CN102226094A - Method for preparing biomass fuel by pyrolysis liquefaction of biomass - Google Patents
Method for preparing biomass fuel by pyrolysis liquefaction of biomass Download PDFInfo
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- CN102226094A CN102226094A CN2011101245939A CN201110124593A CN102226094A CN 102226094 A CN102226094 A CN 102226094A CN 2011101245939 A CN2011101245939 A CN 2011101245939A CN 201110124593 A CN201110124593 A CN 201110124593A CN 102226094 A CN102226094 A CN 102226094A
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- biomass
- pyrolysis liquefaction
- fuel
- pyrolysis
- oil
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
- C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
- C10G1/086—Characterised by the catalyst used
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a method for preparing a biomass fuel by pyrolysis liquefaction of a biomass raw material, which comprises the following steps: conducting pyrolysis liquefaction of biomass raw material granules in the presence of a basic catalyst in a liquid fuel solvent under pressure of 1-6 atmospheres and temperature of 200-300 DEG C, and separating the obtained pyrolysis liquefied products into biomass fuel products of different boiling ranges.
Description
Technical field
The present invention relates to further development and utilization to biomass material, particularly biomass waste, be specifically related to the biomass material pyrolysis liquefaction to prepare the method for biomass fuel, described biomass fuel comprises biomass light oil, biodiesel and biomass heavy oil.
Background technology
Under the industry background of China, have a large amount of biomass wastes, concrete example such as bagasse, vinasse slag, manioc waste, straw, straw, beans stalk, cotton stalk, cornstalk, corn cob, fallen leaves and wood chip etc. contain a large amount of macromolecular substance that can further utilize such as xylogen, Mierocrystalline cellulose, hemicellulose and starch etc. usually in these biomass wastes.In recent years, under the overall background of green low-carbon, the further development and utilization of these biomass wastes is more and more received publicity.
Biomass pyrolytic is a kind of thermochemical method, wherein there is not oxygenant or only providing under the condition of limited oxygenant, make macromolecular substance such as decomposition such as xylogen, Mierocrystalline cellulose, hemicellulose and starch in the biomass be converted into bio-oil, charcoal and inflammable gas by thermal chemical reaction, and can by control thermal chemical reaction condition as temperature, pressure and the residence time wait change as described in ratio between the product, oxygenant described herein such as air, oxygen, water or steam etc.
In the prior art, because biomass pyrolysis process can produce tar, therefore all very high to the requirement of the collection of bio oil and cooling apparatus.For example, in the biomass fast pyrogenation process, the temperature that pyrolysis product leaves reactor is generally 400-500 ℃, this moment, pyrolysis product mostly was gaseous state greatly, in subsequent process, can result in blockage after these gaseous product condensations with solid particulate fouling on pipeline and equipment surface, and then the carrying out continuously of influence process operation, be unfavorable for described technology industrialization, simultaneously also can the influence process yield.
In addition, in the prior art, also there are some problems in the biomass pyrolytic technology, for example, the production cost of bio-oil is usually than mineral innage, and bio-oil can not be directly used in available dynamic equipment, this is because bio-oil is the hydrocarbon polymer of physics and the equal less stable of chemical property mostly, must could use through modification and/or refinement treatment.
Situation based on prior art, it is bio-oil with the biomass waste pyrolysis liquefaction in the liquid fuel within solvent under lower temperature conditions under lower pressure that the present invention seeks a kind of, then the bio-oil fractionation is obtained the method for biomass light oil, biodiesel and biomass heavy oil, thereby can further utilize described biomass waste, a kind of energy derive of Sustainable development is provided.
Summary of the invention
The invention provides a kind of pyrolysis liquefaction biomass to prepare the method for biomass fuel, described method is included in basic catalyst and exists in the liquid fuel within solvent down under 1-6 atmospheric pressure and make the biomass raw material particle pyrolysis liquefaction and the pyrolysis liquefaction product that obtains is separated into the biomass fuel product of different boiling ranges under 200-300 ℃ temperature.
