CN102031132B - Device and method for producing biological fuel oil cleaning fuel via self-heated rapid cracking of biomass - Google Patents
Device and method for producing biological fuel oil cleaning fuel via self-heated rapid cracking of biomass Download PDFInfo
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- 239000000446 fuel Substances 0.000 title claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 title abstract description 13
- 238000004140 cleaning Methods 0.000 title abstract 6
- 239000007789 gas Substances 0.000 claims abstract description 88
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- 239000003921 oil Substances 0.000 claims abstract description 44
- 239000002737 fuel gas Substances 0.000 claims abstract description 36
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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
- 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
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a device and a method for producing biological fuel oil cleaning fuel via the self-heated rapid cracking of biomass, and relates to a device and a method for producing biological fuel oil cleaning fuel via biomass. In allusion to the problems that the traditional device for producing biological fuel oil cleaning fuel via biomass has high manufacturing cost, demand of external fuel for heating and short service life, and the traditional method for producing biological fuel oil cleaning fuel via biomass has high energy consumption, the device provided by the invention has the scheme that: a storage bin is communicated with a liner inverted cone reactor which is arranged in a combustion chamber and sequentially communicated with a primary gas-solid separation device, a secondary gas-solid separation device and a condensation/liquefaction device; the method has the scheme that: a solid heat carrier is replaced by fuel gas a part of which is not condensed after being heated, the raw materials are fluidized and dried by using waste fume, the cracking oil gas in the liner inverted cone reactor enters into the condensation/liquefaction device after passing through the primary gas-solid separation device and the second gas-solid separation device, and the biological fuel oil in the condensation/liquefaction device enters into a finished oil product storage tank. The device and the method in the invention are used for producing biological fuel oil cleaning fuel.
Description
Technical field
The present invention relates to a kind of biomass-making bio-fuel-oil clean fuel device and method.
Background technology
The mankind are being faced with huge energy and environment pressure, and current energy industry mainly is mineral fuel industry, comprise coal, oil and natural gas.On the one hand, the application of fossil energy has promoted social development, and its energy is but exhausting day by day; On the other hand, the extensive use of fossil energy has caused serious environmental problem day by day, as causes global air temperature warming, infringement ozonosphere, destroys ecosphere balance, discharges objectionable impurities, causes natural disaster such as acid rain.
Since the seventies in 20th century first oil crisis; be subjected to the great attention of international community by biomass pyrolysis liquefying being produced research that bio-fuel-oil substitutes oil; its research mainly concentrates on an American-European countries surplus Canada, Finland, Italy, Sweden, Holland, Belgium, Britain and the U.S. etc. 10, has formed comparatively complete technical equipment and industrialization system at present.
Condensation liquefaction, the heat exchange of biomass pyrolysis liquefying bio-fuel-oil process processed relates to that biomass are pulverized, dry, thermal barrier heating, thermal barrier are carried, biomass change into bio-fuel-oil gas and carbon residue, bio-fuel-oil gas and carbon residue, thermal barrier at anaerobic closed reactor high speed endothermic pyrolysis gas solid separation, bio-fuel-oil gas and can not coagulate series of process link such as combustion gas processing.The biomass pyrolysis liquefying product comprises bio-fuel-oil, carbon residue carbon dust and can not coagulate combustion gas.Bio-fuel-oil can directly be used as various industrial furnace fuel such as turbine power generation, various boiler, cement sectors, ceramics, glass industry, also can make more high-grade oil-in-water type low emission biofuel with the diesel oil mixing and emulsifying and directly supply with various car and boat oil engines uses, also can be used as industrial chemicals.Bio-fuel-oil has easy storage, good transportation, low cost and other advantages, therefore is that the biomass pyrolysis liquefying of main products has become the leading mode that biomass energy transforms and utilizes with the bio-fuel-oil.
Yet, the mode of existing bio-fuel-oil processed, generally be utilize solid particulate as thermal barrier (cloudlike sand, ceramic particle, high-quality river sand etc.), earlier the thermal barrier particle is heated to certain temperature, be transported to itself and the biological particles that crushes in the cracking reactor of anaerobic simultaneously by certain proportioning then, in anoxic reactor, the thermal barrier particle that biological particles is several times as much as oneself surrounds, and mix on the limit, the limit motion, the limit is cracked into a large amount of gaseous hydrocarbon and a spot of solid carbon residue particle, the two is derived namely obtain target product bio-fuel-oil and a spot of combustion gas with fixed attention after the cracking oil gas after the gas solid separation is delivered to condenser condenses.It is little owing to calorific value not coagulate combustion gas, and Chang Zuofang burns processing, and carbon residue burns to replenish production with hot because the calorific value height often is transported to special thermal medium boiler.
