CN102408901A - Method for quick thermal cracking of biomass and device thereof - Google Patents
Method for quick thermal cracking of biomass and device thereof Download PDFInfo
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- CN102408901A CN102408901A CN2011103088627A CN201110308862A CN102408901A CN 102408901 A CN102408901 A CN 102408901A CN 2011103088627 A CN2011103088627 A CN 2011103088627A CN 201110308862 A CN201110308862 A CN 201110308862A CN 102408901 A CN102408901 A CN 102408901A
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Abstract
A method for quick thermal cracking of biomass and a device thereof are disclosed, relating to the thermal cracking of biomass. The device is provided with a feeding bin, an automatic feeding device, a mass flow instrument, a gas preheater, a thermal cracking reactor, a separator, a biochar collector, a cooler, a circulating pump, a chilling tower, a tower bottom temporary-storage tank, a first biomass oil collecting tank, a water cooling condenser, a second biomass oil collecting tank, an ice water condenser and a third biomass oil collecting tank. The method comprises: a step of conveying the biomass material into a thermal cracking reactor through a feeding mechanism; a step of performing thermal cracking on the biomass material in the thermal cracking reactor and performing gas-solid separation on thermal cracking steam and ash content in a separator; a step of spraying the thermal cracking steam in the chilling tower to obtain first-stage bio-oil; and a step of condensing the thermal cracking steam in the water cooling condenser to obtain second-stage bio-oil and further condensing the thermal cracking steam in the ice water condenser to obtain third-stage bio-oil. The biomass is high in oil yield and wide in application range.
Description
Technical field
The present invention relates to a kind of biomass through pyrolysis, especially relate to a kind of method and device thereof of biomass fast pyrolysis.
Background technology
Along with the high speed development of China's economic, the insufficient contradiction of power supply is outstanding day by day, and crude oil in China dependence on import problem is serious.Therefore, fully base oneself upon national resource and develop the alternative energy, particularly biomass energy,,, realize that Sustainable development has great importance for guaranteeing national energy security to reduce dependence to oil.Biomass energy is as unique renewable energy source that can be converted into liquid fuel, is to be only second to coal, oil and natural gas and the energy that occupy the 4th of world energy sources total quantity consumed, in whole energy resource system, occupies critical role.Biomass are meant the organic substance that all directly or indirectly utilize green plants photosynthesis to form, and comprise plant, animal and mikrobe and drainage and metabolite etc. except that fossil oil.Biomass fast pyrolysis is the importance that biomass energy is used; It can be with biomass material; Like stalk, wood chip, processing of farm products waste material etc., be converted into high-grade bio-oil, this technology to the requirement of biomass material be water cut be lower than 10% with particle diameter less than 2mm.Biomass fast pyrolysis is meant under oxygen-free environment; Biomass are heated rapidly to higher reaction temperatures, cause macromolecular decomposition, produce the process of micro-molecular gas and condensability volatile matter and a small amount of coke; The condensability volatile matter is cooled to flowable liquids fast, is referred to as bio-oil.Bio-oil has the pungency smell of burning, high-density (～1200kg/m
3), acid (pH value 2.8～3.8) and than low heat value (14～18.5MJ/kg).The bio-oil complicated component; Comprise hundreds of compounds such as acids, aldehydes, ketone, furans, single water-cooling pattern with in the thermo-cracking steam all can condensation bio-oil concentrate in together, can not the bio-oil classification be collected; Be unfavorable for that bio-oil using in the scope widely; Simultaneously, because the heat exchange of water-cooled condensing mode is not good, cause the bio-oil productive rate lower.Like Chinese patent CN200510057216.2 disclosed " a kind of process method and apparatus system thereof of biomass through pyrolysis liquefaction " and CN201110006196.1 disclosed " a kind of biomass through pyrolysis stove " etc.; All be the mode biomass collection oil that adopts water-cooled; This type of cooling can not the classification biomass collection oil; And, caused the bio-oil productive rate low because condensation effect is undesirable.
To this problem, the bio-oil gathering system of the application's case adopts high-pressure spraying, water-cooled and three ice-cold steps to thermo-cracking steam, can collect the bio-oil of heterogeneity, and can improve the bio-oil productive rate.
