CN101481619A - Self-mixing downflow fluidized bed rapid pyrolysis process for solid organics - Google Patents
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- CN101481619A CN101481619A CNA2008100006159A CN200810000615A CN101481619A CN 101481619 A CN101481619 A CN 101481619A CN A2008100006159 A CNA2008100006159 A CN A2008100006159A CN 200810000615 A CN200810000615 A CN 200810000615A CN 101481619 A CN101481619 A CN 101481619A
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- 239000007787 solid Substances 0.000 title claims abstract description 42
- 238000002156 mixing Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000000197 pyrolysis Methods 0.000 title claims description 25
- 230000008929 regeneration Effects 0.000 claims abstract description 14
- 238000011069 regeneration method Methods 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 239000000969 carrier Substances 0.000 claims abstract description 6
- 230000008878 coupling Effects 0.000 claims abstract description 6
- 238000010168 coupling process Methods 0.000 claims abstract description 6
- 238000005859 coupling reaction Methods 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 7
- 235000010627 Phaseolus vulgaris Nutrition 0.000 claims description 6
- 244000046052 Phaseolus vulgaris Species 0.000 claims description 6
- 235000012149 noodles Nutrition 0.000 claims description 6
- 238000010298 pulverizing process Methods 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 239000012071 phase Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 239000003546 flue gas Substances 0.000 claims description 3
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- 239000011859 microparticle Substances 0.000 claims description 3
- 239000000376 reactant Substances 0.000 claims description 3
- 239000007790 solid phase Substances 0.000 claims description 3
- 238000005979 thermal decomposition reaction Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000001149 thermolysis Methods 0.000 abstract 2
- 239000005416 organic matter Substances 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 6
- 239000002028 Biomass Substances 0.000 description 4
- 241000273930 Brevoortia tyrannus Species 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 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 1
- 238000002679 ablation Methods 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 208000012839 conversion disease Diseases 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000013502 plastic waste Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000010517 secondary reaction Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000007158 vacuum pyrolysis Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Processing Of Solid Wastes (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a solid organic matter self-mixing descending fluidized bed fast thermolysis technique. A reaction regeneration cycle system is formed by leading fast thermolysis and scorch to be carried out in different systems and circularly coupling solid heat carriers, thus ensuring pyrolytic reaction to be carried out continuously and the regenerated heat to be reasonably utilized; furthermore, pyrolytic gas and oil with high quality can be produced, so that the resource utilization rate is improved. The invention mainly comprises a self-mixing descending reactor, a fluidized bed reactivator, etc.
Description
1. technical field
The invention provides a kind of solid organic matters self-mixing downflow fluidized bed rapid pyrolysis process, belong to the renewable energy source domain.
2. background technology
Raising along with people's living standard and quality, organic content in the municipal wastes raises gradually, bury processing and can not satisfy environmental protection requirement, burn decrement treatment and can not produce the nuisance that resembles dioxin, the focus that municipal wastes is called people's research and explores is handled on safety economy ground; The rural area straw belongs to renewable resources, existing existing technology with its gasification gas making comprehensive utilization, but because pyrolysis and aerobic burning are finished at same system, and pyrolysis gas calorific value is low, and 4000 kilocalories/m3 is only arranged, improve pyrolysis makings amount and studied focus by people; The pyrolysis of various plastic waste has become people and has utilized waste gas resources effective means, but prior art belongs to periodical operation mostly, and pyrolysis purpose product yield is low, and the pyrolytic gasification of coal also is that coal effectively utilizes one of means in addition, but existing complex process equipment, efficient is low.
Produce in the various technologies of liquid fuel at the solid organic matters fast pyrogenation, reactor all is its core because the type of reactor and type of heating thereof be chosen in the final distribution that has determined product to a great extent.So the selection of type of reactor and the selection of type of heating are the key links of various technological lines.The reactor kind of present domestic and international exploitation is a lot, has formed different technology, mainly is divided into following several types:
(1) mechanical contact formula reactor process, the common ground of this class reactor are directly or indirectly to contact with biomass by a scorching hot reactor surface, with the heat transferred biomass, it are heated up at a high speed, thereby reach fast pyrogenation.The heat transfer mode that it adopts is mainly thermal conduction, and reactor etc. is bored in common have ablation pyrolysis reactor, silk screen pyrolysis reactor, rotation.The problem that the moving portion of cinder wear equipment and equipment broke down easily and is difficult to the industrialization amplification when but also there was high temperature in mechanical means.