Aforesaid method has following shortcoming: the one, need custom-designed thermal medium boiler, and not only cost height, power consumption are high, and need the heat supply of external source fuel more, and economy is very poor, and heat energy consumption generally will account for more than 30% of total cost; The 2nd, owing to the used beat carrier need be collected, rise to more than the enough height in top of the thermal medium boiler that is positioned at the reactor top, release again after pouring thermal barrier into process furnace then and reheating and enter reactor, could form production cycle, so just cause high power consumption situation; The 3rd, because the high-temp solid thermal barrier flows in process furnace, reactor and the various pipelines that are attached thereto always, the very fast thermal wear of equipment causes equipment life low as a result; The 4th, because huge, the firm steel construction of whole production arts demand is installed and supported various device and makes it have order to satisfy processing requirement by highly straggly, the result just causes the whole production device need consume great deal of steel, and construction investment is big, the total production cost height.
Summary of the invention
The present invention provides a kind of biomass from the quick cracking of heat supply bio-fuel-oil clean fuel processed device and method for the problem that solves present biomass-making bio-fuel-oil clean fuel apparatus cost height, needs the heat supply of external source fuel, the life-span is low and the power consumption of biomass-making bio-fuel-oil clean fuel method is high.
The present invention solves the problems of the technologies described above the technical scheme of taking: the device scheme: described device comprises former feed bin, feeding unit, feed bin, the combustion chamber, inner bag back taper reactor, former material separating device, the one-level gas-solid separating device, the secondary gas-solid separating device, the condensation liquefaction device, the carrier gas air pump, the buffering gas tank, non-condensable gas bleed machine, the processed oil storage tank, condensation spray oil pump, the cooling heat transferring device, do not coagulate the combustible gas air pump, do not coagulate the combustible gas combustion engine, built-in cone and carrier gas heating tube, the smoke outlet of combustion chamber is communicated with the discharge port end of former feed bin, the discharge port end of former feed bin is communicated with the entrance end of former material separating device, the exit end of former material separating device is communicated with the entrance end of feed bin, the exit end of feed bin is communicated with the material inlet end of inner bag back taper reactor, inner bag back taper reactor is located in the combustion chamber, the cracking oil gas exit end of inner bag back taper reactor is communicated with the entrance end of one-level gas-solid separating device, the outlet at bottom end of one-level gas-solid separating device is communicated with the backflow entrance end of inner bag back taper reactor, the cracking oil gas exit end of one-level gas-solid separating device is communicated with the entrance end of secondary gas-solid separating device, the carbon dust exit end of secondary gas-solid separating device is communicated with the carbon dust entrance end of combustion chamber, the cracking oil gas exit end of secondary gas-solid separating device is communicated with the entrance end of condensation liquefaction device, the first bio-fuel-oil exit end of condensation liquefaction device is communicated with the entrance end of processed oil storage tank, the second bio-fuel-oil exit end of condensation liquefaction device is communicated with the entrance end of cooling heat transferring device, the cooling heat transferring device is communicated with the bio-fuel-oil entrance end of condensation liquefaction device by condensation spray oil pump, the gas outlet end that do not coagulate of condensation liquefaction device is communicated with by the entrance end of non-condensable gas bleed machine with the buffering gas tank, first of buffering gas tank does not coagulate the gas outlet end and is communicated with an end of carrier gas heating tube, the other end of carrier gas heating tube is communicated with the cracking heat-carrying gas entrance end of inner bag back taper reactor, the carrier gas heating tube is wrapped in inner bag back taper reactor outside, second of buffering gas tank does not coagulate the gas outlet end and is communicated with the fuel gas inlet end that do not coagulate that does not coagulate the combustible gas combustion engine, and built-in cone is contained in the inner bag back taper reactor;
Method scheme: said method comprising the steps of, step 1: open to start and use the straw fuel gas producer to produce straw fuel gas, open to start and use the straw fuel gas combustion engine, start and discharge hot flue gas to the combustion chamber with the straw fuel gas combustion engine, the hot flue gas that biomass material in the former feed bin utilizes the combustion chamber to discharge carries out dry back and passes through the air conveying to former material separating device of flue gas, separate the laggard feed bin of going into through former material separating device, feed to inner bag back taper reactor by feeding unit, primary product is cracking oil gas; Step 2: the cracking oil gas in the inner bag back taper reactor enters the condensation liquefaction device behind one-level gas-solid separating device and secondary gas-solid separating device, and the primary product in the condensation liquefaction device is bio-fuel-oil and does not coagulate combustion gas; Step 3: a part of bio-fuel-oil in the condensation liquefaction device enters the processed oil storage tank, after another part bio-fuel-oil enters the cooling of cooling heat transferring device, pumps into condensation liquefaction device top by condensation spray oil pump and sprays; Step 4: the combustion gas of not coagulating in the condensation liquefaction device is transported to the buffering gas tank by non-condensable gas bleed machine, closes to start with the straw fuel gas combustion engine and start and uses the straw fuel gas producer, starts and does not coagulate the combustible gas combustion engine; Step 5: the part in the buffering gas tank is not coagulated combustion gas and is imported to the carrier gas heating tube through the carrier gas air pump, enter inner bag back taper reactor through the carrier gas heating tube again, the temperature that do not coagulate combustion gas this moment is 460～650 ℃, and another part pumps into not combustible gas combustion engine with fixed attention by not coagulating the combustible gas air pump.
