CN201473491U - Biomass fast thermal decomposition device - Google Patents
Biomass fast thermal decomposition device Download PDFInfo
- Publication number
- CN201473491U CN201473491U CN2009202342915U CN200920234291U CN201473491U CN 201473491 U CN201473491 U CN 201473491U CN 2009202342915 U CN2009202342915 U CN 2009202342915U CN 200920234291 U CN200920234291 U CN 200920234291U CN 201473491 U CN201473491 U CN 201473491U
- Authority
- CN
- China
- Prior art keywords
- condenser
- stage
- gas
- fluidized bed
- thermal decomposition
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
A biomass fast thermal decomposition device comprises a combined feeding system, a carrier gas preheating system, a spray fluidized bed fast thermal decomposition reactor, a gas-solid separating and coke collecting system, a fractional condensation system and a thermal decomposition tail gas circulation system. The device uses the combined feeding system to send biomass material into the spray fluidized bed fast thermal decomposition reactor, while carrier gas enters the spray fluidized bed fast thermal decomposition reactor after being heated by the carrier gas preheating system so as to lead drastic heat transfer and mass transfer process to occur in the reactor; the biomass material quickly splits after being heated and generates volatile and coke; the volatile, the coke and the carrier gas enter the fractional condensation system after coke particles are removed by the gas-solid separating and coke collecting system; and under the action of a condensation manner combining direct method and indirect method, the condensable part of the biomass material is sufficiently condensed into bio-oil. Part of thermal decomposition tail gas is discharged into the air after processing, and other parts thereof respectively enter the carrier gas preheating system after being cleaned by a tail gas cleaner and pressurized by a compressor in the thermal decomposition tail gas circulation system.
Description
Technical field
The utility model relates to Power Engineering and Engineering Thermophysics specialty field of renewable energy resource utilization.
Background technology
The agriculture and forestry organic waste material amount of the annual output of China is considerable, is example with modal byproduct stalk in the farm crop production system, and annual production in 2010 is estimated to reach 7.26 hundred million tons, is equivalent to 3.5 hundred million tons of standard coals.The use of stalk at present mainly in animal feed and life in the countryside with can two broad aspect, wherein stalk is used for life in the countryside and accounts for 45% with the ratio of energy.In addition, Chinese annual yule logs amount is also considerable.According to the limit of forest harvesting the Eleventh Five-Year Plan period of State Council approved, the whole nation annual felling index is 2.48 billion cubic meters, is converted into biomass and is about 2.91 hundred million tons, can produce 1.09 hundred million tons of logging residue biomasss every year.Therefore, efficiently utilize agriculture and forestry organic waste material such as stalk for solving the rural area with can problem significant.Agriculture and forestry organic waste material is a kind of Energy resources of cleaning because its sulfur-bearing and ash amount are all less simultaneously.In addition, because the CO of a large amount of dischargings
2Constantly accumulation and cause " Greenhouse effect " caused negative impact also to cause the great attention of countries in the world, wherein 80% CO in atmospheric layer
2Quantity discharged is closely-related with the burning of fossil oil.And agriculture and forestry organic waste material has CO
2The characteristics of zero release can effectively be alleviated serious day by day " Greenhouse effect ", this for China as second-biggest-in-the-world CO
2Discharging big country has more significance.
Current, the Energy conversion that relates to agriculture and forestry organic waste material utilizes technology a lot, and direct burning, thermochemistry conversion, biochemical conversion etc. are roughly arranged.Wherein, fast pyrolysis technology is in inert atmosphere and moderate temperature (400～600 ℃), high heating rate (10
3～10
4℃/s) and lose heart the phase residence time that (under＜2s) the condition, biomass are subjected to thermo-cracking fast, the fugitive constituent of generation obtains the technology of bio oil through rapid condensation.It can be converted into easy storage, easily transportation, energy density height and bio oil easy to use with agriculture and forestry organic waste material with the mode of production of successive technology and batch production.The bio oil that obtains not only can be directly used in burning, and can also can therefrom extract the Chemicals with commercial value by further being processed as the power fuel of alternative diesel oil or gasoline.Therefore, the biomass fast pyrogenation technical study has obtained the great attention of countries in the world.States such as Canada, the U.S., Australia have begun the commercialized running of biomass fast pyrogenation, and it is 200 tons biomass fast pyrogenation factory that wherein Canadian Dynamotive company has built up day output.At present, domestic Southeast China University, Chinese University of Science and Technology, Zhejiang University, East China University of Science, Guangzhou energy institute of the Chinese Academy of Sciences, Shandong Technology Univ, Anhui Yineng Biologic energy Co., Ltd. etc. are all in the exploitation of carrying out the biomass fast pyrogenation technology one after another.
