CN1803982A - Mobile biomass liquefaction system - Google Patents
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- CN1803982A CN1803982A CN 200510137113 CN200510137113A CN1803982A CN 1803982 A CN1803982 A CN 1803982A CN 200510137113 CN200510137113 CN 200510137113 CN 200510137113 A CN200510137113 A CN 200510137113A CN 1803982 A CN1803982 A CN 1803982A
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Abstract
The disclosed mobile biomass liquefaction system comprising: a biomass gasification furnace, a fuel decontamination plant, a fuel generating set, a biomass pyrolysis furnace with heat from the firing of gasified fuel and incondensable gas, a cooling tower, and a pretreatment device. This system realizes complete self-support for energy, can convert the biomass into bio-oil locally for further centralized treatment, and has high operation efficiency for wide application range.
Description
Technical field
The present invention relates to biomass liquefaction system.
Background technology
Biomass are the renewable resourcess that can be converted into liquid fuel, its liquid product has advantages such as environmental friendliness, energy density height, easy storage, easy transportation, the fuel that both can be used as boiler, internal combustion turbine, engine can therefrom extract the Chemicals with commercial value again.
Developed at present multiple different biomass pyrolysis liquefaction device, as the vacuum reactor of the rotation awl reactor of the fluidized-bed reactor of Canadian Waterloo university exploitation, the exploitation of Dutch Twente university and the exploitation of Canadian Laval university.Yet fluidized-bed reactor endogenous substance and the horizontal mixed characteristic of bed material are not good, and higher carrier gas material ratio causes serious wear, the capacity usage ratio of material and equipment low and equipment volume is big; There is mechanical movement in the rotation awl reactor, is out of order easily under the high temperature; Vacuum reactor energy consumption height, volume is big, oil yield rate is low.
Do not concentrate because biomass resource has distribution, the characteristics that energy density is low are subjected to the restriction of transportation cost, existing pyrolysis installation or small, economy is not good, or can only be in the place that biomass material is relatively concentrated, as building large-scale plant near the large-scale wood-working factory.And in fact the agricultural as China is national, and a large amount of available biomass resources are agricultural wastes such as straw, cotton stalk, maize straw, husk, and they are only in a certain season, and a certain place has suitable amount usable.In this case, as adopt movably that liquefying plant just can be translated into liquid fuel in the biomass material place of production earlier, concentrate again to store and utilize, thereby improve the utilization ratio of device and the economy of operation greatly.Movable liquefied matching requirements energy consumption as far as possible little (preferably can self-supporting), compact construction and be applicable to various types of biomass materials, but existing equipment can't satisfy these requirements fully.
Summary of the invention
The objective of the invention is to overcome above-mentioned the deficiencies in the prior art part, a kind of mobile biomass liquefaction system is proposed, this biomass liquefaction system compact construction, can be neatly directly throughout the biomass material place of production be translated into the bio oil of being convenient to transport, and operation institute of system energy requirement is self-supporting fully, the running efficiency of system height.
For achieving the above object, the technical solution used in the present invention is: feeding machine, biomass gasifying furnace, first cyclonic separator, the coke tar cracking stove, blower fan, gas-holder links to each other successively with the fuel gas generation unit, feed bin, screw feeder, biomass pyrolysis furnace, second cyclonic separator, cooling tower, liquid bath links to each other successively with oil tank, liquid bath links to each other with interchanger by recycle pump, interchanger links to each other with cooling tower, cooling tower all links to each other with settling chamber by recirculation blower with gas-holder, air preheater links to each other with settling chamber, settling chamber links to each other with biomass pyrolysis furnace, biomass pyrolysis furnace links to each other with air preheater, air preheater links to each other with biomass gasifying furnace, and gas blower links to each other with air preheater.
The present invention's advantage compared to existing technology is:
1. the electricity consumption of total system and all directly come from biomass with heat has solved the problem that common pyrolysis plant needs the electrical network energy supply.
2. carry the equipment of biomass cutting, drying, pulverizing, guarantee to be applicable to dissimilar biomass materials.
3. biomass pyrolysis furnace adopts the specially designed spouted bed bioreactor that has annular flow wind transmission chamber and tilting fluidized wind air distribution plate, guarantees material full contact, biomass fast pyrogenation, has overcome the problem of other pyrolysis oven fluidisation inequality; In spouted bed bioreactor, the high-temperature flue gas heat release of adopting pyrolysis non-condensable gas and partial gasification fuel gas buring to produce provides biomass pyrolytic required heat, has avoided existing biomass pyrolysis furnace to cause the excessive problem of load volume by the carrier gas heat release fully.