(2) indirect type reactor process, the principal character of this class reactor are institute's heat requirements that biomass pyrolytic is provided by a pyritous surface or thermal source, and it mainly carries out the heat transmission by thermal radiation, and common thermobalance can belong to this type of.As laboratory study equipment, be difficult to industrialization and amplify.
(3) mixing reactor technology, mixing reactor mainly is by hot gas flow or gas-solid multiphase flow biomass to be carried out rapid heating, the mode that plays leading heat transmission is mainly convective heat exchange, but thermal radiation and thermal conduction also be can not ignore, and common have fluidized-bed reactor, injection bed bioreactor, a circulating fluid bed reactor etc. fast.Wherein, circulating fluidized bed device transforms because of solving heat, realizes the heat self-sufficiency, satisfies fast pyrogenation well the requirement of temperature and temperature rise rate is widely adopted.Being used for commercial off-the-shelf at present has only from carrying bed and circulating fluidized bed system.But because existing installation agriculture and forestry organic waste material particle uses carrier gas with the solid needs that mix of thermal barrier, thermo-efficiency is lower, will strengthen cost of investment and operation difficulty during practical application.
(4) vacuum pyrolysis reactor technology, biological particles enters between the thermostat metal plate that is sent to two levels behind the reactor and is subjected to pyrolysis, the volatile matter that cracking produces relies on the very fast quilt of vacuum state of reactor to take reactor out of, be directly inputted to two condenser systems, collect heavy oil for one, collect light oil and moisture for one.This system's biggest advantage is, vacuum split product next time can very fast disengaging reactor, thereby reduced the probability of secondary reaction, but needed the normal operation of vacuum pump and the fabulous stopping property of reactor to guarantee, and this will strengthen cost of investment and operation difficulty when practical application.
3. summary of the invention
Purpose of the present invention is exactly to provide a kind of solid organic matters self-mixing downflow fluidized bed rapid pyrolysis process for the deficiency that overcomes the prior art existence.This advantages of simple technological process, heat recuperation rate height, temperature of reaction system lower (close) with liquid phase method, be easy to control, the catalyst dust that gas phase is carried secretly removes rationally, is easy to big industrialization, and reaction conversion ratio and selectivity height are easy to large-scale industrial production.
Technical scheme of the present invention:
Mainly burn respectively and carry out, and, form a reaction regeneration coupling circulation system by solid thermal carriers circulation coupling in different system by solid organic matters fast pyrogenation and solid thermal carriers.Solid organic matters after the drying and crushing is through delivering into the inlet of self-mixing downflow fluidized bed reactor by worm conveyor, contact, mix, react self-mixing downflow fluidized bed reactor with the high temperature regeneration agent that speaks into from another inlet, leave conversion zone fast; It is pyrolysis oil and pyrolysis gas that the gaseous phase outlet of gas phase by self-mixing downflow fluidized bed reactor enters the quencher condensation separation, separates through oil tank, and partial thermal decomposition oil is returned water cooler cooling back as the quencher low-temperature receiver by liquid circulating pump; Solid phase enters fluid bed regenerator burning regeneration together by fluidized-bed material returning device and preheated air, solid temperature after fluidized-bed regeneration raises, enter the inertia gas-solid separator, tell most of granular solids earlier and enter the regenerator surge bunker, entering self-mixing downflow fluidized bed reactor again circulates once more, all the other small solids are introduced into the economizer preheated air with air-flow, enter cyclone separator then and tell the microparticle high-temp solid and efflux; Flue gas after the separation enters the dry lifter of organism dried bean noodles by pulverizing feeder, isolates the exsiccant organism after the induced draft fan emptying through cyclone separator then; Air enters through gas blower that the economizer preheating is laggard goes into fluid bed regenerator; Organism enters the dry lifter of organism dried bean noodles by pulverizing feeder, separate the inlet that delivers into self-mixing downflow fluidized bed reactor by worm conveyor through cyclone separator then, self-mixing downflow fluidized bed like this reactor and fluid bed regenerator coupling form a solid thermal carriers round-robin reaction regeneration coupled system.
Self-mixing downflow fluidized bed reactor is a kind of dependence gravity, need the blended solid in the process that falls by reactor in the fixed vent diverter repeatedly disperse the interflow fast, thereby form the downflow fluidized bed of the reactant system that mixes.
4, description of drawings
Accompanying drawing is a process flow sheet of the present invention.