The present invention has following beneficial effect: 1, the inventive method is not used solid thermal carriers, but adopt gas heat-carrying mode, part is not coagulated the combustion gas importing places the carrier gas heating tube anaerobic heating back of combustion chamber as thermophore, replace solid thermal carriers, can eliminate all shortcomings of utilizing the solid thermophore, can significantly reduce by 16～22% heat waste and 10% above current consumption, prolong service life of equipment more than 1 times; 2, the inventive method will not coagulated useless flue gas importing raw material fluidized drying and the e Foerderanlage after carrier gas pipe and inner bag back taper formula reactor are heated in the burning of combustion gas and carbon residue, maximally utilise the waste heat of useless flue gas, realize continuous conveying and the drying of raw material, effectively reduce the oily production cost of system; 3, the inner bag back taper formula reactor in apparatus of the present invention is that thermophore makes the cracking of biomass small-particle become cracked oil gas with the combustion gas of not coagulating that produces in the condensation liquefaction process, and its advantage is: simple in structure, cost is low; No solid thermal carriers thermal wear phenomenon, life-span are long; Specially designed built-in cone can make the biological particles that enters inner bag back taper formula reactor evenly distribute rapidly, comprehensive being heated, and realize dynamic of short duration suspension with thermo-cracking weightlessness, be conducive to the abundant cracking produce oil of raw material, and raising bio-fuel-oil transformation efficiency 8～12% and quality (about 5000kc/kg); 4, apparatus of the present invention adopt and not to coagulate gas burner system and will make the low heat value that produces in the oily process and not coagulate combustion gas and carbon residue and take full advantage of, realize production process from heat supply and thermal energy balance, exempt the use of external source fuel.
Description of drawings
Fig. 1 is one-piece construction synoptic diagram of the present invention.
Embodiment
Embodiment one: present embodiment is described in conjunction with Fig. 1, the device of present embodiment comprises former feed bin 1, feeding unit 2, feed bin 3, combustion chamber 4, inner bag back taper reactor 5, former material separating device 6, one-level gas-solid separating device 7, secondary gas-solid separating device 8, condensation liquefaction device 9, carrier gas air pump 10, buffering gas tank 11, non-condensable gas bleed machine 12, processed oil storage tank 13, condensation spray oil pump 14, cooling heat transferring device 15, do not coagulate combustible gas air pump 18, do not coagulate combustible gas combustion engine 19, built-in cone 20 and carrier gas heating tube 21, the smoke outlet of combustion chamber 4 is communicated with the discharge port end of former feed bin 1, the discharge port end of former feed bin 1 is communicated with the entrance end of former material separating device 6, the exit end of former material separating device 6 is communicated with the entrance end of feed bin 3, the exit end of feed bin 3 is communicated with the material inlet end of inner bag back taper reactor 5, inner bag back taper reactor 5 is located in the combustion chamber 4, the cracking oil gas exit end of inner bag back taper reactor 5 is communicated with the entrance end of one-level gas-solid separating device 7, the outlet at bottom end of one-level gas-solid separating device 7 is communicated with the backflow entrance end of inner bag back taper reactor 5, the cracking oil gas exit end of one-level gas-solid separating device 7 is communicated with the entrance end of secondary gas-solid separating device 8, the carbon dust exit end of secondary gas-solid separating device 8 is communicated with the carbon dust entrance end of combustion chamber 4, the cracking oil gas exit end of secondary gas-solid separating device 8 is communicated with the entrance end of condensation liquefaction device 9, the first bio-fuel-oil exit end of condensation liquefaction device 9 is communicated with the entrance end of processed oil storage tank 13, the second bio-fuel-oil exit end of condensation liquefaction device 9 is communicated with the entrance end of cooling heat transferring device 15, cooling heat transferring device 15 is communicated with the bio-fuel-oil entrance end of condensation liquefaction device 9 by condensation spray oil pump 14, the gas outlet end that do not coagulate of condensation liquefaction device 9 is communicated with by the entrance end of non-condensable gas bleed machine 12 with buffering gas tank 11, first of buffering gas tank 11 does not coagulate the gas outlet end and is communicated with an end of carrier gas heating tube 21, the other end of carrier gas heating tube 21 is communicated with the cracking heat-carrying gas entrance end of inner bag back taper reactor 5, carrier gas heating tube 21 is wrapped in inner bag back taper reactor 5 outsides, second of buffering gas tank 11 does not coagulate the gas outlet end and is communicated with the fuel gas inlet end that do not coagulate that does not coagulate combustible gas combustion engine 19, and built-in cone 20 is contained in the inner bag back taper reactor 5.
