.
Claims (6)
1. a kind of pyrolysis reactor, which is characterized in that including：
It is pyrolyzed oil gas vent；
Heat accumulation type radiant tube, short transverse multi-tier arrangement of the heat accumulation type radiant tube along the pyrolysis reactor, every layer has
More heat accumulation type radiant tubes parallel to each other in the horizontal direction；
Oil gas exports pipeline, and short transverse multi-tier arrangement of the oil gas export pipeline along the pyrolysis reactor, every layer has
More oil gas export pipelines parallel to each other in the horizontal direction, the oil gas export and are provided with through-hole on the surface of pipeline；With
And
Gas collecting tube, the gas collecting tube exports pipeline with the oil gas and the pyrolysis oil gas vent is connected,
Wherein,
The heat accumulation type radiant tube is made of heat accumulating type honeycomb ceramics and radiant tube,
The gas collecting tube includes gas-collecting branch pipe and gas gathering manifold, and the gas gathering manifold passes through multiple gas-collecting branch pipes and multilayer institute
Oil gas export pipeline is stated to be connected.
2. pyrolysis reactor according to claim 1, which is characterized in that divide on the both sides tube wall of the heat accumulation type radiant tube
It is not provided with baffle, the baffle is located at the top of oil gas export pipeline, and covers the whole of the oil gas export pipeline
Vertical projection.
3. pyrolysis reactor according to claim 2, which is characterized in that the baffle is from the pipe of the heat accumulation type radiant tube
The phase tangent line of the vertical section of wall is starting point, extends downward into the vertical section of the oil gas export pipeline, institute at an angle
Angle is stated as 40-90 degree, and without 90 degree.
4. pyrolysis reactor according to claim 1, which is characterized in that the oil gas export pipeline and the neighbouring storage
Tube wall distance between hot type radiant tube exports 1/2-3 times of pipe diameter d for the oil gas.
5. pyrolysis reactor according to claim 1, which is characterized in that the oil gas export pipeline and the heat accumulating type spoke
Pipe parallel arrangement is penetrated, and two oil gas export pipelines are symmetrically arranged at left and right sides of the heat accumulation type radiant tube.
6. pyrolysis reactor according to claim 1, which is characterized in that the oil gas export pipeline of same layer is connected to one
A pyrolysis oil gas vent.
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