Summary of the invention
Technical problem: the purpose of this utility model provides a kind of biomass fast pyrogenation device, solves many-sided problem that present biomass fast pyrogenation technology exists:
(1) how little, the easy bridge formation of biomass material tap density guarantees that the stability and the continuity of feeding in raw material are problem demanding prompt solutions.
(2) biomass fast pyrogenation need satisfy high heating rate, good heat transfer effect and the requirement of the residence time mutually of losing heart.Mechanical type pyrolysis reactor equipment is huge in the existing technology, and operation expense is higher.The limitations restrict of indirect type reactor thermal source its mass-producing use.
(3) the direct spray condensation of generally adopting at present can realize the rapid condensation of hot pyrolysis gas, and is very effective to the wide boiling point mixture that the condensation bio oil is such.But the biology that only uses directly spray condensation to obtain is quite complicated by component, and the fuel quality of bio oil can't improve, and has also increased technology difficulty and the economy of extracting Chemicals from bio oil simultaneously.
(4) the carrier gas demand of hybrid pyrolysis reactor is big, and the tail gas of biomass fast pyrogenation generation simultaneously can cause secondary pollution to environment, the problem of therefore need to be resolved hurrily carrier gas source and tail gas pollution.
Technical scheme: the utility model comprises built-up type charging system, carrier gas pre-heating system, spouted fluidized bed fast pyrolysis reactor, gas solid separation and charcoal gathering system, fractional condensation system and pyrolysis exhaust gas circulation system.This device is sent into biomass material in the spouted fluidized bed fast pyrolysis reactor with the built-up type charging system, and carrier gas enters the spouted fluidized bed fast pyrolysis reactor after the heating of carrier gas pre-heating system, make violent heat and mass transfer process takes place in the reactor, biomass material is subjected to thermo-cracking rapidly, produce volatile matter and coke, volatile matter, coke and carrier gas enter the fractional condensation system together behind gas solid separation and charcoal gathering system removal coke granule, under the condensing mode effect that directly combines indirectly, its condensable part fully is condensed into bio oil.The treated atmosphere that enters of the part of pyrolysis tail gas, another part then through after cleaning of tail gas clearer and the compressor boost in the pyrolysis exhaust gas circulation system, enter the carrier gas pre-heating system respectively as carrier gas and burner aid burning.
Biomass spouted fluidized bed pyrolysis fractional condensation is produced the bio oil device and is comprised charging system, fast pyrolysis reactor, condenser system, pyrolysis exhaust gas circulation system and heating system, wherein,
In the charging system: the built-in mechanical arch breaking apparatus of feed bin, connect first step screw feeder under the feed bin, the end of first step screw feeder connects second stage screw feeder by vertical pipeline, another termination spouted fluidized bed fast pyrolysis reactor of second stage screw feeder, water cold sleeve is coated on second stage screw feeder and spouted fluidized bed fast pyrolysis reactor connection portion;
The spouted fluidized bed fast pyrolysis reactor connects spouted wind inlet, fluidized wind inlet, first step cyclonic separator respectively, and connects burner through the indirect heating chuck; First step cyclonic separator bottom connects first step collection charcoal case, and first step cyclonic separator top and second stage cyclonic separator join, and the top outlet and the bottom of second stage cyclonic separator connect first step condenser below side inlet and second stage collection charcoal case respectively;
In the condenser system: first step condenser outlet at bottom connects first step storage tank, and first step storage tank links to each other with oil pump, and the oil pump the other end is connected to the first step nozzle and the second stage nozzle of first step condenser inside respectively; The top of first step condenser is connected to second stage condenser upper entrance, and second stage condenser links to each other with exhaust purifier with second stage storage tank respectively;
In the pyrolysis exhaust gas circulation system: another termination compressor of exhaust purifier, the outlet of compressor connect the gas-holder inlet, and the gas-holder outlet connects burner and the terminal vertical pipe of first step screw feeder top respectively;
In the heating system: burner connects indirect heating chuck, spouted wind inlet, fluidized wind inlet, gas-holder, oil tank and induced draft fan respectively.