4. can to adopt with the charcoal be that the fixed-bed reactor of catalyzer remove tar, the sewage handling problem of avoiding other treating plant to need water consumption and bring to the coke tar cracking stove; Or to adopt the coke that produces with biomass pyrolytic be that the fixed-bed reactor of catalyzer remove tar, further improved the independence of system.
5. interchanger adopts the temperature of hot tube heat exchanger reduction cooling tower spray liquid, the heat transfer efficiency height, and compact construction has been avoided adopting water cooling to need the problem of water source and water cooling tower.
6. cooling tower adopts the condensation of the present invention's design, the cooling tower of demist one, and compact construction overcomes common cooling system complexity, bulky deficiency.
7. adopt air preheater and loft drier, utilize hot smoke pre-heating air, dried biomass, make full use of waste heat, improve the utilization ratio of system capacity.
8. mobile biomass liquefaction system proposed by the invention, all devices all can be delivered by transportation means such as automobiles, institute's energy requirement is supplied with by biomass fully, need not outer other power supply of biomass, just can be translated into the bio oil of being convenient to transport in the biomass place of production, be applicable to the liquefaction processing of the biomass resource of different sorts and scale, have flexibly, the height of characteristics, and operational efficiency easily.
Description of drawings
Fig. 1 is the schematic flow sheet of a kind of embodiment of mobile biomass liquefaction system of the present invention.
Fig. 2 is the structural representation of a kind of embodiment of biomass pyrolysis furnace among Fig. 1.
Fig. 3 is the A-A sectional view of Fig. 2.
Fig. 4 is the B-B sectional view of Fig. 2.
Fig. 5 is the C-C sectional view of Fig. 3.
Fig. 6 is the structural representation of a kind of embodiment of cooling tower among Fig. 1.
Fig. 7 is the D-D sectional view of Fig. 6.
Fig. 8 is the schematic flow sheet of the another kind of embodiment of mobile biomass liquefaction system of the present invention.
Fig. 9 arranges front view on Fig. 8 system car.
Figure 10 arranges vertical view on Fig. 8 system car.
Embodiment
The present invention is described in further detail below in conjunction with accompanying drawing.
By shown in Figure 1, feeding machine 2, biomass gasifying furnace 1, first cyclonic separator 3, coke tar cracking stove 4, blower fan 5, gas-holder 6 links to each other successively with fuel gas generation unit 7, feed bin 23, screw feeder 9, biomass pyrolysis furnace 8, second cyclonic separator 10, cooling tower 11, liquid bath 12 links to each other successively with oil tank 13, liquid bath 12 links to each other with interchanger 15 by recycle pump 14, interchanger 15 links to each other with cooling tower 11, cooling tower 11 all links to each other with settling chamber 17 by recirculation blower 16 with gas-holder 6, air preheater 19 links to each other with settling chamber 17, settling chamber 17 links to each other with biomass pyrolysis furnace 8, biomass pyrolysis furnace 8 links to each other with air preheater 19, air preheater 19 links to each other with biomass gasifying furnace 1, and gas blower 18 links to each other with air preheater 19.
Between the inlet mouth of the air outlet of biomass gasifying furnace 1 and first cyclonic separator 3, between the inlet mouth of the air outlet of first cyclonic separator 3 and coke tar cracking stove 4, between the import of the air outlet of coke tar cracking stove 4 and blower fan 5, between the outlet of blower fan 5 and the gas-holder 6, all use pipe connection between the inlet mouth of gas-holder 6 and fuel gas generation unit 7, pipeline junction all seals.
Between the opening for feed of the discharge port of feed bin 23 and screw feeder 9, all directly be connected between the opening for feed of the discharge port of screw feeder 9 and biomass pyrolysis furnace 8, the junction all seals.
Between the inlet mouth of the air outlet of biomass pyrolysis furnace 8 and second cyclonic separator 10, between the inlet mouth of the air outlet of second cyclonic separator 10 and cooling tower 11, between the import of liquid bath 12 and recycle pump 14, between the import of the outlet of recycle pump 14 and interchanger 15, all use pipe connection between the shower of the outlet of interchanger 15 and cooling tower 11, pipeline junction all seals.
Between the leakage fluid dram of cooling tower 11 and the liquid bath 12, all directly be connected between liquid bath 12 and the oil tank 13, the junction all seals.