In the method for preparing biomass fuel of the present invention, described biomass material is generally biomass waste, specifically is selected from bagasse, vinasse slag, manioc waste, straw, straw, beans stalk, cotton stalk, cornstalk, corn cob, fallen leaves and wood chip etc.Therefore, for method of the present invention, the source of described biomass material is still very abundant.
In the method for preparing biomass fuel of the present invention, described biomass material is generally through pulverizing and screening is handled and obtained granularity and be less than or equal to about 300 microns (about 50 orders), preferably be less than or equal to the biomass raw material particle of about 200 microns (about 70 orders), pulverize and generally undertaken by Mechanical Crushing, screening then utilizes standard sieve to carry out, to obtain the biomass raw material particle of needed specified particle size scope.
In the method for preparing biomass fuel of the present invention, if described biomass material water content is excessive, then generally dry in advance described biomass material, for example utilize drying machines such as whirlwind to carry out drying, preferably be dried to water-content and be lower than 10wt%, more preferably be dried to water-content and be lower than 5wt%, thereby be beneficial to follow-up pulverizing of described biomass material and screening processing.
In the method for preparing biomass fuel of the present invention, described basic catalyst can be this area any suitable basic catalyst commonly used, be preferably the alkali or the salt of basic metal or alkaline-earth metal, the carbonate of basic metal or alkaline-earth metal more preferably, most preferably be yellow soda ash, salt of wormwood and lime carbonate, with the consumption of described basic catalyst be the 0.2-5wt% of described biomass raw material particle gross weight, be preferably 0.5-3wt%.
In the method for preparing biomass fuel of the present invention, described liquid fuel solvent can be this area any suitable liquid fuel commonly used, the preferred cheap not volatile liquid fuel of price comparison, be specifically as follows not volatile oily liquid fuel such as heavy oil and coal tar and heavy oil component and coal tar component, wherein said heavy oil component such as heavy oil lighting end, described coal tar component such as naphtalene oil, washing oil, carbolineum and anthracene oil, preferred carbolineum and/or the washing oil of using is as described liquid fuel solvent, can suitably select with the weight ratio of described liquid fuel solvent and described biomass raw material particle, be generally 10: 1 to 3: 1, be preferably 8: 1 to 3: 1, most preferably be 6: 1 to 3: 1.
In the method for preparing biomass fuel of the present invention, described biomass raw material particle can be carried out pyrolysis liquefaction in existing in the prior art any suitable reactor, described pyrolyzing and liquefying reactor can be for example circulating fluid bed reactor, bubbling bed reactor, but be preferably reactor class reactor, more preferably have the stainless steel cauldron of stirring rake.
More preferably, in the method for preparing biomass fuel of the present invention, described biomass raw material particle is under 1-6 atmospheric pressure, under preferred 1-3 the atmospheric pressure, more preferably under atmospheric pressure in having the stainless steel cauldron of stirring rake, carry out pyrolysis liquefaction, wherein under stirring condition heat temperature raising to 200-300 ℃, preferred heat temperature raising is to 215-290 ℃, more preferably heat temperature raising is to 230-280 ℃, with the rotating speed of stirring rake be 100-400 rev/min, be preferably 130-350 rev/min, more preferably 150-300 rev/min, with the residence time of described reaction mixture in described reactor be 0.6-5 hour, be preferably 0.8-4.5 hour, more preferably 1-4 hour.
In the method for preparing biomass fuel of the present invention, described pyrolysis liquefaction product can be separated into the biomass fuel product of different boiling ranges by separation processes such as rectifying, the rectifying device that is adopted can be commonly used any suitable rectifying device in this area such as rectifying tower etc., can be separated into the biomass light oil of different boiling ranges with described pyrolysis liquefaction product, biodiesel and biomass heavy oil, wherein the boiling range scope of biomass light oil can be 110-180 ℃, cat head at rectifying tower obtains, the boiling range scope of biodiesel can be 180-365 ℃, in the side line extraction of the middle part of rectifying tower, can at the bottom of the tower of rectifying tower, obtain for more than 365 ℃ with the boiling range scope of biomass heavy oil.