Embodiment two: present embodiment is described in conjunction with Fig. 1, the device of present embodiment also comprises water circulating pump 16 and cold water device 17, cooling heat transferring device 15 is communicated with 17 circulations of cold water device by water circulating pump 16, and this structure is used for the heat exchange that bio-fuel-oil is used in condensation.Other composition and annexation are identical with embodiment one.
Embodiment three: present embodiment is described in conjunction with Fig. 1, the device of present embodiment also comprises starting with straw fuel gas combustion engine 22, straw fuel gas air pump 23 and starting uses straw fuel gas producer 24, start with straw fuel gas producer 24 and be communicated with straw fuel gas combustion engine 22 with startup by straw fuel gas air pump 23, start and use straw fuel gas combustion engine 22 to be communicated with combustion chamber 4, this structure is used for the initial start of total system.Other composition and annexation are identical with embodiment one.
Embodiment four: present embodiment is described in conjunction with Fig. 1, the method of present embodiment may further comprise the steps, step 1: open to start and use straw fuel gas producer 24 to produce straw fuel gas, open and start with straw fuel gas combustion engine 22, startup usefulness straw fuel gas combustion engine 22 is the hot flue gas of 4 dischargings to the combustion chamber, the hot flue gas that biomass material in the former feed bin 1 utilizes combustion chamber 4 to discharge carries out dry back and passes through the air conveying to former material separating device 6 of flue gas, separate the laggard feed bin 3 of going into through former material separating device 6, feed to inner bag back taper reactor 5 by feeding unit 2, primary product is cracking oil gas;
The heat that combustion chamber 4 provides makes raw material generation scission reaction;
Step 2: the cracking oil gas in the inner bag back taper reactor 5 enters condensation liquefaction device 9 behind one-level gas-solid separating device 7 and secondary gas-solid separating device 8, and the primary product in the condensation liquefaction device 9 is bio-fuel-oil and does not coagulate combustion gas;
Step 3: a part of bio-fuel-oil in the condensation liquefaction device 9 enters processed oil storage tank 13, after another part bio-fuel-oil enters 15 coolings of cooling heat transferring device, pumps into condensation liquefaction device 9 tops by condensation spray oil pump 14 and sprays;
Circulating condensing liquefaction is finished in bio-fuel-oil in the condensation liquefaction device 9 and cracked oil gas phase meeting from bottom to top;
Step 4: the combustion gas of not coagulating in the condensation liquefaction device 9 is transported to buffering gas tank 11 by non-condensable gas bleed machine 12, wait to cushion and do not coagulate gas quantity when reaching normal needs in the gas tank, close to start with straw fuel gas combustion engine 22 and start and use straw fuel gas producer 24, start and do not coagulate combustible gas combustion engine 19;
Step 5: the part in the buffering gas tank 11 is not coagulated combustion gas and is imported to carrier gas heating tube 21 through carrier gas air pump 10, enter inner bag back taper reactor 5 through carrier gas heating tube 21 again, the temperature that do not coagulate combustion gas this moment is 460～650 ℃, and another part pumps into not combustible gas combustion engine 19 with fixed attention by not coagulating combustible gas air pump 18;
Do not coagulate combustion gas bottom from inner bag back taper fluidized reactor 5 after heating and enter as the cracking heat-carrying gas, raw material is contacted and heated and heat scission reaction by comprehensive encirclement, finish biomass by solid-state conversion to gaseous state (cracking oil gas); Do not coagulate the flue gas of gas burner system 19 burning back generations by combustion chamber 4 pairs of inner bag back tapers fluidized reactor 5 and gas-carrier pipeline 21 heating.