Summary of the invention
The objective of the invention is to the existing type of cooling can not the classification biomass collection oil; And because condensation effect is undesirable; Problems such as the bio-oil productive rate is low have been caused; A kind of productive rate that not only can improve bio-oil is provided, and obtains bio-oil, can improve the method and the device thereof of biomass fast pyrolysis of the range of application of bio-oil through fractional condensation.
Said biomass fast pyrolysis device is provided with and adds temporary storage tank at the bottom of feed bin, autofeed device, mass rate appearance, gas preheater, pyrolysis reactor, separator, charcoal scoop, water cooler, recycle pump, quenching column, the tower, the 1st bio-oil holding tank, water-cooled condenser, the 2nd bio-oil holding tank, water ice condenser, the 3rd bio-oil holding tank; The said discharge port that adds feed bin connects the biomass material import of pyrolysis reactor through the autofeed device; The import of mass rate appearance connects nitrogen inlet; The outlet of mass rate appearance connects the combi inlet port of pyrolysis reactor through gas preheater; The thermo-cracking steam charcoal of pyrolysis reactor and ash outlet connect the import of separator, and the charcoal of separator and ash outlet connect the import of charcoal scoop, and the thermo-cracking vapor outlet port of separator connects the import of quenching column; The outlet of the bio-oil of quenching column connects the import of temporary storage tank at the bottom of the tower; A way outlet of temporary storage tank connects the import of the 1st bio-oil holding tank at the bottom of the tower, and another way outlet of temporary storage tank connects quenching column through recycle pump and water cooler successively at the bottom of the tower, and quenching column is connected with water ice condenser with the 2nd bio-oil holding tank respectively through water-cooled condenser; The outlet of water ice condenser connects the 3rd bio-oil holding tank, the inlet that can not coagulating property pneumatic outlet connects the mass rate appearance of water ice condenser.
Said separator can be established the 1st grade of separator and the 2nd grade of separator; Said receipts thing charcoal scoop can be established the 1st grade of charcoal scoop and the 2nd grade of charcoal scoop, and the 1st grade of charcoal scoop is located at the 1st grade of separator lower end, and the 2nd grade of charcoal scoop established the 2nd grade of separator lower end.
Said pyrolysis reactor can adopt biomass bubbling fluidization bed bioreactor etc.
The not condensable gases that biomass through pyrolysis produces is as carrier gas.Perolene can adopt the silica sand that Heat stability is good, heat conduction are good, be difficult for powderised.
Said quenching column is a kind of device that makes the bio-oil condensation in the thermo-cracking steam, in this device, will spray medium through recycle pump and be compressed to high pressure conditions; Be injected in the thermo-cracking steam, obtain the bio oil of condensation, the bio oil that density is bigger deposits at the bottom of the tower in the temporary storage tank; The less spray medium of density flows out quenching column; Get into water cooler, discharge, to supply with spray use next time at the systemic heat of tower.
Temporary storage tank is not only collected the bio-oil that obtains in the quenching column at the bottom of the said tower, and temporary tank top also is furnished with spray medium high pressure spray nozzle at the bottom of the tower, guarantees that pyrolysis steam further obtains cooling in temporary storage tank at the bottom of the tower, strengthen the heat exchange effect.
The spray medium is meant lightweight bio-oil, methyl alcohol, hexanaphthene, hexane or n-dodecane etc., is that density is lower than bio-oil to the requirement that sprays medium.If the spray medium can mix with bio oil, then require it to be blended in the bio-oil and can the subsequent applications of bio-oil not impacted, but, preferably select and the immiscible spray medium of bio oil.
Said water-cooled condenser is through the circulating of water of condensation, and carries out wall-type heat exchange with thermo-cracking steam.
Said ice-cold condensing surface is meant the indirect heat exchange through mixture of ice and water and thermo-cracking steam, realizes the device of bio-oil condensation.
The method of said biomass fast pyrolysis adopts said biomass fast pyrolysis device, may further comprise the steps:
1) sends into the step in the pyrolysis reactor to biomass material through feeder;
2) in pyrolysis reactor, biomass material carried out thermo-cracking and in separator, thermo-cracking steam and charcoal and ash carried out the step of gas solid separation;
3) in quenching column, thermo-cracking steam is sprayed the step that obtains the one-level bio oil;
4) in water-cooled condenser, the thermo-cracking vapor condensation obtained two stage biological oil and in ice-cold condensing surface, the further condensation of thermo-cracking steam obtained the step of three grades of bio oil.