Between the import of the air outlet of cooling tower 11 and recirculation blower 16, between the import of gas-holder 6 and recirculation blower 16, between the outlet of recirculation blower 16 and the settling chamber 17, between air preheater 19 and the settling chamber 17, between the inlet mouth of settling chamber 17 and biomass pyrolysis furnace 8, all use pipe connection between the exchanging air import of settling chamber 17 and biomass pyrolysis furnace 8, pipeline junction all seals.
Between the exchanging air outlet and air preheater 19 of biomass pyrolysis furnace 8, between the inlet mouth of air preheater 19 and biomass gasifying furnace 1, all use pipe connection between the outlet of gas blower 18 and the air preheater 19, pipeline junction all seals.
To deliver to biomass gasifying furnace 1 through cutting and dry pretreated biomass by feeding machine 2, under the effect of gasifying medium preheated air, gasify, the temperature out of biomass gasifying furnace 1 is generally 900 ℃, first cyclonic separator 3 is removed the solid particulate in the gasification burning, coke tar cracking stove 4 is with the catalytic cracking of tar in the gasification burning, gasification burning after cracking purifies is transported to 7 generatings of fuel gas generation unit by blower fan 5 through gas-holder 6, satisfies the need for electricity of total system.
To deliver to biomass pyrolysis furnace 8 less than the biomass material of 2mm through pulverizing pretreated particle diameter by screw feeder 9, and contact decomposes with hot quartz sand in biomass pyrolysis furnace 8, and produce coke, condensated gas and non-condensable gas, pyrolysis temperature can be 500 ℃.Coke, condensated gas and non-condensable gas are delivered to second cyclonic separator 10, coke is captured by second cyclonic separator 10, condensated gas becomes bio oil 11 li of cooling towers with low temperature spray liquid condensation by contact, and bio oil is through liquid bath 12 oil tank 13 of packing into, and the bio oil of production stores with oil tank 13.The bio-oil phase composition on liquid bath 12 tops after interchanger 15 coolings, is transported to cooling tower 11 sprayings formation low temperature spray liquid as heat-eliminating medium by recycle pump 14.
Non-condensable gas is removed entrained water smoke and mist of oil through cooling tower 11.The non-condensable gas and the part of having removed water smoke and mist of oil from cooling tower 11 are transported to settling chamber 17 from the gasification burning of gas-holder 6 by recirculation blower 16, carry, burn through the air mixed of air preheater 19 preheatings in settling chamber 17 and by gas blower 18,900 ℃ of high-temperature flue gas that burning produces are transported to biomass pyrolysis furnace 8.
By Fig. 2～shown in Figure 5, the structure of biomass pyrolysis furnace 8 is, the tilting fluidized wind air distribution plate 32 in the bottom of upper shell 25, and fluidized wind air distribution plate 32 seals with the junction of upper shell 25, fluidized wind air distribution plate 32 joins with the jet pipe 30 that is positioned at lower shell 29 bottoms, its junction sealing, fluidized wind air distribution plate 32, form annular flow wind transmission chamber between jet pipe 30 and the lower shell 29, its junction sealing, have blast inlet 31 in the bottom of lower shell 29, emulsion zone at burner hearth, hearth outer wall is furnished with wall chuck 27, vertically being separated of wall chuck 27 by a plurality of spreader plates 37, on the spreader plate 37, on lower edge and the wall chuck 27, leave the gap between the lower surface, the space that is separated laterally is divided into by dividing plate 34, following two portions, respectively with the upper port of the interior pipe laying of in the emulsion zone of burner hearth, arranging 35, lower port communicates, have heat exchange gas approach 33 in the lower end of wall chuck 27, the upper end has heat exchange exhanst gas outlet 26, have opening for feed 28 in the bottom of upper shell 25, top has air outlet 36.
High-temperature flue gas part in the settling chamber 17 feeds biomass pyrolysis furnace 8 direct heating quartz sand and biomass as fluidized wind through jet pipe 30 and blast inlet 31, another part is through the indirect heat release of heat-transfer surface of heat exchange gas approach 33 and interior pipe laying 35, and they provide biomass pyrolytic required heat jointly.Wherein, be used for the flue gas cool-down of indirect heat exchange after, through air preheater 19 preheated airs, the further smoke exhaust system after the cooling.Preheated air part in the air preheater 19 is used for biomass gasifying furnace 1 and makes gasifying medium, and a part is used for settling chamber 17.