Preferably, in the method for preparing biomass fuel of the present invention, described biomass light oil can be used for being specifically as follows described stainless steel cauldron heat being provided for described pyrolysis liquefaction process provides heat, thereby can realize the heat self-sufficiency of described pyrolysis liquefaction process to small part; The calorific value of described biodiesel is 33-36MJ/kg, can be used for substituting or the alternative conventional heavy diesel of part; With the calorific value of described biomass heavy oil be 35-38MJ/kg, can be used for substituting conventional oil fuel.
In the method for preparing biomass fuel of the present invention, the transformation efficiency that described biomass raw material particle pyrolysis liquefaction produces bio-oil is generally 70-96wt%, is preferably 75-95wt%.
According to the present invention, the described method for preparing biomass fuel has obviously improved product yield, technological process is simple relatively, and employed equipment also is the common equipment of prior art, therefore, method of the present invention is carried out industry easily and is amplified, but continuous production, possess good industrial prospect, and then can select fuel for fuel market provides generation.
Description of drawings
Fig. 1 is the schema that is prepared the method for biomass fuel by the biomass material pyrolysis liquefaction of the present invention.
Embodiment
With reference to Fig. 1, pyrolysis liquefaction biomass material of the present invention can carry out according to following process with the method for preparing biomass fuel:
Biomass material such as corn cob are dried to water-content are lower than 10wt%, then through Mechanical Crushing with for example utilize that the screening of 50 purpose standard sieves obtains the biomass raw material particle that granularity is less than or equal to 300 microns;
Select for example carbolineum and for example in container for stirring mix at 5: 1 to scale of liquid fuel solvent with described biomass raw material particle, and to wherein adding selected basic catalyst such as yellow soda ash, the add-on of yellow soda ash is counted for example 3wt% with the weight of described biomass raw material particle, and further mixes;
In the stainless steel cauldron that have stirring rake of uniform reaction mixture adding that obtains previously as pyrolyzing and liquefying reactor, described reactor can be normal-pressure reaction kettle or the compressive reaction still that has steam jacket, for example can be forced under 1-6 the atmospheric pressure, under preferred 1-3 the atmospheric pressure, wherein under agitation condition heat temperature raising to for example 230-280 ℃, the rotating speed of stirring rake is for example 1-4 hour for for example 150-300 rev/min and the residence time of described reaction mixture in described reactor; With
Continuously the product of extraction pyrolysis liquefaction is a bio-oil from described reactor, the bio-oil of extraction is pumped into rectifying tower carries out rectifying, thereby obtain the biomass fuel of different boiling ranges;
Particularly, can obtain the boiling range scope from the cat head of rectifying tower and be 110-180 ℃ biomass light oil, it from rectifying tower middle part side line extraction boiling range scope 180-365 ℃ biodiesel, with obtain the boiling range scope at the bottom of the rectifying Tata is biomass heavy oil more than 365 ℃, and wherein said biomass light oil can be used for providing heat for described stainless steel cauldron, for example can be used for producing the steam of the described reactor of heating, thereby can realize the heat self-sufficiency of pyrolysis liquefaction process of the present invention to small part.
Further describe method of the present invention by following embodiment, but described embodiment is not used in and limits the scope of the invention.
Embodiment
The pyrolysis liquefaction of embodiment 1 bagasse
A certain amount of bagasse is dried to water-content is lower than 10wt%, pulverize and sieve the solid particulate that obtains below 30 gram 50 orders (300 microns) then; With described solid particulate and 120 gram washing oil and 1 gram Na
2CO
3In container, mix; The gained reaction mixture joined in 0.5 liter the stainless steel cauldron, heat temperature raising to 230 ℃ under agitation condition, the mixing speed that is adopted is 300 rev/mins, the residence time of reaction mixture in reactor is 3 hours, and the bio-oil that pyrolysis liquefaction obtains obtains biomass light oil 3.45 grams, biodiesel 75 grams and biomass heavy oil 70 grams through rectifying separation.As calculated as can be known, the product yield of pyrolysis liquefaction is about 98.97% among this embodiment.In addition, through measuring, the calorific value of resulting three kinds of biofuels is 36MJ/kg.
