CN203513564U - Pyrolyzation device for carbon-containing substance - Google Patents
Pyrolyzation device for carbon-containing substance Download PDFInfo
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- CN203513564U CN203513564U CN201320711645.7U CN201320711645U CN203513564U CN 203513564 U CN203513564 U CN 203513564U CN 201320711645 U CN201320711645 U CN 201320711645U CN 203513564 U CN203513564 U CN 203513564U
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- 239000000126 substance Substances 0.000 title abstract description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title abstract 2
- 229910052799 carbon Inorganic materials 0.000 title abstract 2
- 238000001914 filtration Methods 0.000 claims abstract description 40
- 239000007787 solid Substances 0.000 claims abstract description 27
- 238000000197 pyrolysis Methods 0.000 claims description 119
- 238000010438 heat treatment Methods 0.000 claims description 16
- 230000004888 barrier function Effects 0.000 claims description 6
- 239000012528 membrane Substances 0.000 claims description 3
- -1 filter screen Substances 0.000 claims description 2
- 239000000706 filtrate Substances 0.000 claims description 2
- 239000000969 carrier Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 42
- 239000000428 dust Substances 0.000 abstract description 22
- 230000008569 process Effects 0.000 abstract description 20
- 238000000926 separation method Methods 0.000 abstract description 17
- 238000005516 engineering process Methods 0.000 abstract description 15
- 239000003054 catalyst Substances 0.000 abstract description 8
- 230000002779 inactivation Effects 0.000 abstract description 3
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- 230000003197 catalytic effect Effects 0.000 abstract 3
- 230000003750 conditioning effect Effects 0.000 abstract 2
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- 230000001143 conditioned effect Effects 0.000 abstract 1
- 238000001556 precipitation Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 58
- 238000006243 chemical reaction Methods 0.000 description 16
- 239000003575 carbonaceous material Substances 0.000 description 14
- 239000000047 product Substances 0.000 description 14
- 239000002245 particle Substances 0.000 description 12
- 238000006555 catalytic reaction Methods 0.000 description 10
- 239000003245 coal Substances 0.000 description 7
- 238000009434 installation Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 238000010791 quenching Methods 0.000 description 7
- 230000000171 quenching effect Effects 0.000 description 7
- 239000002817 coal dust Substances 0.000 description 6
- 239000006004 Quartz sand Substances 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 5
- 239000000571 coke Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- 238000007599 discharging Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 3
- 239000003034 coal gas Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 235000013339 cereals Nutrition 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
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- 239000007791 liquid phase Substances 0.000 description 2
- 238000010327 methods by industry Methods 0.000 description 2
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- 229910052573 porcelain Inorganic materials 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 1
- 235000011613 Pinus brutia Nutrition 0.000 description 1
- 241000018646 Pinus brutia Species 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000010903 husk Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
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- 239000004058 oil shale Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
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- 238000001149 thermolysis Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
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Abstract
The utility model relates to a pyrolyzation device for a carbon-containing substance. The gas-solid separation and the catalytic conditioning can be synchronously realized in the pyrolyzation process. In the existing pyrolyzation technology, a gas-solid separation device and a catalytic conditioning device for pyrolyzating the gas at high temperature are independent to the pyrolyzation device. The high-boiling-point tar is separated out because of the temperature decrease outside the pyrolyzation device, the dust cannot be effectively removed, and the dust carrying and catalyst inactivation can be caused. Along the precipitation and accumulation of the tar, the dust also can block the device and a pipeline. The pyrolyzation device is characterized by having a two-layer structure. The pyrolyzation gas produced by the pyrolyzation is processed through the three-stage gas-solid separation measure such as filtering by an inner layer 2 of the pyrolyzation device, separation by a diameter expanding section 5 of a gas collection cavity and filtering by a filter layer 6, so that the high-efficient gas-solid separation in the pyrolyzation device can be realized, and the dust in an oil-gas product can be avoided. A catalyst is added in the filter layer 6, so that the catalytic pyrolyzation process can be simplified, and the pyrolyzation oil-gas product can be conditioned.
Description
Technical field
The utility model relates to solid derived energy chemical technical field.Particularly, the utility model relates to a kind of pyrolysis installation of carbonaceous material, and it has bilayer structure, can realize modified integrated of pyrolysis, dedusting and catalysis.
