CN102433165A - Old automobile breaking residue catalytic gasification device - Google Patents
Old automobile breaking residue catalytic gasification device Download PDFInfo
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- CN102433165A CN102433165A CN2011103189740A CN201110318974A CN102433165A CN 102433165 A CN102433165 A CN 102433165A CN 2011103189740 A CN2011103189740 A CN 2011103189740A CN 201110318974 A CN201110318974 A CN 201110318974A CN 102433165 A CN102433165 A CN 102433165A
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- 238000002309 gasification Methods 0.000 title claims abstract description 21
- 230000003197 catalytic effect Effects 0.000 title claims abstract description 14
- 238000000197 pyrolysis Methods 0.000 claims abstract description 93
- 239000007789 gas Substances 0.000 claims abstract description 84
- 238000002485 combustion reaction Methods 0.000 claims abstract description 36
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 23
- 239000001257 hydrogen Substances 0.000 claims abstract description 23
- 239000003054 catalyst Substances 0.000 claims abstract description 18
- 230000005484 gravity Effects 0.000 claims description 27
- 239000000463 material Substances 0.000 claims description 27
- 239000006200 vaporizer Substances 0.000 claims description 25
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 18
- 239000003546 flue gas Substances 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 230000008676 import Effects 0.000 claims description 9
- 239000000126 substance Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 238000002407 reforming Methods 0.000 abstract description 3
- 239000002894 chemical waste Substances 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 239000000779 smoke Substances 0.000 abstract 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 238000006057 reforming reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 239000004576 sand Substances 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 239000002594 sorbent Substances 0.000 description 3
- 235000012255 calcium oxide Nutrition 0.000 description 2
- 239000000292 calcium oxide Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- QEVHRUUCFGRFIF-UHFFFAOYSA-N 6,18-dimethoxy-17-[oxo-(3,4,5-trimethoxyphenyl)methoxy]-1,3,11,12,14,15,16,17,18,19,20,21-dodecahydroyohimban-19-carboxylic acid methyl ester Chemical compound C1C2CN3CCC(C4=CC=C(OC)C=C4N4)=C4C3CC2C(C(=O)OC)C(OC)C1OC(=O)C1=CC(OC)=C(OC)C(OC)=C1 QEVHRUUCFGRFIF-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 101100533283 Dictyostelium discoideum serp gene Proteins 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000007158 vacuum pyrolysis Methods 0.000 description 1
- 230000035899 viability Effects 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention belongs to the technical field of chemical waste utilization and relates to an old automobile breaking residue catalytic gasification device which reforming steam in presence of a catalyst to produce hydrogen. In the device, a pyrolysis chamber is communicated with a combustion chamber through a semicoke returner, a spiral shovelling plate which is uniformly distributed is formed in the inner cavity of the pyrolysis chamber, a residue inlet is formed on one side of the bottom of the pyrolysis chamber, a pyrolysis gas outlet is formed on the same side on the top of the pyrolysis chamber, and the pyrolysis gas outlet is communicated with the bottom end of a gasification chamber through a compressed air pump, a first cyclone separator and a second high-temperature gas control valve, which are connected in series, the internal top part of the inner cavity in the gasification chamber is provided with a second cyclone separator and a high-hydrogen-content gas outlet, and the top end of the combustion of a combustion chamber has a controllable smoke outlet. The old automobile breaking residue catalytic gasification device is characterized by a simple overall structure, safe and reliable working principle, low manufacturing cost and long service life; and when used for pyrolysis treatment of automobile waste material, the device is environment-friendly, and has high yield rate and high economic value.
Description
Technical field:
The invention belongs to chemical waste and utilize technical field; Relate to a kind of catalytic gasification system and device, particularly a kind of junked-auto crushing residua catalytic gasification device with the catalyzer vapor reforming hydrogen production by vacuum tumbler formula pyrolysis reactor and fluidized-bed reactor combination.
