CN101343547A - Apparatus and method for preparing biological oil with biomass vacuum thermal cracking and classification - Google Patents
Apparatus and method for preparing biological oil with biomass vacuum thermal cracking and classification Download PDFInfo
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- CN101343547A CN101343547A CNA2008101982492A CN200810198249A CN101343547A CN 101343547 A CN101343547 A CN 101343547A CN A2008101982492 A CNA2008101982492 A CN A2008101982492A CN 200810198249 A CN200810198249 A CN 200810198249A CN 101343547 A CN101343547 A CN 101343547A
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Abstract
The invention discloses a device for making biological oil according to classification and the method thereof. Under vacuum pressure, when a thermal cracking device is externally heated and the temperature increases, according to the difference of the pyrolysis temperature, the biological oil with high water content manufactured during a low temperature period is separated in advance, the dwell time of the pyrolysis temperature is controlled, and the biological oil with low water content and high organic component content produced in the intermediate temperate period is collected; in addition, a catalytic cracking device is arranged at the down stream of the vacuum cracking reactor, and long chain organism and complex aromatic compound are cracked into short chain organism and simple aromatic compound, which lays a good foundation for effectively utilizing the organic constituent of the biological oil. The method partially solves the problems that in the biological oil prepared by the pyrolysis reactor such as traditional fluidized bed and the like, the total water content is high, simultaneously water and polar organic compounds are highly combined so that the water and the polar organic compounds are difficult to be separated and utilized, and the method extends the application range of the biological oil, which plays an important role in the sustainable supplying of energy and material industry.
Description
Technical field
The present invention relates to the technical field that bio oil is produced, the device and method of bio oil is produced in especially a kind of biomass vacuum thermal cracking classification.
Background technology
Biomass are as a class important renewable energy, and it utilizes technology to be subjected to paying attention to widely.European Union is in the fund to the biomass fuel technological development drops into, and what ratio was the highest is the biomass pyrolytic technology.
Product one bio oil of biomass fast pyrogenation is not the product of pyrolytic reaction under the thermodynamic(al)equilibrium condition, but biomass are through the pyrolytic reaction of short period of time and from the quick refrigerative product of pyrolysis temperature.Characteristics such as bio oil thickness, poor stability, corrodibility are strong, chemical constitution complexity are brought very big obstruction to the process that bio oil substitutes traditional petroleum products, become the restriction bio oil extensively, the efficient bottleneck that utilizes.Bio oil is refining in the world at present mainly contains following several method: methods such as hydrogenation deoxidation upgrading, steam reforming, bio oil steam catalytic pyrolysis, catalytic esterification, emulsification, these methods exist equipment complexity, the easy inactivation of catalyzer or cost than problems such as height.The composition that has been determined in the bio oil surpasses hundreds of, it is less but be worth very high Chemicals and paid close attention to by Many researchers and businessman to reclaim wherein content, and the separation and purification technology becomes the subject matter of its commercialization efficiently, cheaply, has only the extraction of the seasonings of foodstuffs industry to be widely used at present.In the bio oil separation method commonly used at present, still-process can cause the original structure of bio oil to change, and coking is serious; Solvent extraction and column chromatography cost height, be difficult to industrialization; The biomass pyrolysis liquefaction technology can only be mixed the material of all boiling ranges in the bio oil simultaneously the valuable ingredients that makes in the bio oil and both be mixed with high-load water, self also highly mixes, for bio oil as an alternative the industrial chemicals of fuel and high value all be great obstacle.This also is the insurmountable for a long time technical barrier in rapidly pyrolysing and liquefying biomass field, has limited further developing of liquefaction technology.
Summary of the invention
The objective of the invention is to overcome that organic constituent mixes with the large quantity of moisture height in the bio oil of producing in existing rapidly pyrolysing and liquefying biomass field, the problem of later separation difficulty, a kind of high bio oil component of water content of isolating in advance is provided, obtains that water content is low, the device and method of bio oil is produced in the biomass vacuum thermal cracking classification of the high bio oil of organic content.