Fast pyrolysis reactor adopts spouted fluidized bed technique, and reactor temperature is controlled at 400～600 ℃, and the gas phase residence time is controlled in the 2s.
First step condenser is a spray condenser, and first step nozzle that it is inner and second stage nozzle divide two-layer layout up and down along the condenser vertical direction; Second stage condenser is an indirect condenser; The gas temperature of second stage condensator outlet is controlled at 40～70 ℃.
After the pyrolysis tail gas part of gas-holder outlet enters burner and high-temperature flue gas indirect heat exchange, enter the spouted fluidized bed fast pyrolysis reactor by spouted wind inlet, fluidized wind inlet respectively; The part of the pyrolysis tail gas in the gas-holder enters aid burning in the burner burner hearth.
Beneficial effect: the utility model is a kind of novel biomass rapid pyrolysis apparatus of researching and developing out on above-mentioned technical foundation, it has many outstanding advantages: (1) adopts the built-up type charging system, the broken arch of machinery, strength is loosening, screw feeder combines, and what can guarantee to greatest extent to feed in raw material is smooth and easy and stable.(2) owing to adopt the reactor of spouted fluidized bed as biomass fast pyrogenation, medium circulation speed is fast in the reactor, heat and mass is effective, can satisfy three fundamental principles of biomass flash pyrolysis well, be high heating rate, good heat transfer effect and the requirement of the residence time mutually of losing heart, guaranteed the productive rate and the quality of pyrolysis liquids.(3) characteristics that need in a temperature range, carry out at pyrolysis gas of biomass complicated component, condensation, condenser system adopts first step spray chilling and the second stage indirect refrigerative condensed in two stages mode, can guarantee the abundant condensation of pyrolysis gas of biomass, and can control the condensing temperature of condensed in two stages device by adjusting the flow that sprays medium and indirect heat exchange medium, thereby realize separating of bio oil heavy component and light component, not only can improve the productive rate and the quality of bio oil, also energy utilization and extraction Chemicals be combined simultaneously.(4) adopt the pyrolysis exhaust gas circulation system, can realize the recycle of carrier gas, not only alleviated influence, and reduced running cost, make the industry of being more convenient for of a whole set of pyrolysis installation amplify environment.
Description of drawings
Fig. 1 is a structural representation of the present utility model.
Wherein have: feed bin 1-1, machinery arch breaking apparatus 1-2, first step screw feeder 1-3, second stage screw feeder 1-4, water cold sleeve 1-5, spouted fluidized bed fast pyrolysis reactor 2-1, spouted wind inlet 2-2, fluidized wind inlet 2-3, heating jacket 2-4, first step cyclonic separator 3-1, second stage cyclonic separator 3-2, first step collection charcoal case 3-3, second stage collection charcoal case 3-4, first step condenser 4-1, first step nozzle 4-1-1, second stage nozzle 4-1-2, second stage condenser 4-2, oil pump 4-3, first step storage tank 4-4, second stage storage tank 4-5, exhaust purifier 5-1, compressor 5-2, gas-holder 5-3, burner 6-1, burner oil tank 6-2, induced draft fan 6-3.