Background technology:
At present, Hydrogen Energy is as a kind of cleaning, efficient, safety, the continuable energy, is regarded as one of the most potential energy in this century.Method through gasifying after the first pyrolysis is produced the approach that hydrogen is not only a kind of effective processing junked-auto plastics from the junked-auto crushing residua; And help the hydrogen energy source expanding economy; Through pyrolysis junked-auto crushing residua; Obtain the hydrocarbon polymer of different carbon chain, under catalyst action, make hydrogen again through the methane vapor reforming reaction.Adopt vacuum pyrolysis reactor to produce pyrolysis gas, improved pyrolysis gas concentration, help further gasification reaction than traditional method.In junked-auto crushing residua gasification, can pass through the adsorption forced hydrogen manufacturing of carbonic acid gas (SERP) technology, its principle is the CO that produces in the methane vapor reforming reaction process
2Remove with sorbent material, shown in (1)～(3), reaction (1) is thermo-negative reaction, and reaction (2) and (3) is thermopositive reaction.To obtain more H at a lower temperature
2, need from reactor drum, remove CO
2Thereby, break chemical reaction equilibrium, reduce reaction equilibrium constant, the gasification reaction temperature is reduced, thereby generate more H
2, make hydrogen production reaction condition milder, energy consumption lower.The key of the commercial viability research that this is technological is the high temperature CO that adopts in the methane vapor reforming reaction process
2The performance study of sorbent material, and quicklime has high CO
2Loading capacity is as high temperature CO
2Sorbent material.Therefore, can reduce the CO that generates in temperature of reaction and the ability absorption reaction
2New catalyst, can from junked-auto crushing residua catalytic gasification reaction process, obtain more hydrogen.
C+H
2O→CO+H
2(ΔH＞0) (1)
CO+H
2O→CO
2+H
2(ΔH＜0)(2)
CaO+CO
2→CaCO
3(ΔH＜0)(3)
The tradition gasification installation can not effectively be produced hydrogen from solid waste and fuel; And need under higher temperature, carry out; Energy consumption is higher; Therefore, seek to design the important technology content that a kind of catalytic gasification hydrogen production system employing reforming technology all has clear superiority at aspects such as energy consumption, transformation efficiency and hydrogen outputs equipment configuration is just becoming expert scholar's research and development.
Summary of the invention:
The objective of the invention is to overcome the shortcoming that prior art exists; Seek a kind of catalytic gasification system and device of designing and preparing; This system and device can be used for the pyrolysis of the catalytic gasification of junked-auto crushing residua, thereby produces hydrogen-rich synthetic gas, realizes the environment protection-type utilization of junked-auto.
To achieve these goals, agent structure of the present invention comprises pyrolysis chamber, combustion chamber, vaporizer, first internal cyclone separators, first preheating chamber, first gravity separator, semicoke returning charge ascent stage, semicoke returning charge horizontal section, semicoke returning charge downcomer, the first high-temperature gas valve, second preheating chamber, second gravity separator, second internal cyclone separators, semicoke material returning device, first exhanst gas outlet, second exhanst gas outlet, semicoke inlet, bottom, pyrolysis chamber inlet, catalyst inlet, pyrolysis gas outlet, high hydrogen richness pneumatic outlet, the second high-temperature gas valve, the import of junked-auto crushing residua, semicoke outlet, lime-ash outlet, spiral flight and air driven pump; And A is catalyzer, and B is a flue gas, and C is an inert support, and D is a pyrolysis gas, and E is a vaporized chemical, and F is a fluidizing agent, and G is the junked-auto crushing residua, and H is high hydrogen content gas, and I is a semicoke, and K is cindery trend or import and export; The semicoke outlet that one side of vacuum tumbler formula pyrolysis chamber is shaped on is communicated with the semicoke inlet of bottom, combustion chamber through the semicoke material returning device; Be shaped on equally distributed spiral flight in the inner chamber of pyrolysis chamber; Bottom one side of pyrolysis chamber is shaped on the import of junked-auto crushing residua; The homonymy at the top of pyrolysis chamber is shaped on the pyrolysis gas outlet, is communicated with the bottom of vaporizer behind air driven pump, first internal cyclone separators and the second high-temperature gas valve of pyrolysis gas outlet through serial connection; The semicoke material returning device comprises semicoke returning charge ascent stage, semicoke returning charge horizontal section and semicoke returning charge downcomer three segment pipes; Bottom, the pyrolysis chamber inlet that the top of pyrolysis chamber is shaped on is communicated with the top formula of ganging up of combustion chamber through first gravity separator, first preheating chamber and the first high-temperature gas valve; One side lower part of combustion chamber is shaped on the lime-ash outlet, and the top end of combustion chamber is communicated with the bottom catalyst inlet of vaporizer through the first high-temperature gas valve, second preheating chamber, second gravity separator of serial connection; The top is shaped on second internal cyclone separators and high hydrogen richness pneumatic outlet in the inner chamber of vaporizer; The top of combustion chamber is shaped on controllable type exhanst gas outlet B through the first high-temperature gas valve, is shaped on first exhanst gas outlet and second exhanst gas outlet on first gravity separator and second gravity separator respectively, and its function is identical with exhanst gas outlet B with structure.