Background technology
Carbonaceous material, such as coal, biomass, resinous shale etc., obtains pyrolysis oil, gas product by pyrolytic process, is the efficient effective way of utilizing of solid energy high value added utilization and energy step.The subject matter that pyrolytic process exists is at present that high temperature gas-solid separation efficiency is low, and in high temperature pyrolysis gas, dust is carried secretly seriously, can cause the obstruction of equipment and pipeline, affects the steady running of equipment; The pyrolysis oil particle concentration of simultaneously collecting is high, need further take off dirt and process, high because of processing costs, has reduced its utility value.
Pyrolytic process of coal can be divided into external-heat and internal heat type two classes by type of heating.The thermal source of external-heat pyrolysis technique is to be provided outward by pyrolysis oven, and representational technique has metallurgical coke oven, Wood (W-D) charring furnace and Kao Baisi charring furnace; The thermal source of internal heat type pyrolysis is that the heat by high-temperature heat carrier is directly passed to coal dust, makes carbonaceous material generation pyrolytic reaction.Internal heat type pyrolytic process, according to the difference of thermal barrier, is divided into gaseous heat-carrier pyrolytic process and solid heat carrier pyrolysis technique.Gaseous heat-carrier pyrolytic process is normally directly introduced the high-temperature flue gas obtaining after fuel combustion in pyrolyzer, mixes with carbonaceous material, realizes the heating to raw material, and representational technique has COED technology and the ENCOAL technology of the U.S.; Solid heat carrier pyrolysis technique is utilized in high-temperature solid particle (such as semicoke, Ceramic Balls, quartz sand etc.) Yu Mei pyrolysis chamber and to be mixed the pyrolysis that realizes coal, and representational technique has the coal of U.S. Garrett technology, German Lu Qi-Rule (L-R) technology, Chinese Academy Of Sciences Process Engineering Research Institute to pull out the DG technology etc. of a technology, Dalian University of Technology.Due to pyrolytic reaction, relate to complicated gas, liquid, solid phase reaction, when high temperature pyrolysis gas is spilled over to outside stove, can be entrained with dust.Particularly in internal heat type pyrolytic process, therefore no matter gas phase and solid phase disturbance are violent, and the dust content of carrying secretly in pyrolysis gas can be higher, which kind of pyrolytic process, the high temperature pyrolysis gas of its generation all need carry out gas-solid separation at hot stage, to realize dedusting and the purification of high temperature pyrolysis gas.
Current high temperature gas-solid equipment is all independent mutually with pyrolyzer, is placed in pyrolyzer rear end.Main equipment comprise cyclonic separator (Institute of Engineering Thernophysics, Academia Sinica. solid heat carrier rapid pyrolysis method and device. Chinese patent, 200710119476.7), wire gauzee filter (Chinese Academy Of Sciences Process Engineering Research Institute. the method for thermolysis preparing liquid fuel from steam explosion stalk fermented residue and device, Chinese patent, 20051001l104.3), porcelain filter (Wuwei, Tian Guishan, crux. with porcelain filter, carry out high-temperature gas duster technical study. Liaoning Project Technology University's journal: natural science edition, 2000, 19 (2): 214), grain bed (Xia Juncang, Xu Shisen, Gao Shiwang. the experimental study of Moving Granular Bed Filter for Hot Gas Cleanup. power engineering, 2003, 23 (2): 2337) etc.In these isolation technique, cyclonic separator is the normal gas-solid isolation technique adopting, but be limited by pyrolysis air-flow, is that solid carbonaceous substance produces after pyrolytic reaction, and flow velocity is unstable, therefore the separation efficiency of the cyclonic separator of single-stage is low, efficiency of dust collection for fine dust is not high, in theory, adopts multi-cyclone can improve efficiency of dust collection, but correspondingly, can increase the residence time of high temperature pyrolysis gas before cooling, can cause the secondary reaction of high temperature pyrolysis gas, reduce oil gas quality.Some filtering techniques in addition, comprise the technology such as filtering membrane, filtering layer, grain bed, by the adjusting to filter opening, can improve separation efficiency, but resistance all can increase with load in operational process, and need the blowback of intermittence to guarantee the stable of separation efficiency.
Due to these all separated equipment and technology, all independent mutually with pyrolysis equipment, be positioned at the afterbody of pyrolyzer, high temperature pyrolysis gas leaves pyrolyzer and enters after gas-solid separated equipment, inevitably temperature drop, can cause pyrolysis oil to be separated out from high temperature pyrolysis gas, and be bonded together with dust, cause adhesion or the obstruction of separating device parts, remove extremely inconvenient.And the more important thing is, because the dust of carrying secretly can not effectively be removed in separator, so the tar dirt obtaining is high containing rate, processing cost increases, utility value is low.Particularly, the pyrolytic process of some internal heat types, solid particulate disturbance in pyrolyzer is violent, and the particle concentration in high temperature pyrolysis gas is larger, and the problem of line clogging is more serious.