Wherein: 1. fluid bed regenerator 2. inertia gas-solid separators 3. economizers 4. cyclone separators 5. self-mixing downflow fluidized bed reactor 6. quenchers 7. fluidized-bed material returning devices 8. regenerator surge bunkers 9. gas blowers 10. worm conveyors 11. induced draft fans 12. are pulverized feeder 13. dry lifter 14. cyclone separators 15. oil tanks 16. liquid circulating pumps.
5. embodiment
The present invention will be described in detail below in conjunction with accompanying drawing: in actual design with in making, the present invention be with by the solid organic matters after the drying and crushing through deliver into inlet by worm conveyor (10) from the descending reactor of mixed fluidized bed (5), contact, mix, react self-mixing downflow fluidized bed reactor (5) with the high temperature regeneration agent that enters from another inlet, leave conversion zone fast; It is pyrolysis oil and pyrolysis gas that the gaseous phase outlet of gas phase by self-mixing downflow fluidized bed reactor (5) enters quencher (6) condensation separation, separate through oil tank (15), partial thermal decomposition oil is returned water cooler (17) cooling back as quencher (6) low-temperature receiver by liquid circulating pump (16); Solid phase enters fluid bed regenerator (1) burning regeneration together by fluidized-bed material returning device (7) and preheated air, solid temperature after fluidized-bed regeneration raises, enter inertia gas-solid separator (2), tell most of granular solids earlier and enter regenerator surge bunker (8), entering self-mixing downflow fluidized bed reactor (5) again circulates once more, all the other small solids are introduced into economizer (3) preheated air with air-flow, enter cyclone separator (4) then and tell the microparticle high-temp solid and efflux; Flue gas after the separation enters the dry lifter of organism dried bean noodles (13) by pulverizing feeder (12), isolates the exsiccant organism after induced draft fan (11) emptying through cyclone separator (14) then; Air enters through gas blower (9) that economizer (3) preheating is laggard goes into fluid bed regenerator (1); Organism enters the dry lifter of organism dried bean noodles (13) by pulverizing feeder (12), separate the inlet that delivers into self-mixing downflow fluidized bed reactor (5) by worm conveyor (10) through cyclone separator (14) then, self-mixing downflow fluidized bed like this reactor (5) and fluid bed regenerator (1) coupling form a solid thermal carriers round-robin reaction regeneration coupled system.
Self-mixing downflow fluidized bed reactor (5) is a kind of dependence gravity, need the blended solid in the process that falls by reactor in the fixed vent diverter repeatedly disperse the interflow fast, thereby form the downflow fluidized bed of the reactant system that mixes.
The present invention has the following advantages:
1. pyrolysis efficient height is the 3. gentle quality height of pyrolysis oil of pyrolysis G﹠O yield height 2., and wherein the pyrolysis gas calorific value has improved 2-3 times of 4. dresses Install meter rationally, realized that 5. self thermal cycle balance install multiple spot and annotate oxygen, Strength regenerate peculiarity is big, has increased substantially disposal ability and has 6. supported Source utilization rate height has been eliminated environmental pollution simultaneously.
Claims (3)
1. the invention provides a kind of solid organic matters self-mixing downflow fluidized bed rapid pyrolysis process, it is characterized in that solid organic matters after the drying and crushing is through delivering into the inlet of self-mixing downflow fluidized bed reactor by worm conveyor, contact, mix, react self-mixing downflow fluidized bed reactor with the high temperature regeneration agent that enters from another inlet, leave conversion zone fast; It is pyrolysis oil and pyrolysis gas that the gaseous phase outlet of gas phase by self-mixing downflow fluidized bed reactor enters the quencher condensation separation, separates through oil tank, and partial thermal decomposition oil is returned water cooler cooling back as the quencher low-temperature receiver by liquid circulating pump; Solid phase enters fluid bed regenerator burning regeneration together by fluidized-bed material returning device and preheated air, solid temperature after fluidized-bed regeneration raises, enter the inertia gas-solid separator, tell most of granular solids earlier and enter the regenerator surge bunker, entering self-mixing downflow fluidized bed reactor again circulates once more, all the other small solids are introduced into the economizer preheated air with air-flow, enter cyclone separator then and tell the microparticle high-temp solid and efflux; Flue gas after the separation enters the dry lifter of organism dried bean noodles by pulverizing feeder, isolates the exsiccant organism after the induced draft fan emptying through cyclone separator then; Air enters through gas blower that the economizer preheating is laggard goes into fluid bed regenerator; Organism enters the dry lifter of organism dried bean noodles by pulverizing feeder, separate the inlet that delivers into self-mixing downflow fluidized bed reactor by worm conveyor through cyclone separator then, descending like this from mixed fluidized bed reactor and fluid bed regenerator coupling, form a solid thermal carriers round-robin reaction regeneration coupled system.