Concrete enforcement side is a formula
Specific embodiments of the present utility model is as follows:
It comprises charging system, fast pyrolysis reactor, condenser system, pyrolysis exhaust gas circulation system and heating system, wherein,
In the charging system: the built-in mechanical arch breaking apparatus 1-2 of feed bin 1-1, meet first step screw feeder 1-3 under the feed bin 1-1, the end of first step screw feeder 1-3 meets second stage screw feeder 1-4 by vertical pipeline, another termination spouted fluidized bed fast pyrolysis reactor of second stage screw feeder 1-4 2-1, water cold sleeve 1-5 is coated on second stage screw feeder 1-4 and spouted fluidized bed fast pyrolysis reactor 2-1 connection portion;
Spouted fluidized bed fast pyrolysis reactor 2-1 meets spouted wind inlet 2-2, fluidized wind inlet 2-3, first step cyclonic separator 3-1 respectively, and meets burner 6-1 through indirect heating chuck 2-4; First step cyclonic separator 3-1 bottom meets first step collection charcoal case 3-3, first step cyclonic separator 3-1 top and second stage cyclonic separator 3-2 join, and top outlet and the bottom of second stage cyclonic separator 3-2 meet first step condenser 4-1 below side inlet and second stage collection charcoal case 3-4 respectively;
In the condenser system: first step condenser 4-1 outlet at bottom meets first step storage tank 4-4, first step storage tank 4-4 links to each other with oil pump 4-3, and the oil pump 4-3 the other end is connected to the first step nozzle 4-1-1 and the second stage nozzle 4-1-2 of first step condenser 4-1 inside respectively; The top of first step condenser 4-1 is connected to second stage condenser 4-2 upper entrance, and second stage condenser 4-2 links to each other with exhaust purifier 5-1 with second stage storage tank 4-5 respectively;
In the pyrolysis exhaust gas circulation system: another termination compressor of exhaust purifier 5-1 5-2, the outlet of compressor 5-2 connects gas-holder 5-3 inlet, and gas-holder 5-3 outlet connects burner 6-1 and the terminal vertical pipe of first step screw feeder 1-3 top respectively;
In the heating system: burner 6-1 meets indirect heating chuck 2-4, spouted wind inlet 2-2, fluidized wind inlet 2-3, gas-holder 5-3, oil tank 6-2 and induced draft fan 6-3 respectively.
Biomass material is added in the feed bin 1-1.Mechanical arch breaking apparatus 1-2 is installed in the feed bin, can avoids material arch formation in feed bin, to occur.Biomass material enters the two-stage screw feeding device downwards by feed bin, and the effect of first step spiral 1-3 is the weight feed that guarantees material, and second stage spiral 1-4 prevents then that material is heated and stops up the reactor charging opening.Between first and second grade spiral, increase blanking wind and guarantee that first step spiral end materials enters second stage spiral smoothly.The spiral end installs water cold sleeve 1-5 additional in the second stage, further reduces possibility of jamming takes place.Biomass material enters spouted fluidized bed fast pyrolysis reactor 2-1 by second stage spiral.Spouted fluidized bed fast pyrolysis reactor 2-1 uses 60 ° of taper cloth wind modes, and reactor institute heat requirement is from the heat exchange of high-temperature flue gas among the reactor external jacket 2-4.Spouted wind and fluidized wind through preheating enter inside reactor by the spouted wind inlet 2-2 and the fluidized wind inlet 2-3 of spouted fluidized bed fast pyrolysis reactor 2-1 bottom respectively.Temperature is controlled at 400～600 ℃ in the spouted fluidized bed fast pyrolysis reactor 2-1, the gas phase residence time guarantees in 2s, biomass material is at reactor generation fast pyrogenation, the pyrolysis gas that produces enters the two stage cyclone separator by spouted fluidized bed fast pyrolysis reactor 2-1 top exit, and the coke granule under centrifugation falls to entering collection charcoal case.The pyrolysis gas of removing behind the coke granule continues to enter first step condenser 4-1, first step condenser 4-1 adopts the directly mode of spray, be provided with two groups of nozzles from bottom to top, pyrolysis gas is from bottom to top through two groups of nozzle sprays, condensable part is condensed into liquid and flows into first step storage tank 4-4 downwards, first step storage tank 4-4 lower side meets oil pump 4-3, and the partially liq bio oil is drawn back to nozzle by oil pump 4-3 and served as the spray medium.Pyrolysis gas enters second stage condenser 4-2 by the outlet of first step condenser top, and second stage condenser 4-2 adopts the mode of indirect condensing, and the product liquid under the condensation enters second stage storage tank 4-5 downwards.The pyrolysis exhaust temperature of second stage condenser 4-2 outlet is at 40～70 ℃.Can realize separating of bio oil heavy component and light component by regulating the spray medium with the fractional condensation mode that the flow of indirect heat exchange medium is controlled the condensing temperature of condensed in two stages device, not only can improve the productive rate and the quality of bio oil, also energy utilization and extraction Chemicals be combined simultaneously.A pyrolysis tail gas part that obtains after the condensation enters atmosphere after treatment, and another part is then through entering gas-holder 5-3 after exhaust purifier 5-1 cleaning and the compressor 5-2 supercharging.Draw four road gases from gas-holder 5-3, one tunnel blanking wind that connects charging system wherein, one the tunnel enters the spouted wind inlet 2-2 of spouted fluidized bed fast pyrolysis reactor 2-1 bottom as spouted wind after burner 6-1 preheating, one the tunnel enters the fluidized wind inlet 2-3 of spouted fluidized bed fast pyrolysis reactor 2-1 lower side as fluidized wind after fluidized bed combustion device 6-1 preheating, one the tunnel enters combustion chamber 6-1 participates in burning, and heat is provided.