By Fig. 6, shown in Figure 7, the structure of cooling tower 11 is, have inlet mouth 39 at the middle part of tower body 38, put in shower 42 above inlet mouth 39, shower 42 can not be exposed at outside the wall, also can be exposed at outside the wall, shower 42 seals with the junction of tower body 38, and a plurality of nozzles 43 are arranged on the shower 42, has air outlet 41 at the top of tower body 38, the bottom has leakage fluid dram 44, between shower 42 and air outlet 41 mist eliminator 40 is housed.Mist eliminator 40 can adopt conventional traverse baffle mist eliminator or eddy flow plate mist eliminator, also can adopt the mist eliminator of types such as mesh mist eliminator, filler mist eliminator, and installs by common mode.
On the basis of Fig. 1, between biomass and feed bin 23, can be connected to cutting machine 20, loft drier 21, pulverizer 22, or be connected to wherein two kinds, or be connected to wherein a kind of.
By Fig. 8～shown in Figure 10, between biomass and feed bin 23, be connected to cutting machine 20, loft drier 21, pulverizer 22.Air preheater 19 is used pipe connection with loft drier 21, the pipeline junction sealing, and further the flue gas after the cooling is to 21 li dried biomass of loft drier.
Biomass material is cut into pieces through cutting machine 20, after drying case 21 dryings, delivers to feeding machine 2 and pulverizer 22, pulverizes through pulverizer 22, makes biological particles, delivers to feed bin 23 and stores, and is carried by screw feeder 9 again.
For example:
All devices of the present invention all by automobile 24 deliveries, supplied with by biomass fully by institute's energy requirement.
When system starts, the gasification burning that stores in advance in the gas-holder 6 is for 7 generatings of fuel gas generation unit, start blower fan 5, biomass gasifying furnace 1 igniting, behind the aerogenesis, start recirculation blower 16, gas blower 18, the bed material in the settling chamber 17 burning generation high-temperature flue gas heating biomass pyrolysis furnaces 8 is introduced in the partial gasification combustion gas, when reaching pyrolysis temperature, start screw feeder 9, beginning biomass pyrolytic system bio oil, start recycle pump 14 simultaneously, the bio oil that stores in advance in the liquid bath 12 is made spray liquid, progressively improves the treatment capacity of biomass gasifying furnace 1 and biomass pyrolysis furnace 8, improve the generated energy of fuel gas generation unit 7, be in the normal and continuous operation state until the system's all devices that comprises pre-processing device.
When system normally moved, biomass gasifying furnace 1 feeding coal was 130kg/h, and gas production rate is 300Nm
3/ h, gasification burning calorific value are 5000kJ/Nm
3, 210Nm wherein
3The gasification burning of/h is for 7 generatings of 40kW internal combustion unit; Biomass pyrolysis furnace 8 feeding coals are 100kg/h, and pyrolysis temperature is 500 ℃, and fluidizing velocity is 3m/s; Second cyclonic separator 10 is per hour collected coke 10kg; Cooling tower 11 per hour obtains bio oil 60kg.
250Nm
3The non-condensable gas of/h and 90Nm
3The gasification burning of/h and 100Nm
3/ h temperature is that 400 ℃ preheated air produces 420Nm in settling chamber 17 mixed firings
3/ h temperature is 900 ℃ high-temperature flue gas, wherein 230Nm
3The high-temperature flue gas of/h is as bed material and biomass in the fluidized wind direct heating biomass pyrolysis furnace 8, remaining high-temperature flue gas provides biomass pyrolytic required heat through the wall chuck 27 and the indirect heat release of interior pipe laying 35 heat-transfer surfaces of biomass pyrolysis furnace 8, and this part flue gas is subsequently through tubular air preheater 19 heating 200Nm
3/ h air to 400 ℃, and be used for dried biomass at last.Blower fan 5, recirculation blower 16, gas blower 18, the about 25kW of recycle pump 14 total powers, cutting machine 20, the about 15kW of pulverizer 22 total powers.