2. a kind of solid organic matters self-mixing downflow fluidized bed rapid pyrolysis process according to claim 1 is characterized in that the fluid bed regenerator gas solid separation adopts two-stage to separate, and the first step is the inertia gas-solid separator, and the second stage is cyclonic separator.
3. a kind of solid organic matters self-mixing downflow fluidized bed rapid pyrolysis process according to claim 1, it is characterized in that self-mixing downflow fluidized bed is a kind of dependence gravity, need the blended solid in the process that falls by reactor in the fixed vent diverter repeatedly disperse the interflow fast, thereby form the downflow fluidized bed of the reactant system that mixes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200810000615A CN101481619B (en) | 2008-01-11 | 2008-01-11 | Self-mixing downflow fluidized bed rapid pyrolysis process for solid organics |
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| CN200810000615A CN101481619B (en) | 2008-01-11 | 2008-01-11 | Self-mixing downflow fluidized bed rapid pyrolysis process for solid organics |
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| Publication Number | Publication Date |
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| CN101481619A true CN101481619A (en) | 2009-07-15 |
| CN101481619B CN101481619B (en) | 2012-10-17 |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104692607A (en) * | 2015-03-17 | 2015-06-10 | 东南大学 | Oil sludge pyrolysis resource utilization method and device |
| CN106247342A (en) * | 2016-09-30 | 2016-12-21 | 上海垒锦环境科技中心 | Coal and house refuse coupling combustion system |
| CN108397773A (en) * | 2018-03-02 | 2018-08-14 | 农业部规划设计研究院 | A kind of mixed combustion equipment of biomass pyrolytic oil gas |
| CN109456787A (en) * | 2018-08-08 | 2019-03-12 | 葫芦岛市锦隆石化高科技有限责任公司 | A kind of waste tire processing unit and processing method |
| US10487266B1 (en) | 2018-12-10 | 2019-11-26 | China University Of Petroleum (East China) | Polygeneration method of biomass downflow circulation bed millisecond pyrolysis liquefaction-gasification coupling |
| CN111088057A (en) * | 2019-12-27 | 2020-05-01 | 青岛惠城环保科技股份有限公司 | Method for producing hydrogen by using waste plastics to produce oil |
| CN112940765A (en) * | 2021-02-07 | 2021-06-11 | 四川大学 | System for biomass non-phase change drying coupled downer pyrolysis |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2511878Y (en) * | 2001-11-05 | 2002-09-18 | 田原宇 | Continuous-operation pyrolytic apparatus for solid organics |
| CN1847364A (en) * | 2006-04-30 | 2006-10-18 | 大连理工大学 | Method of pyrolyzing thermoset carrier in circular fluidizing bed and rotary kiln |
-
2008
- 2008-01-11 CN CN200810000615A patent/CN101481619B/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104692607A (en) * | 2015-03-17 | 2015-06-10 | 东南大学 | Oil sludge pyrolysis resource utilization method and device |
| CN104692607B (en) * | 2015-03-17 | 2016-08-24 | 东南大学 | A kind of greasy filth pyrolysis resource utilization method and device |
| CN106247342A (en) * | 2016-09-30 | 2016-12-21 | 上海垒锦环境科技中心 | Coal and house refuse coupling combustion system |
| CN108397773A (en) * | 2018-03-02 | 2018-08-14 | 农业部规划设计研究院 | A kind of mixed combustion equipment of biomass pyrolytic oil gas |
| CN109456787A (en) * | 2018-08-08 | 2019-03-12 | 葫芦岛市锦隆石化高科技有限责任公司 | A kind of waste tire processing unit and processing method |
| US10487266B1 (en) | 2018-12-10 | 2019-11-26 | China University Of Petroleum (East China) | Polygeneration method of biomass downflow circulation bed millisecond pyrolysis liquefaction-gasification coupling |
| CN111088057A (en) * | 2019-12-27 | 2020-05-01 | 青岛惠城环保科技股份有限公司 | Method for producing hydrogen by using waste plastics to produce oil |
| CN112940765A (en) * | 2021-02-07 | 2021-06-11 | 四川大学 | System for biomass non-phase change drying coupled downer pyrolysis |
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| CN101481619B (en) | 2012-10-17 |
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