Claims (4)
1. biomass fast pyrogenation device, it is characterized in that: it comprises charging system, fast pyrolysis reactor, condenser system, pyrolysis exhaust gas circulation system and heating system, wherein,
In the charging system: the built-in mechanical arch breaking apparatus of feed bin (1-1) (1-2), connect first step screw feeder (1-3) under the feed bin (1-1), the end of first step screw feeder (1-3) connects second stage screw feeder (1-4) by vertical pipeline, another termination spouted fluidized bed fast pyrolysis reactor (2-1) of second stage screw feeder (1-4), water cold sleeve (1-5) are coated on second stage screw feeder (1-4) and spouted fluidized bed fast pyrolysis reactor (2-1) connection portion;
Spouted fluidized bed fast pyrolysis reactor (2-1) connects spouted wind inlet (2-2), fluidized wind inlet (2-3), first step cyclonic separator (3-1) respectively, and connects burner (6-1) through indirect heating chuck (2-4); First step cyclonic separator (3-1) bottom connects first step collection charcoal case (3-3), first step cyclonic separator (3-1) top and second stage cyclonic separator (3-2) join, and the top outlet and the bottom of second stage cyclonic separator (3-2) connect first step condenser (4-1) below side inlet and second stage collection charcoal case (3-4) respectively;
In the condenser system: first step condenser (4-1) outlet at bottom connects first step storage tank (4-4), first step storage tank (4-4) links to each other with oil pump (4-3), and oil pump (4-3) the other end is connected to first step condenser (4-1) inner first step nozzle (4-1-1) and second stage nozzle (4-1-2) respectively; The top of first step condenser (4-1) is connected to second stage condenser (4-2) upper entrance, and second stage condenser (4-2) links to each other with exhaust purifier (5-1) with second stage storage tank (4-5) respectively;
In the pyrolysis exhaust gas circulation system: another termination compressor (5-2) of exhaust purifier (5-1), the outlet of compressor (5-2) connects gas-holder (5-3) inlet, and gas-holder (5-3) outlet connects burner (6-1) and the terminal vertical pipe of first step screw feeder (1-3) top respectively;
In the heating system: burner (6-1) connects indirect heating chuck (2-4), spouted wind inlet (2-2), fluidized wind inlet (2-3), gas-holder (5-3), oil tank (6-2) and induced draft fan (6-3) respectively.
2. a kind of biomass fast pyrogenation device according to claim 1 is characterized in that: fast pyrolysis reactor (2-1) adopts spouted fluidized bed technique, and reactor temperature is controlled at 400～600 ℃, and the gas phase residence time is controlled in the 2s.
3. a kind of biomass fast pyrogenation device according to claim 1, it is characterized in that: first step condenser (4-1) is a spray condenser, and first step nozzle (4-1-1) that it is inner and second stage nozzle (4-1-2) divide two-layer layout up and down along the condenser vertical direction; Second stage condenser (4-2) is an indirect condenser; The gas temperature of second stage condenser (4-2) outlet is controlled at 40～70 ℃.