In step 1); The said step of sending into biomass material in the pyrolysis reactor through feeder is following: the not condensable gases that biomass through pyrolysis produces is as carrier gas; Through being preheated to 500～600 ℃; Flow into through gas distributor from the pyrolysis reactor bottom, make thermal barrier and biomass material be in fluidization; Pyrolysis reactor is preheated to 400～600 ℃ in advance, and biomass material gets into pyrolysis reactor under the effect of autofeed device, and the temperature rise rate with 500～1000 ℃/s heats in reactor drum.
In step 2) in; Said in pyrolysis reactor, biomass material to be carried out the step of thermo-cracking following: biomass material carries out thermo-cracking in pyrolysis reactor after; Thermo-cracking steam, charcoal and ash leave pyrolysis reactor and get into the two-stage solid separator, in the collection canister of separator lower end, collect charcoal and ash.
In step 3), said in quenching column, thermo-cracking steam to be sprayed the step that obtains the one-level bio oil following: the thermo-cracking steam that does not contain charcoal and ash gets into quenching column, uses to spray medium thermo-cracking steam is sprayed.The quenching column that this case is used is an internal-circulation type; With lightweight bio-oil, methyl alcohol, hexanaphthene, hexane or n-dodecane as the spray medium; Under the recycle pump effect, will spray medium and be increased to certain pressure, from the high pressure spray nozzle ejection of quenching column; Make the thermo-cracking vapor condensation of inflow become bio-oil, obtain first step bio-oil.
In step 4), said step in water-cooled condenser that thermo-cracking vapor condensation acquisition two stage biological is oily is following: after thermo-cracking steam leaves quenching column, get into water cooling heat exchanger, after cooling, obtain second stage bio-oil; Behind the thermo-cracking steam leaving water cold heat exchanger, flow into ice-cold interchanger, further condensation obtains third stage bio-oil.Thermo-cracking steam subsequently is condensable gases not, draws as carrier gas and gets back to the pyrolysis reactor bottom.
Said biomass are meant the organic substance that all directly or indirectly utilize green plants photosynthesis to form, and comprise plant, animal and mikrobe and drainage and metabolite etc. except that fossil oil.The present invention to the requirement of biomass material be water cut be lower than 10% with particle diameter less than 2mm.
Because therefore feeder outer wrap watercooling jacket has been stopped because of the heat conduction influence of pyrolysis reactor the situation that thermo-cracking took place before not getting into reactor drum part biological pledge material to be taken place.
Compared with prior art, the present invention has following outstanding advantage:
1) in the bio-oil quenching column; Most heavy bio-oil and a part of lightweight bio-oil component realize condensation in the thermo-cracking steam; This be since highly compressed spray medium through with the direct contact heat-exchanging of pyrolysis steam; Can strengthen the heat exchange effect of thermo-cracking steam, the bio-oil productive rate that obtains more than simple dividing wall type water-cooled condenser is high;
2) temporary storage tank is not only collected the bio-oil that obtains in the quenching column at the bottom of the tower, and the quenching column top also is furnished with spray medium high-pressure atomization nozzle, guarantees that pyrolysis steam further obtains cooling in temporary storage tank at the bottom of the tower, strengthen the heat exchange effect;
3) classification of bio-oil is collected and can also be obtained to have the bio-oil component of obvious difference, and convenient follow-up improving quality of biomass oil is purified, and increases the range of application of bio-oil;
4) the biomass through pyrolysis reactor drum that uses of the present invention is the bubbling fluidization bed bioreactor, and the maturation that possesses skills is easy to advantages such as amplification in the industry, and therefore, the bio-oil gathering system that adopts the present invention to use need not carried out bigger change to existing installation.