For realizing above purpose, the present invention has taked following technical scheme: the device of bio oil is produced in the biomass vacuum thermal cracking classification, comprise interconnective vacuum thermal cracking reaction unit, first condenser system, second condenser system and vacuum-control(led) system, this vacuum thermal cracking reaction unit comprises that inside is provided with the fixed-bed reactor of silk screen interlayer, the temperature controller that is equipped with electric heater unit and is electrically connected in this reactor outer periphery with this electric heater unit, this temperature controller the other end is connected with the thermopair that is inserted into fixed-bed reactor inside, this reactor upper end is connected with vacuum meter, and is communicated with first condenser system by export pipeline; Described first condenser system includes the multi-stage condensing pipe that is communicated with export pipeline and reaches and a plurality of liquid traps of its paired, be equipped with the one-level condensing works in this liquid trap outer periphery, each prolong front end in the described multi-stage condensing pipe is provided with the prolong early gate, and pneumatic outlet is provided with the liquid trap late gate behind described each liquid trap.
With being provided with the multi-layer silk screen interlayer in the fixed bed reactor, in the biomass material that clean dry is crossed is housed, reactor temperature can be contrasted design temperature easily and effectively and be opened or close heat-processed automatically by thermocouple measurement, temperature controller control; The reactor upper end is provided with cavity, and pyrolysis gas outlet is arranged on the cavity sidewalls, and there is the vacuum meter connected entrance of measurement of vacuum the cavity upper end; The multi-stage condensing pipe comprises a plurality of condensation channels, respectively by controlling with the liquid trap late gate before each channel condensing pipe, utilize the jacketed type prolong with the organic steam condensation, and be collected in the liquid trap, according to the pyrolysis temperature difference, open before the corresponding prolong and liquid trap after valve, with this interval organic steam condensation, collection that produces, the bio oil classification of the interval thermo-cracking generation of differing temps is collected in the different liquid traps like this.Cooling medium in the prolong chuck is a mixture of ice and water.
Described second condenser system includes the B-grade condensation device.The B-grade condensation device can prevent that bio oil steam from being detached the quality that influences pump oil to the vacuum pump rapidly, causes the vacuum pump stall.
Be provided with ice-water bath in the described one-level condensing works.
Be provided with frozen water salt (sodium-chlor) (expression salt is sodium-chlor) mixture in the described B-grade condensation device.First non-condensable gas that forms in condenser system is discharged behind B-grade condensation device time condensation, and frozen water salt may command condensing temperature is got off the bio oil composition condensation of trace below 0 ℃.
Described vacuum-control(led) system includes the surge flask that is communicated with the B-grade condensation device, and this surge flask is communicated with vacuum pump by electrovalve, is connected with low-vacuum load-tripping device between electrovalve and surge flask, and this vacuum pump the other end is communicated with air hatch.The vacuum tightness of whole device realizes that by the terminal vacuum pump that connects of device by low-vacuum load-tripping device control, system pressure maintains between 3500～4000Pa.
Be filled with the granulated dried agent in the described export pipeline.The employing siccative can effectively be removed the water vapour composition in the organic steam.
Described granulated dried agent is activated alumina or anhydrous magnesium sulfate.These two kinds of siccative drying properties are good, easily regeneration, and difficult absorption bio oil component prevents to influence productive rate.
Described silk screen interlayer is stainless steel.Employing Stainless Steel Cloth interlayer also is not easy oxidized under the environment of fixed bed reactor high temperature and is out of shape, and has reduced the generation of impurity simultaneously, brings inorganic ash content to bio oil.
The present invention also has the method that the bio oil device is produced in this biomass vacuum thermal cracking classification of a kind of application, comprises the steps:
(1) will be filled into the silk screen interlayer through the biomass material after cleaning, drying, and this silk screen interlayer will be placed in the fixed-bed reactor,, open vacuum pump, the check system resistance to air loss thermopair insertion reaction device inside;
(2) open the preceding and No. 1 liquid trap late gate of prolong No. 1, close other valves, open the electric heater unit that is arranged on the fixed-bed reactor periphery, carry out heat temperature raising;
(3) when pyrolysis temperature at 170～300 ℃, the residence time is when remaining on 4～8 minutes, the pyrolysis steam that generates in the fixed-bed reactor detaches reactor rapidly and enters liquid trap No. 1 by No. 1 prolong;
(4) after temperature in the fixed-bed reactor arrives 300 ℃, open the preceding and No. 2 liquid trap late gates of prolong No. 2, close the preceding and No. 1 liquid trap late gate of prolong No. 1, pyrolysis temperature is in the time of 300～500 ℃, the residence time remained between 26～29 minutes, and the bio oil that reaction generates is collected in No. 2 liquid traps;
(5) when temperature in the fixed-bed reactor reaches 500 ℃, open the preceding and No. 3 liquid trap late gates of prolong No. 3, close the preceding and No. 2 liquid trap late gates of prolong No. 2, stop heating, the fixed bed reaction actuator temperature rises to 515 ± 5 ℃ naturally under the effect of electric heater unit waste heat, remain between 14～18 minutes 500～515 ± 5 ℃ of residence time, the bio oil that reaction generates is collected in No. 3 liquid traps;
(6) the fixed bed reaction actuator temperature rises to 515 ± 5 ℃ naturally, open the preceding and No. 4 liquid trap late gates of prolong No. 4, close the preceding and No. 3 liquid trap late gates of prolong No. 3, continue to keep vacuum state, naturally cooling, temperature of reactor is reduced to 100 ± 10 ℃, and the bio oil that reaction generates also is to be collected in No. 4 liquid traps, close vacuum pump, the unlatching reactor is also cleared up;
(7) non-condensable gas that is generated in above-mentioned each step passes through the second condenser system time condensation after the vacuum pump emptying.