4. a kind of biomass fast pyrogenation device according to claim 1, it is characterized in that: after the pyrolysis tail gas part of gas-holder (5-3) outlet enters burner (6-1) and high-temperature flue gas indirect heat exchange, enter spouted fluidized bed fast pyrolysis reactor (2-1) by spouted wind inlet (2-2), fluidized wind inlet (2-3) respectively; The part of the pyrolysis tail gas in the gas-holder (5-3) enters aid burning in burner (6-1) burner hearth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202342915U CN201473491U (en) | 2009-08-06 | 2009-08-06 | Biomass fast thermal decomposition device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202342915U CN201473491U (en) | 2009-08-06 | 2009-08-06 | Biomass fast thermal decomposition device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201473491U true CN201473491U (en) | 2010-05-19 |
Family
ID=42409735
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202342915U Expired - Lifetime CN201473491U (en) | 2009-08-06 | 2009-08-06 | Biomass fast thermal decomposition device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201473491U (en) |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962563A (en) * | 2010-10-30 | 2011-02-02 | 上海交通大学 | Device for preparing biofuel by quick thermal cracking of biomass |
| CN101624531B (en) * | 2009-08-06 | 2012-08-15 | 东南大学 | Device for preparing bio-oil by utilizing biomass spouted fluidized bed through pyrolysis and fractional condensation |
| CN102936507A (en) * | 2012-11-05 | 2013-02-20 | 北京华电光大新能源环保技术有限公司 | Poly-generation device and method for biomass pyrolysis |
| CN103131453A (en) * | 2013-03-11 | 2013-06-05 | 北京神雾环境能源科技集团股份有限公司 | Pyrolytic evaluation device for carbon-containing substances |
| CN103596672A (en) * | 2011-04-07 | 2014-02-19 | 可再生石油国际有限公司 | Method and apparatus for a combination moving bed thermal treatment reactor and moving bed filter |
| CN103657134A (en) * | 2013-12-09 | 2014-03-26 | 云南新立有色金属有限公司 | Condensing system of titanium tetrachloride gas and condensing method of titanium tetrachloride gas |
| CN103756712A (en) * | 2014-01-13 | 2014-04-30 | 东南大学 | Biomass quick cracking device based on internal-external circulation spouted fluidized bed |
| CN104263391A (en) * | 2014-09-24 | 2015-01-07 | 济南联星石油化工有限公司 | Crop cracking system |
| CN105972602A (en) * | 2016-05-24 | 2016-09-28 | 华东理工大学 | Processing device for solid organic waste and processing technique using same |
| CN109161394A (en) * | 2018-10-23 | 2019-01-08 | 山西大学 | A kind of low energy consumption biomass liquefier |
| CN110375308A (en) * | 2019-07-03 | 2019-10-25 | 中国科学院广州能源研究所 | The processing method of the irregular form organic solid castoff of low-density |
| CN110527543A (en) * | 2019-08-05 | 2019-12-03 | 浙江骐骥环境科技有限公司 | A kind of the receipts oil and fixed gas purification system of RDF pyrolysis gas |
| CN111040794A (en) * | 2020-01-03 | 2020-04-21 | 重庆科技学院 | System and process for producing oil by continuously and efficiently pyrolyzing waste plastics |
| CN114042355A (en) * | 2021-09-27 | 2022-02-15 | 浙江中烟工业有限责任公司 | Tobacco leaf raw fluidized bed dry distillation product filtering system and cyclone separation process thereof |
-
2009
- 2009-08-06 CN CN2009202342915U patent/CN201473491U/en not_active Expired - Lifetime
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101624531B (en) * | 2009-08-06 | 2012-08-15 | 东南大学 | Device for preparing bio-oil by utilizing biomass spouted fluidized bed through pyrolysis and fractional condensation |
| CN101962563B (en) * | 2010-10-30 | 2013-11-06 | 上海交通大学 | Device for preparing biofuel by quick thermal cracking of biomass |
| CN101962563A (en) * | 2010-10-30 | 2011-02-02 | 上海交通大学 | Device for preparing biofuel by quick thermal cracking of biomass |
| CN103596672A (en) * | 2011-04-07 | 2014-02-19 | 可再生石油国际有限公司 | Method and apparatus for a combination moving bed thermal treatment reactor and moving bed filter |
| CN102936507A (en) * | 2012-11-05 | 2013-02-20 | 北京华电光大新能源环保技术有限公司 | Poly-generation device and method for biomass pyrolysis |
| CN103131453A (en) * | 2013-03-11 | 2013-06-05 | 北京神雾环境能源科技集团股份有限公司 | Pyrolytic evaluation device for carbon-containing substances |
| CN103657134B (en) * | 2013-12-09 | 2015-11-25 | 云南新立有色金属有限公司 | The condenser system of titanium tetrachloride gases and the condensation method of titanium tetrachloride gases |
| CN103657134A (en) * | 2013-12-09 | 2014-03-26 | 云南新立有色金属有限公司 | Condensing system of titanium tetrachloride gas and condensing method of titanium tetrachloride gas |