The catalytic gasification device that the present invention relates to comprises vacuum tumbler formula pyrolysis chamber, three funtion parts of fluidised bed combustion chamber and fluidized-bed gasification chamber; The junked-auto crushing residua carries out pyrolytic reaction in the pyrolysis chamber, produce pyrolysis gas and semicoke; The semicoke that the pyrolysis chamber produces is sent into the combustion chamber after-flame through the semicoke material returning device that is arranged at the pyrolysis chamber, produces high-temperature gas and inert support and catalyst mix, is used for the preheating material; In the combustion chamber, the burn high-temperature flue gas that produces of semicoke enters into first, second preheating chamber respectively and carries out preheating after the first high-temperature gas valve is controlled the high-temperature flue gas flow, the material preheating is heated; Go out flue gas and inert support and catalyzer through gravity separation again, inert support is sent into the pyrolysis chamber, catalyzer is sent into vaporizer; The pyrolysis gas that the pyrolysis chamber of vacuum tumbler pyrolysis reactor structure produces is pumped into first cyclonic separator through placing the outside pressurized air in pyrolysis chamber, and the outlet and the vaporized chemical water vapour of warp first cyclonic separator feed vaporizer through the second high-temperature gas valve.
The present invention compared with prior art, its one-piece construction is simple, principle of work is safe and reliable, low cost of manufacture, long service life is applied to the pyrolysis processing of automobile waste materials, environmental friendliness, earning rate is high, economic worth obviously,
Description of drawings:
Fig. 1 is the structural principle synoptic diagram of apparatus of the present invention.
Embodiment:
Below through embodiment and combine accompanying drawing that the present invention is described further.
Embodiment:
The agent structure of present embodiment comprises pyrolysis chamber 1; Combustion chamber 2; Vaporizer 3; First internal cyclone separators 4; First preheating chamber 5; First gravity separator 6; The semicoke returning charge ascent stage 7; Semicoke returning charge horizontal section 8; Semicoke returning charge downcomer 9; The first high-temperature gas valve 10; Second preheating chamber 11; Second gravity separator 12; Second internal cyclone separators 13; Semicoke material returning device 14; First exhanst gas outlet 15; Second exhanst gas outlet 16; Semicoke inlet 17; Bottom, pyrolysis chamber inlet 18; Catalyst inlet 19; Pyrolysis gas outlet 20; High hydrogen richness pneumatic outlet 21; The second high-temperature gas valve 22; Junked-auto crushing residua import 23; Semicoke outlet 24; Lime-ash outlet 25; Spiral flight 26 and air driven pump 27; In addition, A is a catalyzer, and B is a flue gas, and C is an inert support, and D is a pyrolysis gas, and E is a vaporized chemical, and F is a fluidizing agent, and G is the junked-auto crushing residua, and H is high hydrogen content gas, and I is a semicoke, and K is cindery trend or import and export; The semicoke outlet 24 that one side of vacuum tumbler formula pyrolysis chamber 1 is shaped on is communicated with the semicoke inlet 17 of 2 bottoms, combustion chamber through semicoke material returning device 14; Be shaped on equally distributed spiral flight 26 in the inner chamber of pyrolysis chamber 1; Bottom one side of pyrolysis chamber 1 is shaped on junked-auto crushing residua import 23; The homonymy at the top of pyrolysis chamber 1 is shaped on pyrolysis gas outlet 20, and pyrolysis gas outlet 20 air driven pumps 27 through serial connection, first internal cyclone separators 4 and the second high-temperature gas valve, 22 backs are communicated with the bottom of vaporizer 3; Semicoke material returning device 14 comprises semicoke returning charge ascent stage 7, semicoke returning charge horizontal section 8 and semicoke returning charge downcomer 9 three segment pipes; Bottom, pyrolysis chamber that the top of pyrolysis chamber 1 is shaped on inlet 18 is communicated with the top formula of ganging up of combustion chamber 2 through first gravity separator 6, first preheating chamber 5 and the first high-temperature gas valve 10; One side lower part of combustion chamber 2 is shaped on lime-ash outlet 25, and the first high-temperature gas valve 10 of the top end of combustion chamber 2 through serial connection, second preheating chamber 11, second gravity separator 12 are communicated with the bottom catalyst inlet 19 of vaporizer 3; The top is shaped on second internal cyclone separators 13 and high hydrogen richness pneumatic outlet 21 in the inner chamber of vaporizer 3; The top of combustion chamber 2 is shaped on controllable type exhanst gas outlet B through the first high-temperature gas valve 10; Be shaped on first exhanst gas outlet 15 and second exhanst gas outlet 16 on first gravity separator 6 and second gravity separator 12 respectively, its function is identical with exhanst gas outlet B with structure.