Fine powders such as biomass material such as timber, stalk, rice husk are through cleaning, 105 ℃ of oven dry are after 24 hours, get and fill up each silk screen interlayer in right amount, insert in the fixed-bed reactor, tighten sealing with flange, seal, vacuumize, when vacuum tightness reaches 3500～4000Pa in the system, open electric heater unit, heat temperature raising is when temperature raises, pyrolysis gas is detached reactor rapidly by outlet, the interval organic steam that produces of differing temps is introduced different prolongs, and then import the different vessels collection, non-condensable gas is by emptying behind the vacuum pump.
The present invention compared with prior art, have following advantage: the present invention is in conjunction with the characteristics of bio oil production process and the characteristic of composition, with the vacuum thermal cracking reaction unit with the bio oil classification is produced and utilization combines, with the differing temps interval, the bio oil classification of the different residence time is produced, separate in advance and refinement bio oil component, can be with the extract phase combination of energy utilization and Chemicals, embodied good and economic again, be the later use bio oil, realize that biomass one chemical lays the foundation, solved in the bio oil of pyrolysis reactors such as traditional fluidized-bed preparation, water combined with polarity organic constituent height when overall moisture content was high, be difficult to the problem of separating and utilizing, expanded the scope that bio oil is used, significant for the sustainable supply of the energy and materials industry.
Description of drawings
Fig. 1 is apparatus of the present invention structural representation;
Fig. 2 is a principle of the invention block diagram;
Description of reference numerals: 1, temperature controller, 2, electric heater unit, 3, the silk screen interlayer, 4, thermopair, 5, vacuum meter, 6, fixed-bed reactor, 7, export pipeline, 8, the granulated dried agent, 9, the multi-stage condensing pipe, 10, the prolong early gate, 11, the liquid trap late gate, 12, liquid trap, 13, the one-level condensing works, 14, ice-water bath, 15, the mixture of frozen water salt and sodium-chlor, 16, the B-grade condensation device, 17, low-vacuum load-tripping device, 18, electrovalve, 19, air hatch, 20, surge flask, 21, vacuum pump, 111, the vacuum thermal cracking reaction unit, 112, first condenser system, 113, second condenser system, 114, vacuum-control(led) system.
Embodiment
With embodiment content of the present invention is described in further details in conjunction with the accompanying drawings down.
Embodiment:
See also shown in Figure 1, the device of bio oil is produced in a kind of biomass vacuum thermal cracking classification, comprise interconnective vacuum thermal cracking reaction unit 111, first condenser system 112, second condenser system 113 and vacuum-control(led) system 114, this vacuum thermal cracking reaction unit 111 comprises that inside is provided with the fixed-bed reactor 6 of the silk screen interlayer 3 of stainless steel, the temperature controller 1 that is equipped with electric heater unit 2 and is electrically connected in these reactor 6 outer periphery with this electric heater unit 2, this temperature controller 1 the other end is connected with the thermopair 4 that is inserted into fixed-bed reactor 6 inside, these reactor 6 upper ends are connected with vacuum meter 5, and are communicated with first condenser system 112 by export pipeline 7; First condenser system 112 includes the multi-stage condensing pipe 9 that is communicated with export pipeline 7 and reaches and a plurality of liquid traps 12 of its paired, be equipped with one-level condensing works 13 in these liquid trap 12 outer periphery, be provided with ice-water bath 14 within it, each prolong front end in the multi-stage condensing pipe 9 is provided with prolong early gate 10, and each liquid trap 12 back pneumatic outlet is provided with liquid trap late gate 11.