In addition, modified in order to realize the catalysis of pyrolysis oil gas product, it is modified that the coal gas of high temperature that need produce pyrolysis carries out catalysis in catalyticreactor, general technique is method (the PT Williams that adopts two sections of stoves, HM Chishti.Two stage pyrolysis of oil shale using a zeolite catalyst, Journal of Analytical and Applied Pyrolysis.2000, 55 (2): 217), make the high temperature pyrolysis gas producing in pyrolyzer after overflowing pyrolyzer, directly enter catalyticreactor, complete quality regulation and control and reconstruction to high temperature pyrolysis oil gas, to improve the quality of pyrolysis oil gas product.But due to pyrolyzer and catalyticreactor separate, the dust that high temperature pyrolysis gas is carried secretly is removed, and easily causes the inactivation of catalyzer, causes the obstruction of catalyticreactor; If after catalyticreactor placement and gas-solid tripping device, dust is removed in advance, need again insulation and heating installation, there is the shortcoming that energy consumption is high.
Therefore visible, in existing pyrolytic process, due to pyrolytic reaction device and high-temperature dust removing device and catalyse pyrolysis reaction unit independent separately, operational path is long, inevitably temperature drop can make tar separate out, cause that dust removal efficiency is low, the problem such as catalyst deactivation and e-quipment and pipe obstruction, and the tar particle concentration of collecting is high, utility value is low.
Summary of the invention
The purpose of this utility model is, in order to overcome because pyrolyzer and gas-solid separator, catalyticreactor are independent separately, under hot conditions, the problem such as efficiency of dust collection is low causes line clogging, the easy inactivation of catalyzer, tar particle concentration is high and steady running is difficult, provides a kind of and has realized gas-solid separation and the modified method of catalysis in pyrolyzer inter-sync.
Another one object of the present utility model is, the device of realizing above-mentioned pyrolysis way is provided.
According to carbonaceous material method for pyrolysis of the present utility model, its pyrolysis reactor is the two sleeve pipes of bilayer structure or double-walled kiln structure, take two sleeve pipes as follows as example, summary of the invention is described, carbonaceous material is added to inner tube 2 and pyrolytic reaction occurs in inner tube from feeding mouth 1, the high temperature pyrolysis gas that reaction produces spreads to outer tube 3 by inner tube 2, enter in the air collecting chamber 4 between two-tube, filtering function by inner tube 2 by most of dust-filtering in inner tube, along with the particle after pyrolysis is discharged, pyrolysis gas in air collecting chamber 4 is through the extension diameter section 5 of outer tube and the filtering layer 6 of air collecting chamber simultaneously, pyrolysis gas is purified completely.
The inner tube 2 of described pyrolyzer is comprised of the filter opening of different pore size, has filtering function, and carbonaceous material is after the interior inner reaction tube of pyrolyzer, and the high temperature pyrolysis gas of generation enters in air collecting chamber 4 after filtration from inner tube.
The outer tube 3 of described pyrolyzer expands in top radius, forms extension diameter section 5, and the gas flow rate in air collecting chamber 4 is declined herein, promotes the further separation of the dust carried secretly in pyrolysis gas, drops on the bottom of air collecting chamber.
The top of the air collecting chamber 4 of described pyrolyzer, before pyrolysis gas spillway 7, is provided with filtering layer 6, and pyrolysis gas is further purified.
Filtering layer 6 in described air collecting chamber by filter plate or/and filter membrane or/and filter screen, or/and filtrate forms, was removed the dust that pyrolysis gas is carried secretly completely before being discharged to pyrolyzer.
Filtering layer 6 in described air collecting chamber, in filtering layer inside or top place catalyzer, make high temperature pyrolysis coal gas obtain catalysis upgrading, pyrolysis oil, the yield of gas product, composition, quality are improved.
Between the inner tube 2 and outer tube 3 of described pyrolyzer, and in inner tube 3, some good heat-transfers, resistant to elevated temperatures web member are set as reinforced heat conduction plate 9, the at least outer tube wall of one end of heat-conducting plate or a side and pyrolyzer or high temperature end face close contact, promote the transmission of heat, and guarantee the even of heating surface.