The pyrolysis chamber 1 of present embodiment is a vacuum tumbler formula pyrolysis reactor structure, and pyrolytic reaction takes place in pyrolysis chamber 1 the junked-auto crushing residua, produces pyrolysis gas D and semicoke I, and the semicoke I that pyrolysis chamber 1 produces sends into combustion chamber 2 bottom after-flames through semicoke material returning device 14; The high-temperature flue gas B that combustion chamber 2 produces is divided into three parts through the first high-temperature gas valve 10; First part feeds first preheating chamber 5 and mixes the back with inert support C and get into first gravity separator 6 and carry out gas solid separation; Flue gas gets into follow-up waste heat boiler from first exhanst gas outlet 15 of first gravity separator 6, the rare gas element C of the preheating 18 entering pyrolysis chambers 1 that enter the mouth through the bottom, pyrolysis chamber; Second section mixes back entering second gravity separator 12 through second preheating chamber 11 and carries out gas solid separation with catalyst A; Second exhanst gas outlet 16 emptyings of flue gas on second gravity separator 12, catalyzer get into vaporizer 3 through the catalyst inlet 19 of vaporizer 3 bottoms again; Third part directly gets into follow-up waste heat boiler; The pyrolysis gas D string that pyrolysis chamber 1 produces is through first cyclonic separator 4 mixes through the second high-temperature gas valve, 22 entering vaporizers 3 with vaporized chemical E in.
The flue gas heat of carrying out the combustion reactions generation in the combustion chamber 2 of present embodiment is higher; Arrange heating surface in residing first preheating chamber 5 of material and second preheating chamber 11; To absorb heat from high-temperature flue gas; Need not all high-temperature flue gas are used for the preheating material, can discharge most of flue gas and be used for other device heat supply; The semicoke that produces in the pyrolysis chamber 1 is sent into combustion chamber 2 after-flames, can effectively improve junked-auto crushing residua utilization ratio; The pyrolysis gas that pyrolysis chamber 1 produces gets into vaporizer 3, issues the reaction of unboiled water steam catalytic gasification in the effect of catalyzer, makes high hydrogen content synthetic gas.
The junked-auto material of present embodiment carries out pyrolytic reaction in pyrolysis chamber 1, produce pyrolysis gas D and semicoke I; The semicoke I high-temperature flue gas B that produces that in combustion chamber 2, burns gets into first and second preheating chambers 5 and 11 respectively, and is respectively inert support silica sand C and catalyst A provides heat; Through first and second gravity separator 6 and 12, isolate flue gas B and silica sand C and catalyst A again, respectively silica sand C is sent into pyrolysis chamber 1, catalyst A is sent into vaporizer 3; Pyrolysis chamber 1 is a vacuum tumbler formula pyrolysis reactor structure, and the pyrolysis gas D of generation feeds vaporizer 3 with vaporized chemical water vapour E through the second high-temperature gas valve 22 through first cyclonic separator 4; The semicoke I that pyrolysis chamber 1 produces sends into combustion chamber 2 bottom after-flames through semicoke material returning device 14; Combustion chamber 2 is the bubbling fluidization bed structure, and the bottom feeds fluidizing agent air F; Vaporizer 3 is the turbulent fluidized bed structure, under the effect of catalyst A, makes pyrolysis gas generation reforming reaction produce high hydrogen content synthetic gas H.