Description of drawings
Fig. 1 is that the structure of biomass fast pyrolysis device embodiment according to the invention is formed synoptic diagram.In Fig. 1, respectively be labeled as: add at the bottom of feed bin 1, autofeed device 2, nitrogen inlet 3, mass rate appearance 4, gas preheater 5, fluidized-bed reactor the 6, the 1st cyclonic separator the 7, the 1st charcoal scoop the 8, the 2nd cyclonic separator the 9, the 2nd charcoal scoop 10, water cooler 11, recycle pump 12, quenching column 13, the tower temporary storage tank the 14, the 1st biomass collection oil tank 15, water-cooled condenser the 16, the 2nd biomass collection oil tank 17, water ice condenser the 18, the 3rd biomass oil tank 19, condensable gases 20 not.
Fig. 2 is the structural representation of the quenching column of biomass fast pyrolysis device embodiment of the present invention.In Fig. 2, respectively be labeled as: pyrolysis steam-in 21, high pressure spray nozzle 22,23, Liquid level scale 24, cooling medium outlet 25, pyrolysis vapour outlet 26.
Embodiment
Following examples will combine accompanying drawing that the present invention is further described.
Referring to Fig. 1, biomass fast pyrolysis device embodiment according to the invention is provided with and adds at the bottom of feed bin 1, autofeed device 2, mass rate appearance 4, gas preheater 5, pyrolysis reactor 6, separator, charcoal scoop, water cooler 11, recycle pump 12, quenching column 13, the tower temporary storage tank the 14, the 1st bio-oil holding tank 15, water-cooled condenser the 16, the 2nd bio-oil holding tank 17, water ice condenser 18 and the 3rd bio-oil holding tank 19; The said discharge port that adds feed bin 1 connects the biomass material import of pyrolysis reactor 6 through autofeed device 2; The import of mass rate appearance 4 connects nitrogen inlet 3; The outlet of mass rate appearance 4 connects the combi inlet port of pyrolysis reactor 6 through gas preheater 5; The thermo-cracking steam charcoal of pyrolysis reactor 6 and ash outlet connect the import of separator; The charcoal of separator and ash outlet connect the import of charcoal scoop; The thermo-cracking vapor outlet port of separator connects the import of quenching column 13, and the outlet of the bio-oil of quenching column 13 connects the import of temporary storage tank 14 at the bottom of the tower, and a way outlet of temporary storage tank 14 connects the import of the 1st bio-oil holding tank 15 at the bottom of the tower; Another way outlet of temporary storage tank 14 connects quenching column 13 through recycle pump 12 and water cooler 11 successively at the bottom of the tower; Quenching column 13 is connected with water ice condenser 18 with the 2nd bio-oil holding tank 17 respectively through water-cooled condenser 16, and the outlet of water ice condenser 18 connects the 3rd bio-oil holding tank 19, the inlet that can not coagulating property pneumatic outlet connects mass rate appearance 4 of water ice condenser 18.
Said separator is established the 1st grade of separator 7 and the 2nd grade of separator 9; The 1st grade of charcoal scoop 8 established by said receipts thing charcoal scoop and 10, the 1 grades of charcoal scoops 8 of the 2nd grade of charcoal scoop are located at the 1st grade of separator 7 lower ends, and the 2nd grade of charcoal scoop 10 established the 2nd grade of separator 9 lower ends.
Said pyrolysis reactor can adopt biomass bubbling fluidization bed bioreactor etc.
The not condensable gases that biomass through pyrolysis produces is as carrier gas.Perolene can adopt the silica sand that Heat stability is good, heat conduction are good, be difficult for powderised.
Said quenching column is a kind of device that makes the bio-oil condensation in the thermo-cracking steam, in this device, will spray medium through recycle pump and be compressed to high pressure conditions; Be injected in the thermo-cracking steam, obtain the bio oil of condensation, the bio oil that density is bigger deposits at the bottom of the tower in the temporary storage tank; The less spray medium of density flows out quenching column; Get into water cooler, discharge, to supply with spray use next time at the systemic heat of tower.
Temporary storage tank is not only collected the bio-oil that obtains in the quenching column at the bottom of the said tower, and temporary tank top also is furnished with spray medium high pressure spray nozzle at the bottom of the tower, guarantees that pyrolysis steam further obtains cooling in temporary storage tank at the bottom of the tower, strengthen the heat exchange effect.