See also shown in Figure 2ly, the multi-stage condensing pipe 9 of present embodiment is made up of 1 to No. 4 prolong, all is provided with valve 10 before each prolong, is provided with liquid trap 12 equally 1 to No. 4 with this prolong pairing.
Also have second condenser system 113 that is connected between first condenser system 112 and the vacuum-control(led) system 114, be provided with B-grade condensation device 16 in this second condenser system 113, be provided with frozen water salt (sodium-chlor) mixture 15 within it.
Vacuum-control(led) system 114 includes the surge flask 20 that is communicated with second condenser system 113, this surge flask 20 is communicated with vacuum pump 21 by electrovalve 18, be connected with low-vacuum load-tripping device 17 between electrovalve 18 and surge flask 20, these vacuum pump 21 the other ends are communicated with air hatch 19.
Present embodiment is filled with the granulated dried agent 8 of activated alumina or anhydrous magnesium sulfate for effectively removing the water vapour composition in the organic steam in export pipeline 7.
In conjunction with said apparatus, the step that bio oil is produced in the classification of present embodiment biomass vacuum thermal cracking is as follows: screening biomass pine powder 40～60 orders wash twice with clear water, squeeze the water out, and place 105 ℃ of oven dry of baking oven 24 hours, during often stir wood powder; After the wood powder drying, fill up the Stainless Steel Cloth interlayer 3 of fixed-bed reactor 6 respectively, use flange seal, tighten the screws inserts thermopair 4, with all valve opens of first condenser system 111, open vacuum pump 21, observe vacuum meter 5, guarantee system sealing, vacuum tightness arrives standard, system pressure maintains between 3500～4000Pa, open electric heater unit 2, open No. 1 prolong early gate and liquid trap late gate, close other valves.When the thermo-cracking temperature rises to 170 ℃, suspend heating, pyrolysis this moment steam begins to generate, and detached reactor rapidly, enter No. 1 condensing tube condensation and become liquid, and collect in No. 1 liquid trap, when treating that temperature rises to 300 ℃, it is 4～8 minutes 170～300 ℃ the residence time; Open electric heater unit 2, open the preceding and liquid trap late gate of prolong rapidly No. 2, close the preceding and liquid trap late gate of prolong No. 1, when thermo-cracking temperature to 440 ℃, suspend heating, pyrolysis steam is detached, condensation and collecting when treating that temperature rises to 500 ℃ in No. 2 liquid traps, and in the time of 300～500 ℃, the residence time is 26～29 minutes; Close before No. 2 prolongs and the liquid trap late gate, opens before No. 3 prolongs and the liquid trap late gate, temperature rises naturally, and during 515 ± 5 ℃ of arrival top temperatures, the residence time between 500 ℃～top temperature is 14～18 minutes; When temperature begins to descend, open the preceding and liquid trap late gate of prolong No. 4, close the preceding and liquid trap late gate of prolong No. 3, continue to keep vacuum state, naturally cooling, when temperature of reactor was reduced to 100 ± 10 ℃, the vacuum thermal cracking reaction finished, close vacuum pump, open reactor and remove byproduct of reaction---wood charcoal powder on the stainless (steel) wire interlayer.
Be among the above embodiment in the table 1, the experimental data of bio oil is produced in the classification of pine powder vacuum thermal cracking, as seen the bio oil that generates between 300～500 ℃ accounts for 75.73% of bio oil total amount, the bio oil productive rate reaches 43.22% under this temperature and residence time control, and water-content reduces more than 1/3 than other temperature sections.When table 2 was 20 ℃/minute of definite values for heat-up rate in the thermal cracking processes, the experimental data of bio oil was produced in classification, and the bio oil moisture content between 300～500 ℃ raises 14%, and it is nearly 20% that mass ratio reduces, and the bio oil overall yield reduces by 11.3%.