The pyrolysis liquefaction of embodiment 2 corn cobs
A certain amount of corn cob is dried to water-content is lower than 10wt%, pulverize and sieve the solid particulate that obtains below 30 gram 70 orders (200 microns) then; With described solid particulate and 120 gram carbolineums and 1.2 gram CaCO
3In container, mix; The gained reaction mixture joined in 0.5 liter the stainless steel cauldron, heat temperature raising to 260 ℃ under agitation condition, the mixing speed that is adopted is 200 rev/mins, the residence time of reaction mixture in reactor is 2.5 hours, and the bio-oil that pyrolysis liquefaction obtains obtains biomass light oil 3.05 grams, biodiesel 70 grams and biomass heavy oil 74 grams through rectifying separation.As calculated as can be known, the product yield of pyrolysis liquefaction is about 98.03% among this embodiment.In addition, through measuring, the calorific value of resulting three kinds of biofuels is 35MJ/kg.
The pyrolysis liquefaction of embodiment 3 cotton stalks
A certain amount of cotton stalk is dried to water-content is lower than 10wt%, pulverize and sieve the solid particulate that obtains below 30 gram 60 orders (250 microns) then; With described solid particulate and 120 gram washing oil and 0.6 gram K
2CO
3In container, mix; The gained reaction mixture joined in 0.5 liter the stainless steel cauldron, heat temperature raising to 240 ℃ under agitation condition, the mixing speed that is adopted is 350 rev/mins, the residence time of reaction mixture in reactor is 4 hours, and the bio-oil that pyrolysis liquefaction obtains obtains biomass light oil 2.95 grams, biodiesel 69 grams and biomass heavy oil 72 grams through rectifying separation.As calculated as can be known, the product yield of pyrolysis liquefaction is about 95.97% among this embodiment.In addition, through measuring, the calorific value of resulting three kinds of biofuels is 37MJ/kg.
Claims (9)
1. a pyrolysis liquefaction biomass material is to prepare the method for biomass fuel, described method is included in basic catalyst and exists in the liquid fuel within solvent down under 1-6 atmospheric pressure and make the biomass raw material particle pyrolysis liquefaction and the pyrolysis liquefaction product that obtains is separated into the biomass fuel product of different boiling ranges under 200-300 ℃ temperature.
2. the process of claim 1 wherein that described biomass material is the biomass waste that is selected from bagasse, vinasse slag, manioc waste, straw, straw, beans stalk, cotton stalk, cornstalk, corn cob, fallen leaves and wood chip.
3. claim 1 or 2 method wherein are dried to water-content in advance with described biomass material and are lower than 10wt%, and the granularity that preferably is lower than 5wt% and described biomass raw material particle is less than or equal to about 300 microns, preferably is less than or equal to about 200 microns.
4. each method of claim 1-3, wherein said basic catalyst is the carbonate of basic metal or alkaline-earth metal, the consumption that is preferably yellow soda ash, salt of wormwood and lime carbonate and described basic catalyst is the 0.2-5wt% of described biomass raw material particle gross weight, is preferably 0.5-3wt%.
5. each method of claim 1-4, wherein said liquid fuel solvent is selected from heavy oil and coal tar and heavy oil component and coal tar component, be preferably selected from carbolineum and washing oil, with the weight ratio of described liquid fuel solvent and described biomass raw material particle be 10: 1 to 3: 1, be preferably 8: 1 to 3: 1, most preferably be 6: 1 to 3: 1.
6. each method of claim 1-5, wherein said pyrolysis feed particle is under 1-3 the atmospheric pressure, preferably under atmospheric pressure having in the stainless steel cauldron of stirring rake and carrying out pyrolysis liquefaction, wherein under agitation condition heat temperature raising to 215-290 ℃, preferred heat temperature raising is to 230-280 ℃, with the rotating speed of stirring rake be 100-400 rev/min, be preferably 130-350 rev/min, more preferably 150-300 rev/min.
7. the method for claim 6, the residence time of wherein said reaction mixture in described reactor is 0.6-5 hour, is preferably 0.8-4.5 hour, more preferably 1-4 hour.