The access structure of the gentle material of material of present embodiment is: pyrolysis chamber 1 communicates with semicoke material returning device 14; Semicoke material returning device 14 communicates with 2 bottoms, combustion chamber; First gravity separator 6 communicates with 1 bottom, pyrolysis chamber; Second gravity separator 12 communicates with vaporizer 3 bottoms, and the pyrolysis gas that pyrolysis chamber 1 produces mixes feeding vaporizer 3 through the second high-temperature gas valve 22 with vaporized chemical E; Be shaped on the junked-auto crushing residua import 23 and semicoke material returning device 14 of open type structure on the sidewall of pyrolysis chamber 1; Semicoke material returning device 14 is made up of semicoke returning charge ascent stage 7, semicoke returning charge horizontal section 8 and semicoke returning charge downcomer 9 communication type successively; Semicoke returning charge ascent stage 7, semicoke returning charge horizontal section 8 and semicoke returning charge downcomer 9 bottoms feed the adjustable fluidizing agent of flow respectively, and semicoke returning charge downcomer 9 is communicated with the semicoke inlet 17 of 2 bottoms, combustion chamber; Vaporizer 3 bottoms are shaped on catalyst inlet 19; All be furnished with heating surface in residing first and second preheating chambers 5 of material and 11, to absorb heat from high-temperature flue gas.
Claims (2)
1. junked-auto crushing residua catalytic gasification device; Comprise pyrolysis chamber, combustion chamber, vaporizer, first internal cyclone separators, first preheating chamber, first gravity separator, semicoke returning charge ascent stage, semicoke returning charge horizontal section, semicoke returning charge downcomer, the first high-temperature gas valve, second preheating chamber, second gravity separator, second internal cyclone separators, semicoke material returning device, first exhanst gas outlet, second exhanst gas outlet, semicoke inlet, bottom, pyrolysis chamber inlet, catalyst inlet, pyrolysis gas outlet, high hydrogen richness pneumatic outlet, the second high-temperature gas valve, the import of junked-auto crushing residua, semicoke outlet, lime-ash outlet, spiral flight and air driven pump; It is characterized in that the semicoke outlet that vacuum tumbler formula pyrolysis chamber one side is shaped on is communicated with the semicoke inlet of bottom, combustion chamber through the semicoke material returning device; Be shaped on equally distributed spiral flight in the inner chamber of pyrolysis chamber; Bottom one side of pyrolysis chamber is shaped on the import of junked-auto crushing residua; The homonymy at the top of pyrolysis chamber is shaped on the pyrolysis gas outlet, is communicated with the bottom of vaporizer behind air driven pump, first internal cyclone separators and the second high-temperature gas valve of pyrolysis gas outlet through serial connection; The semicoke material returning device comprises semicoke returning charge ascent stage, semicoke returning charge horizontal section and semicoke returning charge downcomer three segment pipes; Bottom, the pyrolysis chamber inlet that top, pyrolysis chamber is shaped on is communicated with the top formula of ganging up of combustion chamber through first gravity separator, first preheating chamber and the first high-temperature gas valve; Combustion chamber one side lower part is shaped on the lime-ash outlet, and the top end of combustion chamber is communicated with the bottom catalyst inlet of vaporizer through the first high-temperature gas valve, second preheating chamber, second gravity separator of serial connection; The top is shaped on second internal cyclone separators and high hydrogen richness pneumatic outlet in the inner chamber of vaporizer; The top of combustion chamber is shaped on the controllable type exhanst gas outlet through the first high-temperature gas valve, is shaped on first exhanst gas outlet and second exhanst gas outlet on first gravity separator and second gravity separator respectively, and its function is identical with exhanst gas outlet with structure.