Bio oil parameter (retention time of control pyrolysis temperature) is produced in the classification of table 1 vacuum cracking
Bio oil parameter (20 ℃/minute of temperature rise rates) is produced in the classification of table 2 vacuum cracking
Above-listed detailed description is at the specifying of possible embodiments of the present invention, and this embodiment is not in order to limiting claim of the present invention, and the equivalence that all the present invention of disengaging do is implemented or change, all should be contained in the claim of this case.
Claims (10)
1, the device of bio oil is produced in a kind of biomass vacuum thermal cracking classification, it is characterized in that: comprise interconnective vacuum thermal cracking reaction unit (111), first condenser system (112), the two or two condenser system (113) and vacuum-control(led) system (114), this vacuum thermal cracking reaction unit (111) comprises that inside is provided with the fixed-bed reactor of silk screen interlayer (3) (6), the temperature controller (1) that is equipped with electric heater unit (2) and is electrically connected in this reactor (6) outer periphery with this electric heater unit (2), this temperature controller (1) the other end is connected with and is inserted into the inner thermopair (4) of fixed-bed reactor (6), this reactor (6) upper end is connected with vacuum meter (5), and is communicated with first condenser system (112) by export pipeline (7); Described first condenser system (112) includes the multi-stage condensing pipe (9) that is communicated with export pipeline (7) and reaches and a plurality of liquid traps of its paired (12), be equipped with one-level condensing works (13) in this liquid trap (12) outer periphery, each prolong front end in the described multi-stage condensing pipe (9) is provided with prolong early gate (10), and described each liquid trap (12) back pneumatic outlet is provided with liquid trap late gate (11).
2, the device of bio oil is produced in biomass vacuum thermal cracking classification as claimed in claim 1, it is characterized in that: described second condenser system (113) includes B-grade condensation device (16).
3, the device of bio oil is produced in biomass vacuum thermal cracking classification as claimed in claim 2, it is characterized in that: be provided with ice-water bath (14) in the described one-level condensing works (13).
4, the device of bio oil is produced in biomass vacuum thermal cracking classification as claimed in claim 3, it is characterized in that: be provided with frozen water salt (sodium-chlor) mixture (15) in the described B-grade condensation device (16).
5, produce the device of bio oil as arbitrary described biomass vacuum thermal cracking classification in the claim 1 to 4, it is characterized in that: described vacuum-control(led) system (114) includes the surge flask (20) that is communicated with B-grade condensation device (16), this surge flask (20) is communicated with vacuum pump (21) by electrovalve (18), be connected with low-vacuum load-tripping device (17) between electrovalve (18) and surge flask (20), this vacuum pump (21) the other end is communicated with air hatch (19).
6, the device of bio oil is produced in biomass vacuum thermal cracking classification as claimed in claim 5, it is characterized in that: be filled with granulated dried agent (8) in the described export pipeline (7).
7, the device of bio oil is produced in biomass vacuum thermal cracking classification as claimed in claim 6, it is characterized in that: described granulated dried agent (8) is activated alumina or anhydrous magnesium sulfate.
8, the device of bio oil is produced in biomass vacuum thermal cracking classification as claimed in claim 7, it is characterized in that: described silk screen interlayer (3) is stainless steel.
9, a kind ofly be applied to the method that the bio oil device is produced in the classification of claim 1 biomass vacuum thermal cracking, it is characterized in that, comprise the steps:
(1) will be filled into the silk screen interlayer through the biomass material after cleaning, drying, and this silk screen interlayer will be placed in the fixed-bed reactor,, open vacuum pump, the check system resistance to air loss thermopair insertion reaction device inside;
(2) open the preceding and No. 1 liquid trap late gate of prolong No. 1, close other valves, open the electric heater unit that is arranged on the fixed-bed reactor periphery, carry out heat temperature raising;
(3) when pyrolysis temperature at 170～300 ℃, the residence time is when remaining on 4～8 minutes, the pyrolysis steam that generates in the fixed-bed reactor detaches reactor rapidly and enters liquid trap No. 1 by No. 1 prolong;
(4) after temperature in the fixed-bed reactor arrives 300 ℃, open the preceding and No. 2 liquid trap late gates of prolong No. 2, close the preceding and No. 1 liquid trap late gate of prolong No. 1, pyrolysis temperature is in the time of 300～500 ℃, the residence time remained between 26～29 minutes, and the bio oil that reaction generates is collected in No. 2 liquid traps;
(5) when temperature in the fixed-bed reactor reaches 500 ℃, beat and rise the preceding and No. 3 liquid trap late gates of prolong No. 3, close the preceding and No. 2 liquid trap late gates of prolong No. 2, stop heating, the fixed bed reaction actuator temperature rises to 515 ± 5 ℃ naturally under the effect of electric heater unit waste heat, remain between 14～18 minutes 500 ℃～515 ± 5 ℃ residence time, the bio oil that reaction generates is collected in No. 3 liquid traps;
(6) the fixed bed reaction actuator temperature rises to 515 ± 5 ℃ naturally, open the preceding and No. 4 liquid trap late gates of prolong No. 4, close the preceding and No. 3 liquid trap late gates of prolong No. 3, continue to keep vacuum state, naturally cooling, temperature of reactor is reduced to 100 ± 10 ℃, and the bio oil that reaction generates also is to be collected in No. 4 liquid traps, close vacuum pump, the unlatching reactor is also cleared up;
(7) non-condensable gas that is generated in the above steps passes through the second condenser system time condensation after the vacuum pump emptying.