Embodiment five: present embodiment is described in conjunction with Fig. 1, carbon dust in the step 2 of present embodiment in the one-level gas-solid separating device 7 enters in the inner bag back taper reactor 5, carbon dust in the secondary gas-solid separating device 8 enters in the inner bag back taper reactor 5, carbon dust enters in the inner bag back taper fluidized reactor 5 in this step, wherein big solid particulate is conducive to the homogenize of biological particles, and carbon dust imports combustion chamber 4 and acts as a fuel utilization so that production heat energy to be provided.Other step is identical with embodiment four.
Claims (5)
1. biomass are from the quick cracking of heat supply bio-fuel-oil clean fuel processed device, it is characterized in that described device comprises former feed bin (1), feeding unit (2), feed bin (3), combustion chamber (4), inner bag back taper reactor (5), former material separating device (6), one-level gas-solid separating device (7), secondary gas-solid separating device (8), condensation liquefaction device (9), carrier gas air pump (10), buffering gas tank (11), non-condensable gas bleed machine (12), processed oil storage tank (13), condensation spray oil pump (14), cooling heat transferring device (15), do not coagulate combustible gas air pump (18), do not coagulate combustible gas combustion engine (19), built-in cone (20) and carrier gas heating tube (21), the smoke outlet of combustion chamber (4) is communicated with the discharge port end of former feed bin (1), the discharge port end of former feed bin (1) is communicated with the entrance end of former material separating device (6), the exit end of former material separating device (6) is communicated with the entrance end of feed bin (3), the exit end of feed bin (3) is communicated with the material inlet end of inner bag back taper reactor (5), inner bag back taper reactor (5) is located in the combustion chamber (4), the cracking oil gas exit end of inner bag back taper reactor (5) is communicated with the entrance end of one-level gas-solid separating device (7), the outlet at bottom end of one-level gas-solid separating device (7) is communicated with the backflow entrance end of inner bag back taper reactor (5), the cracking oil gas exit end of one-level gas-solid separating device (7) is communicated with the entrance end of secondary gas-solid separating device (8), the carbon dust exit end of secondary gas-solid separating device (8) is communicated with the carbon dust entrance end of combustion chamber (4), the cracking oil gas exit end of secondary gas-solid separating device (8) is communicated with the entrance end of condensation liquefaction device (9), the first bio-fuel-oil exit end of condensation liquefaction device (9) is communicated with the entrance end of processed oil storage tank (13), the second bio-fuel-oil exit end of condensation liquefaction device (9) is communicated with the entrance end of cooling heat transferring device (15), cooling heat transferring device (15) is communicated with the bio-fuel-oil entrance end of condensation liquefaction device (9) by condensation spray oil pump (14), the gas outlet end that do not coagulate of condensation liquefaction device (9) is communicated with by the entrance end of non-condensable gas bleed machine (12) with buffering gas tank (11), first of buffering gas tank (11) does not coagulate the gas outlet end and is communicated with an end of carrier gas heating tube (21), the other end of carrier gas heating tube (21) is communicated with the cracking heat-carrying gas entrance end of inner bag back taper reactor (5), carrier gas heating tube (21) is wrapped in inner bag back taper reactor (5) outside, second of buffering gas tank (11) does not coagulate the gas outlet end and is communicated with the fuel gas inlet end that do not coagulate that does not coagulate combustible gas combustion engine (19), and built-in cone (20) is contained in the inner bag back taper reactor (5).
According to the described biomass of claim 1 from the quick cracking of heat supply bio-fuel-oil clean fuel processed device, it is characterized in that described device also comprises water circulating pump (16) and cold water device (17), cooling heat transferring device (15) is communicated with cold water device (17) circulation by water circulating pump (16).