| CN103756712A (en) * | 2014-01-13 | 2014-04-30 | 东南大学 | Biomass quick cracking device based on internal-external circulation spouted fluidized bed |
| CN104263391A (en) * | 2014-09-24 | 2015-01-07 | 济南联星石油化工有限公司 | Crop cracking system |
| CN105972602A (en) * | 2016-05-24 | 2016-09-28 | 华东理工大学 | Processing device for solid organic waste and processing technique using same |
| CN109161394A (en) * | 2018-10-23 | 2019-01-08 | 山西大学 | A kind of low energy consumption biomass liquefier |
| CN110375308A (en) * | 2019-07-03 | 2019-10-25 | 中国科学院广州能源研究所 | The processing method of the irregular form organic solid castoff of low-density |
| CN110375308B (en) * | 2019-07-03 | 2020-07-28 | 中国科学院广州能源研究所 | Method for treating low-density irregular-form organic solid waste |
| CN110527543A (en) * | 2019-08-05 | 2019-12-03 | 浙江骐骥环境科技有限公司 | A kind of the receipts oil and fixed gas purification system of RDF pyrolysis gas |
| CN111040794A (en) * | 2020-01-03 | 2020-04-21 | 重庆科技学院 | System and process for producing oil by continuously and efficiently pyrolyzing waste plastics |
| CN111040794B (en) * | 2020-01-03 | 2023-12-22 | 重庆科技学院 | System and process for producing oil by continuous and efficient pyrolysis of waste plastics |
| CN114042355A (en) * | 2021-09-27 | 2022-02-15 | 浙江中烟工业有限责任公司 | Tobacco leaf raw fluidized bed dry distillation product filtering system and cyclone separation process thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN201473491U (en) | Biomass fast thermal decomposition device | |
| CN101624531B (en) | Device for preparing bio-oil by utilizing biomass spouted fluidized bed through pyrolysis and fractional condensation | |
| CN101921627B (en) | Air-oil co-production device forcoupling fluidized bed pulverized coal gasification and solid heat carrier pyrolysis and method therefor | |
| CN103242869B (en) | Device and method for pyrolyzing and carbonizing biomass at low temperature by utilizing boiler flue gas | |
| CN105238432B (en) | Method and device for preparing high-quality bio-oil and white carbon black through self-heating acid pickling-pyrolysis-combustion integration | |
| CN101280201A (en) | Full cycle dry distillation process and system for producing shale oil from oil shale (coal) | |
| CN201834893U (en) | Fluidized bed pulverized coal gasification and solid heat carrier pyrolysis coupled petroleum coproduction device | |
| CN103060008A (en) | Biomass comprehensive transformation device and method thereof | |
| CN102807884A (en) | Method for preparing biological oil and biological char by thermal cracking and liquefying bamboo wood | |
| CN105950195A (en) | Cocurrent downward circulating fluidized bed millisecond pyrolysis and liquefaction technology for biomass | |
| CN103113905A (en) | Composite pulverized coal destructive distillation device and method | |
| CN108342211A (en) | A kind of novel biomass pyrolysis comprehensive utilization process and system | |
| CN202808710U (en) | Ore catalyst bed biomass flash pyrolysis oil production device | |
| CN100378193C (en) | Treatment method of organic waste material for gasification cracking multi coproduction | |
| CN103194246B (en) | Large kelp biomass dry distillation energy self-balancing oil production system and method thereof | |
| CN200996005Y (en) | Oil producer of circulation fluidized bed boiler by high-temperature ash pyrolytic biomass | |
| CN102517079B (en) | Biomass gasifying device with function of catalytically cracking inner circulation tar | |
| CN102226113A (en) | Biomass gasified tar processing system and method | |
| CN202152330U (en) | Production system by utilizing biomass raw material for making gasoline and diesel directly | |
| CN101602954B (en) | Method for manufacturing fuel through straw quick thermal cracking and fuel product thereof | |
| CN102994127A (en) | Low-rank coal multi-stage fluidized bed coal chemical industry multiple production system and method | |
| CN103074118A (en) | Pyrolysis-gasification integrated conversion and utilization system and method for waste agricultural resources | |
| CN103160297A (en) | Ore catalytic bed biomass fast pyrolysis oil-making device | |
| CN201634633U (en) | Device for producing biomass pyrolytic oil through rapid pyrolysis by biomass fluidized bed | |
| CN204589076U (en) | The resinous shale utilization system of a kind of coupled gas and solid thermal carriers |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20100519 Effective date of abandoning: 20090806 |