10, the method for bio oil is produced in biomass vacuum thermal cracking classification as claimed in claim 9, it is characterized in that: described biomass material is timber, stalk or rice husk particle.
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| CN101805647A (en) * | 2010-04-23 | 2010-08-18 | 倪建辉 | Method for preparing natural gas by biomass material thermal cracking and thermal cracking furnace used by same |
| CN102070403A (en) * | 2011-01-10 | 2011-05-25 | 东南大学 | Method for preparing polyalcohol type and saturated furan nucleus type compounds from biological oil |
| CN102226095A (en) * | 2011-05-27 | 2011-10-26 | 中国科学院过程工程研究所 | Device and method for preparing fuel and chemicals by gradient pyrolysis of biomass and step-by-step collection |
| CN102459517A (en) * | 2009-06-02 | 2012-05-16 | 芬欧汇川公司 | Method of carrying out pyrolysis and pyrolysis apparatus |
| CN101613617B (en) * | 2009-07-23 | 2012-07-04 | 东南大学 | Method for preparing biological oil through vacuum pyrolysis of biomasses |
| CN102676259A (en) * | 2012-04-18 | 2012-09-19 | 吉林大学 | Preparation method and novel using methods of carbon monolith binder |
| CN103396821A (en) * | 2013-07-23 | 2013-11-20 | 浙江工业大学 | Cracking reaction device and method of preparing biological oil based on bagasse quick cracking |
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| CN102459517A (en) * | 2009-06-02 | 2012-05-16 | 芬欧汇川公司 | Method of carrying out pyrolysis and pyrolysis apparatus |
| CN101613617B (en) * | 2009-07-23 | 2012-07-04 | 东南大学 | Method for preparing biological oil through vacuum pyrolysis of biomasses |
| CN101805647A (en) * | 2010-04-23 | 2010-08-18 | 倪建辉 | Method for preparing natural gas by biomass material thermal cracking and thermal cracking furnace used by same |
| CN102070403A (en) * | 2011-01-10 | 2011-05-25 | 东南大学 | Method for preparing polyalcohol type and saturated furan nucleus type compounds from biological oil |
| CN102070403B (en) * | 2011-01-10 | 2014-01-22 | 东南大学 | Method for preparing polyalcohol type and saturated furan nucleus type compounds from biological oil |
| CN102226095A (en) * | 2011-05-27 | 2011-10-26 | 中国科学院过程工程研究所 | Device and method for preparing fuel and chemicals by gradient pyrolysis of biomass and step-by-step collection |
| CN102226095B (en) * | 2011-05-27 | 2014-01-15 | 中国科学院过程工程研究所 | Device and method for preparing fuel and chemicals by gradient pyrolysis of biomass and step-by-step collection |
| CN102676259A (en) * | 2012-04-18 | 2012-09-19 | 吉林大学 | Preparation method and novel using methods of carbon monolith binder |
| CN103396821A (en) * | 2013-07-23 | 2013-11-20 | 浙江工业大学 | Cracking reaction device and method of preparing biological oil based on bagasse quick cracking |
| CN104046374A (en) * | 2014-06-12 | 2014-09-17 | 江苏大学 | Device and method for quickly preparing bio-oil by catalytically cracking biomass pyrolysis vapor on line |
| CN105176550A (en) * | 2015-10-28 | 2015-12-23 | 湖南炭道新能源科技有限公司 | Continuous carbonizing device and method |
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