According to claim 1 or 2 described biomass from the quick cracking of heat supply bio-fuel-oil clean fuel processed device, it is characterized in that described device also comprises startup straw fuel gas combustion engine (22), straw fuel gas air pump (23) and startup straw fuel gas producer (24), start and use straw fuel gas producer (24) to be communicated with straw fuel gas combustion engine (22) with startup by straw fuel gas air pump (23), startup is communicated with combustion chamber (4) with straw fuel gas combustion engine (22).
4. biomass of utilizing the described device of claim 1 are from the quick cracking of heat supply bio-fuel-oil clean fuel processed method, it is characterized in that said method comprising the steps of, step 1: open to start and use straw fuel gas producer (24) to produce straw fuel gas, open and start with straw fuel gas combustion engine (22), start with straw fuel gas combustion engine (22) to the combustion chamber (4) discharge hot flue gas, the hot flue gas that biomass material in the former feed bin (1) utilizes combustion chamber (4) to discharge carries out dry back and passes through the air conveying to former material separating device (6) of flue gas, separate the laggard feed bin (3) of going into through former material separating device (6), feed to inner bag back taper reactor (5) by feeding unit (2), primary product is cracking oil gas; Step 2: the cracking oil gas in the inner bag back taper reactor (5) enters condensation liquefaction device (9) behind one-level gas-solid separating device (7) and secondary gas-solid separating device (8), and the primary product in the condensation liquefaction device (9) is bio-fuel-oil and does not coagulate combustion gas; Step 3: a part of bio-fuel-oil in the condensation liquefaction device (9) enters processed oil storage tank (13), after another part bio-fuel-oil enters cooling heat transferring device (15) cooling, pump into condensation liquefaction device (9) top by condensation spray oil pump (14) and spray; Step 4: the combustion gas of not coagulating in the condensation liquefaction device (9) is transported to buffering gas tank (11) by non-condensable gas bleed machine (12), close to start with straw fuel gas combustion engine (22) and start and use straw fuel gas producer (24), start and do not coagulate combustible gas combustion engine (19); Step 5: the part in the buffering gas tank (11) is not coagulated combustion gas and is imported to carrier gas heating tube (21) through carrier gas air pump (10), enter inner bag back taper reactor (5) through carrier gas heating tube (21) again, the temperature that do not coagulate combustion gas this moment is 460～650 ℃, and another part pumps into not combustible gas combustion engine (19) with fixed attention by not coagulating combustible gas air pump (18).
According to the described biomass of claim 4 from the quick cracking of heat supply bio-fuel-oil clean fuel processed method, it is characterized in that the carbon dust in the one-level gas-solid separating device (7) enters in the inner bag back taper reactor (5) in the step 2, the carbon dust in the secondary gas-solid separating device (8) enters in the inner bag back taper reactor (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010106157605A CN102031132B (en) | 2010-12-30 | 2010-12-30 | Device and method for producing biological fuel oil cleaning fuel via self-heated rapid cracking of biomass |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010106157605A CN102031132B (en) | 2010-12-30 | 2010-12-30 | Device and method for producing biological fuel oil cleaning fuel via self-heated rapid cracking of biomass |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1425494A (en) * | 2003-01-17 | 2003-06-25 | 清华大学 | Large fluidized bed reactor for wide sieving fluidized particles |
| CN2890053Y (en) * | 2006-04-07 | 2007-04-18 | 王述洋 | Tricone-shaped heat carrier partial reflection refluxing type reactor for flashing speed cleavage preparation of biological fuel oil |
| CN101445737A (en) * | 2008-12-31 | 2009-06-03 | 合肥工业大学 | Internal combustion type heating rotating cone type biomass pyrolysis liquefaction device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1425494A (en) * | 2003-01-17 | 2003-06-25 | 清华大学 | Large fluidized bed reactor for wide sieving fluidized particles |
| CN2890053Y (en) * | 2006-04-07 | 2007-04-18 | 王述洋 | Tricone-shaped heat carrier partial reflection refluxing type reactor for flashing speed cleavage preparation of biological fuel oil |
| CN101445737A (en) * | 2008-12-31 | 2009-06-03 | 合肥工业大学 | Internal combustion type heating rotating cone type biomass pyrolysis liquefaction device |
Non-Patent Citations (2)
| Title |
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| 李滨.转锥式生物质闪速热解装置设计理论及仿真研究.《中国博士学位论文全文数据库 工程科技II辑》.2009,(第10期),C041-2. |
| 转锥式生物质闪速热解装置设计理论及仿真研究;李滨;《中国博士学位论文全文数据库 工程科技II辑》;20091015(第10期);C041-2 * |
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