Claims (9)
1. mobile biomass liquefaction system is characterized in that:
Feeding machine (2), biomass gasifying furnace (1), first cyclonic separator (3), coke tar cracking stove (4), blower fan (5), gas-holder (6) links to each other successively with fuel gas generation unit (7), feed bin (23), screw feeder (9), biomass pyrolysis furnace (8), second cyclonic separator (10), cooling tower (11), liquid bath (12) links to each other successively with oil tank (13), liquid bath (12) links to each other with interchanger (15) by recycle pump (14), interchanger (15) links to each other with cooling tower (11), cooling tower (11) all links to each other with settling chamber (17) by recirculation blower (16) with gas-holder (6), air preheater (19) links to each other with settling chamber (17), settling chamber (17) links to each other with biomass pyrolysis furnace (8), biomass pyrolysis furnace (8) links to each other with air preheater (19), air preheater (19) links to each other with biomass gasifying furnace (1), and gas blower (18) links to each other with air preheater (19).
2. mobile biomass liquefaction system according to claim 1 is characterized in that: also be connected to cutting machine (20), loft drier (21), pulverizer (22), or be connected to wherein two kinds, or be connected to wherein a kind of.
3. mobile biomass liquefaction system according to claim 1 and 2, it is characterized in that: the structure of biomass pyrolysis furnace (8) is, at the tilting fluidized wind air distribution plate in the bottom of upper shell (25) (32), fluidized wind air distribution plate (32) joins with the jet pipe (30) that is positioned at lower shell (29) bottom, fluidized wind air distribution plate (32), form annular flow wind transmission chamber between jet pipe (30) and the lower shell (29), have blast inlet (31) in the bottom of lower shell (29), emulsion zone at burner hearth, hearth outer wall is furnished with wall chuck (27), vertically being separated of wall chuck (27) by a plurality of spreader plates (37), on the spreader plate (37), on lower edge and the wall chuck (27), leave the gap between the lower surface, the space that is separated laterally is divided into by dividing plate (34), following two portions, respectively with the upper port of the interior pipe laying of in the emulsion zone of burner hearth, arranging (35), lower port communicates, have heat exchange gas approach (33) in the lower end of wall chuck (27), the upper end has heat exchange exhanst gas outlet (26), have opening for feed (28) in the bottom of upper shell (25), top has air outlet (36).
4. mobile biomass liquefaction system according to claim 1 and 2, it is characterized in that: the structure of cooling tower (11) is, have inlet mouth (39) at the middle part of tower body (38), put in shower (42) in the top of inlet mouth (39), a plurality of nozzles (43) are arranged on the shower (42), have air outlet (41) at the top of tower body (38), the bottom has leakage fluid dram (44), between shower (42) and air outlet (41) mist eliminator (40) is housed.
5. mobile biomass liquefaction system according to claim 3, it is characterized in that: the structure of cooling tower (11) is, have inlet mouth (39) at the middle part of tower body (38), put in shower (42) in the top of inlet mouth (39), a plurality of nozzles (43) are arranged on the shower (42), have air outlet (41) at the top of tower body (38), the bottom has leakage fluid dram (44), between shower (42) and air outlet (41) mist eliminator (40) is housed.
6. mobile biomass liquefaction system according to claim 1 and 2 is characterized in that: biomass gasifying furnace (1) is the downdraft fixed-bed gasification furnace.
7. mobile biomass liquefaction system according to claim 1 and 2 is characterized in that: coke tar cracking stove (4) is a fixed bed catalytic reactor.
8. mobile biomass liquefaction system according to claim 1 and 2 is characterized in that: interchanger (15) is a hot tube heat exchanger.