The type of heating of described pyrolyzer is for passing through the external-heat pyrolysis mode of heating outer tube, or take high-temperature gas thermal barrier or high-temp solid thermal barrier is thermal source, internal heat type pyrolysis way at inner tube heating carbonaceous material, or in order to guarantee heat supply, adopt external-heat and internal heat type Hybrid Heating mode.
Pyrolyzer in the utility model adopts double-deck structure, by the filtration of endothecium structure, the hole enlargement of air collecting chamber is separated and three grades of gas-solid separating measure such as filtering layer filtration, by gas-solid separating unit independently in common pyrolytic technique, be integrated in pyrolysis oven, make separation system maintain hot stage operation always, avoid separating out of liquid phase, improved separation efficiency.In addition, by filtering layer addition catalyzer, the catalysis that also can synchronously carry out pyrolysis is modified, can, by traditional catalyst converter and the separate catalyse pyrolysis technique of pyrolyzer, be integrated in pyrolysis oven and carry out equally.Therefore, pyrolysis installation of the present utility model can be realized modified integrated of pyrolysis, dedusting and catalysis, has greatly simplified pyrolytic process flow process, and energy efficient lowers investment cost, has good industrial applicability prospect.
Accompanying drawing explanation
Fig. 1 is the two sleeve pipe pyrolyzer schematic diagram of the utility model;
Fig. 2 is the principle schematic of the two sleeve pipe pyrolysis installation pyrolysis carbonaceous materials of the utility model;
Fig. 3 is the reinforced heat conduction plate schematic diagram in air collecting chamber in the two sleeve pipe pyrolysis installations of the utility model;
Accompanying drawing sign
1, pyrolyzer feeding mouth 2, two sleeve pipe pyrolyzer inner tube 3, two sleeve pipe pyrolyzer outer tube
4, air collecting chamber 5, pyrolyzer outer tube extension diameter section 6, filtration (catalysis) layer
7, pyrolysis gas-phase product spillway 8, pyrolysis char relief outlet 9, the pyrolyzer heat-conducting plate between two-tube
10, two sleeve pipe heat engine devices 11, screw feeder 12, heating chamber
13, pyrolysis particle discharge gate
Embodiment
Below in conjunction with accompanying drawing, device of the present utility model is further described.
Fig. 1 is shown in by two sleeve pipe pyrolyzer schematic diagram, and the agent structure of this pair of sleeve pipe pyrolyzer comprises inner tube 2 and outer tube 3, and the air collecting chamber between inner and outer tubes 4.Wherein inner tube 2 is reaction tubes, and pyrolytic reaction occurs carbonaceous material in pipe, and the high temperature pyrolysis gas of generation to diffuse outside, through filtering, enters air collecting chamber 4 in inner tube.In air collecting chamber, due to the hole enlargement of outer tube 3 at its afterbody, form extension diameter section 5, make pyrolysis gas after the extension diameter section 5 of air collecting chamber, flow velocity declines, and enters filtering layer 6 simultaneously, obtain further taking off dirt, complete the gas solid separation before deriving from gas-phase product spillway 7.
Gas-solid separating measure of the present utility model is carried out in pyrolyzer, inner tube 2 is comprised of the filter opening of different pore size, the high temperature pyrolysis gas producing is after the filtration of inner tube filter opening, enter air collecting chamber 4, rise to the extension diameter section 5 of air collecting chamber, flow velocity declines, make the further separation of dust of carrying secretly, when gas is finally derived from spillway 7 through filtering layer 6, the fine powder that pyrolysis gas is carried secretly can thoroughly be removed, and realizes high-temperature dust efficiently removing in pyrolysis oven.
And in two sleeve pipe pyrolyzer, because pyrolysis of coal is absorption reaction, pyrolytic reaction occurs in inner tube, make pyrolyzer maintain gas collection cavity temperature a little more than the state in inner tube always, the high temperature pyrolysis gas producing is shifted to high-temperature zone from cold zone, this has been avoided the liquid phase causing due to temperature drop in pyrolysis oven to separate out as much as possible, thereby has overcome the problem of the adhesion of coal dust wall built-up and efficiency of dust collection decline.
The principle schematic of two sleeve pipe pyrolysis installation pyrolysis carbonaceous materials is shown in Fig. 2, comprises two sleeve pipe pyrolyzer 10, screw feeding device 11, heating unit 12, pyrolysis particle discharge gate 13 etc.The outlet of feeding unit is connected with the inner tube import of pyrolyzer.
The utility model illustrates with following embodiment, but the utility model is not limited to following embodiment, and before and after not departing from, under the scope of described aim, change is included in technical scope of the present utility model.