2. junked-auto crushing residua catalytic gasification device according to claim 1 is characterized in that the junked-auto crushing residua carries out pyrolytic reaction in the pyrolysis chamber, produces pyrolysis gas and semicoke; The semicoke that the pyrolysis chamber produces is sent into the combustion chamber after-flame through the semicoke material returning device that is arranged at the pyrolysis chamber, produces high-temperature gas and inert support and catalyst mix, is used for the preheating material; In the combustion chamber, the burn high-temperature flue gas that produces of semicoke enters into first, second preheating chamber respectively and carries out preheating after the first high-temperature gas valve is controlled the high-temperature flue gas flow, the material preheating is heated; Go out flue gas and inert support and catalyzer through gravity separation again, inert support is sent into the pyrolysis chamber, catalyzer is sent into vaporizer; The pyrolysis gas that the pyrolysis chamber of vacuum tumbler pyrolysis reactor structure produces is pumped into first cyclonic separator through placing the outside pressurized air in pyrolysis chamber, and the outlet and the vaporized chemical water vapour of warp first cyclonic separator feed vaporizer through the second high-temperature gas valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103189740A CN102433165A (en) | 2011-10-19 | 2011-10-19 | Old automobile breaking residue catalytic gasification device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011103189740A CN102433165A (en) | 2011-10-19 | 2011-10-19 | Old automobile breaking residue catalytic gasification device |
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|---|---|
| CN102433165A true CN102433165A (en) | 2012-05-02 |
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|---|---|---|---|
| CN2011103189740A Pending CN102433165A (en) | 2011-10-19 | 2011-10-19 | Old automobile breaking residue catalytic gasification device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103468322A (en) * | 2013-07-25 | 2013-12-25 | 易高环保能源研究院有限公司 | Preparation method for hydrogen-rich gas through steam gasification of solid organic matter |
| CN103923705A (en) * | 2014-03-25 | 2014-07-16 | 东南大学 | Device and method for preparing hydrogen-rich gas by gasifying biomass |
| CN107674695A (en) * | 2017-11-16 | 2018-02-09 | 山西易通环能科技集团有限公司 | A kind of worn-out agricultural film plastics pyrolysis oven |
| CN108315027A (en) * | 2018-02-11 | 2018-07-24 | 武汉凯迪工程技术研究总院有限公司 | Carbon containing biomass material carbonizes powder integral method processed and its system |
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| CN1376188A (en) * | 1999-09-24 | 2002-10-23 | 米伦两合公司 | Method for gasifying organic materials and mixtures of materials |
| CN101045524A (en) * | 2007-05-04 | 2007-10-03 | 大连理工大学 | Method for preparing hydrogen-riched gas by solid fuel catalytic gasification |
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2011
- 2011-10-19 CN CN2011103189740A patent/CN102433165A/en active Pending
Patent Citations (3)
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|---|---|---|---|---|
| WO1979000687A1 (en) * | 1978-03-02 | 1979-09-20 | O Lindstroem | Means and procedure for gasification of solid fuels |
| CN1376188A (en) * | 1999-09-24 | 2002-10-23 | 米伦两合公司 | Method for gasifying organic materials and mixtures of materials |
| CN101045524A (en) * | 2007-05-04 | 2007-10-03 | 大连理工大学 | Method for preparing hydrogen-riched gas by solid fuel catalytic gasification |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103468322A (en) * | 2013-07-25 | 2013-12-25 | 易高环保能源研究院有限公司 | Preparation method for hydrogen-rich gas through steam gasification of solid organic matter |
| WO2015010448A1 (en) * | 2013-07-25 | 2015-01-29 | 易高环保能源研究院有限公司 | Method for preparing hydrogen-rich gas by gasification of solid organic substance and steam |
| CN103468322B (en) * | 2013-07-25 | 2015-08-12 | 易高环保能源研究院有限公司 | A kind of method being produced hydrogen-rich gas by solid organic matters steam gasification |
| US9809770B2 (en) | 2013-07-25 | 2017-11-07 | Eco Environmental Energy Research Institute Limited | Method for preparing hydrogen-rich gas by gasification of solid organic substance and steam |
| CN103923705A (en) * | 2014-03-25 | 2014-07-16 | 东南大学 | Device and method for preparing hydrogen-rich gas by gasifying biomass |
| CN103923705B (en) * | 2014-03-25 | 2016-01-06 | 东南大学 | Gasifying biomass produces the device and method of hydrogen-rich gas |
| CN107674695A (en) * | 2017-11-16 | 2018-02-09 | 山西易通环能科技集团有限公司 | A kind of worn-out agricultural film plastics pyrolysis oven |
| CN108315027A (en) * | 2018-02-11 | 2018-07-24 | 武汉凯迪工程技术研究总院有限公司 | Carbon containing biomass material carbonizes powder integral method processed and its system |
| CN108315027B (en) * | 2018-02-11 | 2023-10-24 | 武汉凯迪工程技术研究总院有限公司 | Carbonization and pulverization integrated method and system for carbonaceous biomass material |
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