9. mobile biomass liquefaction system according to claim 1 and 2 is characterized in that: air preheater (19) is a tubular preheater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101371137A CN100340637C (en) | 2005-12-31 | 2005-12-31 | Mobile biomass liquefaction system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005101371137A CN100340637C (en) | 2005-12-31 | 2005-12-31 | Mobile biomass liquefaction system |
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| CN1803982A true CN1803982A (en) | 2006-07-19 |
| CN100340637C CN100340637C (en) | 2007-10-03 |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101818892A (en) * | 2010-05-04 | 2010-09-01 | 张建臣 | Straw fuel flying furnace |
| CN101502286B (en) * | 2009-03-23 | 2011-03-30 | 罗泽宽 | Mobile drying machine for biomass fuel |
| CN101671570B (en) * | 2009-09-08 | 2012-08-15 | 北京林业大学 | Miniature movable type agricultural and forest biomass fast pyrolysis device |
| CN102863976A (en) * | 2012-10-11 | 2013-01-09 | 南京瑞恰新能源科技有限公司 | Vehicular straw treatment system and vehicular straw treatment method |
| CN103146403A (en) * | 2013-03-22 | 2013-06-12 | 清华大学 | Biomass pyrolysis system and method through self-sufficient energy |
| CN105642655A (en) * | 2016-01-29 | 2016-06-08 | 杭州能态思特科技有限公司 | Domestic garbage treatment method, device and mobile machinery shop |
| CN106590706A (en) * | 2016-12-21 | 2017-04-26 | 北京林业大学 | Vehicle-mounted biomass pyrolysis liquefaction system |
| CN108977226A (en) * | 2018-09-30 | 2018-12-11 | 广州威能机电有限公司 | The electricity-generating method of biomass power generation system and application biomass |
| WO2019029599A1 (en) * | 2017-08-11 | 2019-02-14 | 武汉丰盈长江生态科技研究总院有限公司 | Mobile platform-based micro biomass synthetic oil method and system |
| CN115449389A (en) * | 2022-09-20 | 2022-12-09 | 陕西煤业化工技术研究院有限责任公司 | Internal heating type low-temperature pyrolysis furnace and working method thereof |
| EP4065890A4 (en) * | 2019-11-29 | 2023-12-20 | Royal Melbourne Institute of Technology | A system and method for pyrolysis |
| CN115449389B (en) * | 2022-09-20 | 2024-05-03 | 陕西煤业化工技术研究院有限责任公司 | Internal heating type low-temperature pyrolysis furnace and working method thereof |
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| CN2484328Y (en) * | 2001-07-16 | 2002-04-03 | 中国科学院广州能源研究所 | Self-heating type circulating fluidizing-bed biological-material pyrolytic oiling apparatus |
| CN1417290A (en) * | 2001-11-01 | 2003-05-14 | 中国科学技术大学 | Low-cost and pollution-less biomass liquefying process and equipment |
| CN2578337Y (en) * | 2002-10-18 | 2003-10-08 | 山东理工大学 | Biomass pyrolytic liquefier |
| CN1181160C (en) * | 2002-10-18 | 2004-12-22 | 山东理工大学 | Biomass pyrolysis liquefying systems |
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2005
- 2005-12-31 CN CNB2005101371137A patent/CN100340637C/en not_active Expired - Fee Related
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| CN101502286B (en) * | 2009-03-23 | 2011-03-30 | 罗泽宽 | Mobile drying machine for biomass fuel |
| CN101671570B (en) * | 2009-09-08 | 2012-08-15 | 北京林业大学 | Miniature movable type agricultural and forest biomass fast pyrolysis device |
| CN101818892A (en) * | 2010-05-04 | 2010-09-01 | 张建臣 | Straw fuel flying furnace |
| CN101818892B (en) * | 2010-05-04 | 2012-07-18 | 张建臣 | Straw fuel flying furnace |
| CN102863976A (en) * | 2012-10-11 | 2013-01-09 | 南京瑞恰新能源科技有限公司 | Vehicular straw treatment system and vehicular straw treatment method |
| CN103146403B (en) * | 2013-03-22 | 2014-05-21 | 清华大学 | Biomass pyrolysis system and method through self-sufficient energy |
| CN103146403A (en) * | 2013-03-22 | 2013-06-12 | 清华大学 | Biomass pyrolysis system and method through self-sufficient energy |
| CN105642655A (en) * | 2016-01-29 | 2016-06-08 | 杭州能态思特科技有限公司 | Domestic garbage treatment method, device and mobile machinery shop |
| CN106590706A (en) * | 2016-12-21 | 2017-04-26 | 北京林业大学 | Vehicle-mounted biomass pyrolysis liquefaction system |
| WO2019029599A1 (en) * | 2017-08-11 | 2019-02-14 | 武汉丰盈长江生态科技研究总院有限公司 | Mobile platform-based micro biomass synthetic oil method and system |
| CN108977226A (en) * | 2018-09-30 | 2018-12-11 | 广州威能机电有限公司 | The electricity-generating method of biomass power generation system and application biomass |
| EP4065890A4 (en) * | 2019-11-29 | 2023-12-20 | Royal Melbourne Institute of Technology | A system and method for pyrolysis |
| CN115449389A (en) * | 2022-09-20 | 2022-12-09 | 陕西煤业化工技术研究院有限责任公司 | Internal heating type low-temperature pyrolysis furnace and working method thereof |
| CN115449389B (en) * | 2022-09-20 | 2024-05-03 | 陕西煤业化工技术研究院有限责任公司 | Internal heating type low-temperature pyrolysis furnace and working method thereof |
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| CN100340637C (en) | 2007-10-03 |
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