Embodiment 1
Particle diameter 200 object coal dusts, 105 ℃ dry after, from the top feeding mouth 1 of pyrolyzer, join in the inner tube 2 of pyrolyzer, outside under hot heating mode, inner tube temperature is remained within the scope of 400～700 ℃, coal dust generation pyrolytic reaction, gaseous product is on average filtered footpath 0.5mm by the filtration of inner tube) derive the air collecting chamber 4 enter between two sleeve pipes, high temperature pyrolysis gas in air collecting chamber on flow, extension diameter section 5 and filtering layer 6 through outer tube, at gas-phase product spillway 7, discharge, through cooling, process and carry out pyrolysis gas and pyrolysis oil separating; Reach after predetermined reaction time, coal dust obtains abundant pyrolytic reaction, in pyrolyzer bottom, carries out coke discharging operation, semicoke is discharged from coke discharging mouth 8, and carry out quenching processing.The pyrolysis oil relevant to pyrolysis, gas disposal and collection technique and quenching technology can be processed by existing ripe mode.
By the high temperature pyrolysis gas producing after this kind of mode pyrolysis, through three grades of gas-solid separating measure such as two filtrations of internal surface of sleeve pipe, the hole enlargement of air collecting chamber separation and filtering layer filtrations, can make the dirt of pyrolytic tar be controlled at below 0.1% containing rate.
Particle diameter is less than the coal dust of 1mm, 105 ℃ dry after, the pattern of heating pyrolysis in adopting, the quartz sand of 950 ℃ that is 2.5mm with median size mixes at feeding mouth 1 place, the top of pyrolyzer, and joins in the inner tube 2 of pyrolyzer, take quartz sand as thermal barrier, pulverized coal particle is heated, by adjusting the material proportion of coal dust and quartz sand, inner tube temperature is remained within the scope of 400～700 ℃, there is pyrolytic reaction.The high temperature pyrolysis gas producing is through the filtration (filter footpath～0.45mm) of inner tube, enter the air collecting chamber 4 between two sleeve pipes, high temperature pyrolysis gas in air collecting chamber on flow, extension diameter section 5 and filtering layer 6 through outer tube, at gas-phase product spillway, 7 places discharge, and through cooling, process and carry out pyrolysis gas and pyrolysis oil separating.The quenching relevant to pyrolysis, pyrolysis gas are processed and collection technique, and quartz sand can be processed by existing ripe mode with the separated of pyrolysis char and thermal barrier circulating technology.
The pine wood chip of 105 ℃ of oven dry, the abandoned biomass that mixes of sawdust and rice husk, after high speed disintegrator is pulverized, from pyrolyzer top feeding mouth, add, under the pattern of external heat, the inner tube temperature of pyrolyzer is remained within the scope of 400～750 ℃, the raw pyrolytic reaction of biomass fermentation, pyrolysis high-temperature gas product is derived by the filtration (filter footpath is between 0.1-0.5mm) of inner tube, enter the air collecting chamber 4 between two sleeve pipes, high temperature pyrolysis gas in air collecting chamber on flow, extension diameter section 5 and filtering layer 6 through outer tube, at gas-phase product spillway, 7 places discharge, by cooling, process and carry out pyrolysis gas and pyrolysis oil separating, resinous shale powder in pyrolyzer inwall reaches after predetermined reaction time, discharges, and carry out quenching processing from coke discharging mouth 8.The pyrolysis oil relevant to pyrolysis, gas disposal and collection technique and quenching technology can be processed by existing ripe mode.
Resinous shale is after pulverizing, 6mm is with thin resinous shale powder, from pyrolyzer top feeding mouth, add, under the pattern of external heat, the inner tube temperature of pyrolyzer is remained within the scope of 400～750 ℃, resinous shale generation pyrolytic reaction, pyrolysis high-temperature gas product is derived by the filtration (on average filtering footpath 0.5mm) of inner tube, enter the air collecting chamber 4 between two sleeve pipes, high temperature pyrolysis gas in air collecting chamber on flow, through extension diameter section 5 and the filtering layer 6 of outer tube, through gas-phase product spillway, go out to discharge, by cooling, process and carry out pyrolysis gas and pyrolysis oil separating; Resinous shale powder in pyrolyzer inner tube reaches after predetermined reaction time, discharges, and carry out quenching processing at pyrolyzer bottom coke discharging mouth 8.The pyrolysis oil relevant to pyrolysis, gas disposal and collection technique and quenching technology can be processed by existing ripe mode.