8. each method of claim 1-7, wherein said pyrolysis liquefaction product separates by rectifying and the biomass fuel product of described different boiling ranges comprises that the boiling range scope is that 110-180 ℃ biomass light oil, biodiesel that the boiling range scope is 180-365 ℃ and boiling range scope are the biomass heavy oil more than 365 ℃.
9. the method for claim 8 wherein utilizes described biomass light oil to provide heat for pyrolysis liquefaction process.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110124593.9A CN102226094B (en) | 2011-05-16 | 2011-05-16 | Method for preparing biomass fuel by pyrolysis liquefaction of biomass |
| PCT/CN2011/079512 WO2012155414A1 (en) | 2011-05-16 | 2011-09-09 | Method for preparing biomass fuel by pyrolyzing and liquefying biomass |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201110124593.9A CN102226094B (en) | 2011-05-16 | 2011-05-16 | Method for preparing biomass fuel by pyrolysis liquefaction of biomass |
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| CN102226094A true CN102226094A (en) | 2011-10-26 |
| CN102226094B CN102226094B (en) | 2014-03-12 |
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| WO (1) | WO2012155414A1 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102559324A (en) * | 2011-12-12 | 2012-07-11 | 广西力源宝农林科技发展有限责任公司 | Method for preparing biomass fuel by utilizing processing residua of cassava |
| WO2012155414A1 (en) * | 2011-05-16 | 2012-11-22 | 科威国际技术转移有限公司 | Method for preparing biomass fuel by pyrolyzing and liquefying biomass |
| CN102899097A (en) * | 2012-09-20 | 2013-01-30 | 西安益众环保产业有限公司 | Biomass liquid fuel and production method thereof |
| CN104226229A (en) * | 2014-10-10 | 2014-12-24 | 苏州新协力环保科技有限公司 | Biomass fuel reactor |
| CN105664801A (en) * | 2016-04-19 | 2016-06-15 | 河南城建学院 | Gas/liquid switching feeding device and heavy organic matter pyrolysis device |
| CN106147914A (en) * | 2015-04-02 | 2016-11-23 | 天津市澍丰农业科技有限公司 | A kind of clean type bio-fuel |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109060406B (en) * | 2018-08-21 | 2020-03-13 | 嘉兴新嘉爱斯热电有限公司 | Automatic sampling and analyzing system for biomass fuel |
| DE102019001696A1 (en) * | 2019-03-11 | 2020-09-17 | Olaf Heimbürge | Plant and process for the catalytic production of diesel oils from organic materials |
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| CN102226094B (en) * | 2011-05-16 | 2014-03-12 | 科威国际技术转移有限公司 | Method for preparing biomass fuel by pyrolysis liquefaction of biomass |
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- 2011-09-09 WO PCT/CN2011/079512 patent/WO2012155414A1/en active Application Filing
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| JP2006063310A (en) * | 2004-07-27 | 2006-03-09 | Univ Nihon | Method and apparatus for producing wood-biomass-derived liquid fuel |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012155414A1 (en) * | 2011-05-16 | 2012-11-22 | 科威国际技术转移有限公司 | Method for preparing biomass fuel by pyrolyzing and liquefying biomass |
| CN102559324A (en) * | 2011-12-12 | 2012-07-11 | 广西力源宝农林科技发展有限责任公司 | Method for preparing biomass fuel by utilizing processing residua of cassava |
| CN102899097A (en) * | 2012-09-20 | 2013-01-30 | 西安益众环保产业有限公司 | Biomass liquid fuel and production method thereof |
| CN102899097B (en) * | 2012-09-20 | 2015-06-03 | 西安益众环保产业有限公司 | Biomass liquid fuel and production method thereof |
| CN104226229A (en) * | 2014-10-10 | 2014-12-24 | 苏州新协力环保科技有限公司 | Biomass fuel reactor |
| CN106147914A (en) * | 2015-04-02 | 2016-11-23 | 天津市澍丰农业科技有限公司 | A kind of clean type bio-fuel |
| CN105664801A (en) * | 2016-04-19 | 2016-06-15 | 河南城建学院 | Gas/liquid switching feeding device and heavy organic matter pyrolysis device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102226094B (en) | 2014-03-12 |
| WO2012155414A1 (en) | 2012-11-22 |
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