Embodiment 5
The difference of embodiment 5 and embodiment 1, is to have increased reinforced heat conduction plate 9 in the air collecting chamber of two sleeve pipe pyrolyzer.Some good heat-transfers, resistant to elevated temperatures web member are set between the inner and outer tubes of two sleeve pipe pyrolyzer as reinforced heat conduction plate, promote the importing of heat from the outer tube (3) of the heating zone of pyrolyzer to inner tube (2), rapid heating carbonaceous material.
Embodiment 6
Embodiment 6 and embodiment 1 difference, the filtering layer that is two sleeve pipe pyrolyzer contains loaded catalyst particle, in filtering layer inside or top place catalyzer, make high temperature pyrolysis coal gas obtain catalysis upgrading, change yield, composition and the quality of pyrolysis oil gas product.With 20-40 order γ-Al
2o
3as support of the catalyst, it is the preferred 6-12% of 1-20%(that carrier surface load accounts for carrier quality) Cr
3o
4catalyzer is as catalyse pyrolysis catalyzer, at catalyst packing height, be the preferred 6-10cm of 2-20cm() condition under, high temperature pyrolysis gas is carried out to catalysis, can increase pyrolysis gas yield approximately 12%, and can promote the lighting of tar, increase the quality approximately 10% of benzene, naphthalene and derivative thereof.
It is pointed out that for the utility model specific implementation method, the sleeve pipe of described two sleeve pipe pyrolyzer can be the structures such as round, square or Polygons.The combining form of this pyrolyzer and other devices and operating method can suitably be improved, but can not deviate from thus scope of the present utility model and the essence spirit of crossing regulation in claims.
Claims (9)
1. a pyrolysis reactor, comprises interior outer double-layer structure, and internal layer forms pyrolysis chamber, and inner layer wall is provided with filter opening, is air collecting chamber between ectonexine, and feeding mouth is connected with pyrolysis chamber, and the top of air collecting chamber is provided with spillway.
2. a kind of pyrolysis reactor according to claim 1, is characterized in that described ectonexine is for two sleeve pipes or double-walled kiln structure.
3. a kind of pyrolysis reactor according to claim 2, is characterized in that described sleeve pipe is round, square or polygonal.
4. a kind of pyrolysis reactor according to claim 1 and 2, is characterized in that described outer top is provided with extension diameter section.
5. a kind of pyrolysis reactor according to claim 1 and 2, is characterized in that being provided with heat-conducting plate between described ectonexine, the outer tube wall of one end of described heat-conducting plate or a side and pyrolyzer or high temperature end face close contact.
6. a kind of pyrolysis reactor according to claim 1 and 2, is characterized in that the top spillway of described air collecting chamber is provided with filtering layer before.
7. a kind of pyrolysis reactor according to claim 1 and 2, the type of heating that it is characterized in that described pyrolyzer is the external-heat pyrolysis mode at outer tube external heat, or take the internal heat type pyrolysis way that high-temperature gas thermal barrier or solid thermal carriers heat in inner tube as thermal source, or for adopt the Hybrid Heating mode of external-heat and internal heat type simultaneously.
8. a kind of pyrolysis reactor according to claim 6, is characterized in that described filtering layer is their combination of filter plate, filter membrane, filter screen, filtrate or two kinds.
9. a kind of pyrolysis reactor according to claim 6, is characterized in that described filtering layer inside or top placement catalyzer.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104212469A (en) * | 2014-09-10 | 2014-12-17 | 中国科学院过程工程研究所 | Pyrolysis, dust removal and catalytic conditioning integrated reaction device |
| CN104629775A (en) * | 2013-11-12 | 2015-05-20 | 中国科学院过程工程研究所 | Pyrolysis device for carbonaceous substance |
| CN105087077A (en) * | 2014-05-05 | 2015-11-25 | 汪春雷 | Internal heat vertical type garbage full vapourizing furnace |
-
2013
- 2013-11-12 CN CN201320711645.7U patent/CN203513564U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104629775A (en) * | 2013-11-12 | 2015-05-20 | 中国科学院过程工程研究所 | Pyrolysis device for carbonaceous substance |
| CN105087077A (en) * | 2014-05-05 | 2015-11-25 | 汪春雷 | Internal heat vertical type garbage full vapourizing furnace |
| CN104212469A (en) * | 2014-09-10 | 2014-12-17 | 中国科学院过程工程研究所 | Pyrolysis, dust removal and catalytic conditioning integrated reaction device |
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