The spray medium is meant lightweight bio-oil, methyl alcohol, hexanaphthene, hexane or n-dodecane etc., is that density is lower than bio-oil to the requirement that sprays medium.If the spray medium can mix with bio oil, then require it to be blended in the bio-oil and can the subsequent applications of bio-oil not impacted, but, preferably select and the immiscible spray medium of bio oil.
Said water-cooled condenser is through the circulating of water of condensation, and carries out wall-type heat exchange with thermo-cracking steam.
Said ice-cold condensing surface is meant the indirect heat exchange through mixture of ice and water and thermo-cracking steam, realizes the device of bio-oil condensation.
The biomass through pyrolysis liquefaction technology step that realizes said goal of the invention comprises: send into the step in the pyrolysis reactor to biomass material through feeder; In pyrolysis reactor, biomass material carried out the step of thermo-cracking; In separator, thermo-cracking steam and charcoal and ash carried out the step of gas solid separation; In quenching column, thermo-cracking steam is sprayed the step that obtains the one-level bio oil; In water-cooled condenser, the thermo-cracking vapor condensation obtained the step of two stage biological oil, in ice-cold condensing surface, the further condensation of thermo-cracking steam obtained the step of three grades of bio oil.
Said biomass are meant the organic substance that all directly or indirectly utilize green plants photosynthesis to form, and comprise plant, animal and mikrobe and drainage and metabolite etc. except that fossil oil.The present invention to the requirement of biomass material be water cut be lower than 10% with particle diameter less than 2mm.
Because therefore feeder outer wrap watercooling jacket has been stopped because of the heat conduction influence of pyrolysis reactor the situation that thermo-cracking took place before not getting into reactor drum part biological pledge material to be taken place.
Said biomass through pyrolysis technological process is following:
1) the not condensable gases of biomass through pyrolysis generation, flows into through gas distributor from the pyrolysis reactor bottom through being preheated to 500～600 ℃ as carrier gas, makes thermal barrier and biomass material be in fluidization; Pyrolysis reactor is preheated to 400～600 ℃ in advance, and biomass material gets into pyrolysis reactor under the effect of autofeed device, and the temperature rise rate with 500～1000 ℃/s heats in reactor drum;
2) after biomass material carried out thermo-cracking in pyrolysis reactor, thermo-cracking steam, charcoal and ash left pyrolysis reactor and get into the two-stage solid separator, in the collection canister of separator lower end, collect charcoal and ash;
3) the thermo-cracking steam that does not contain charcoal and ash gets into quenching column, uses the spray medium that thermo-cracking steam is sprayed.The quenching column that this case is used is an internal-circulation type; With lightweight bio-oil, methyl alcohol, hexanaphthene, hexane or n-dodecane as the spray medium; Under the recycle pump effect, will spray medium and be increased to certain pressure, from the high pressure spray nozzle ejection of quenching column; Make the thermo-cracking vapor condensation of inflow become bio-oil, obtain first step bio-oil;
4) after thermo-cracking steam leaves quenching column, get into water cooling heat exchanger, after cooling, obtain second stage bio-oil; Behind the thermo-cracking steam leaving water cold heat exchanger, flow into ice-cold interchanger, further condensation obtains third stage bio-oil;
5) subsequently thermo-cracking steam is condensable gases not, draws as carrier gas and gets back to the pyrolysis reactor bottom.
Below provide specific embodiment:
Biomass are stored in and add in the feed bin, under the effect of autofeed device, from the middle part entering inside reactor of fluidized-bed reactor; Condensable gases does not mix with nitrogen, entering gas preheater under the control of mass rate appearance, and the gas after the preheating gets in the reactor drum from the bottom of fluidized-bed reactor; Make biomass material and thermal barrier be in fluidized state, biomass material carries out thermo-cracking in pyrolysis reactor after, thermo-cracking steam, charcoal and ash leave pyrolysis reactor and get into the two-stage separator; In the charcoal scoop of separator lower end, collect charcoal and ash; The thermo-cracking steam that does not contain charcoal and ash gets into quenching column, through cooling medium thermo-cracking steam is sprayed, and the bio-oil that obtains deposits at the bottom of the tower in the temporary storage tank; And in the bio-oil holding tank, collect; Subsequently, thermo-cracking steam gets into water-cooled condenser and ice-cold condensing surface, and the bio-oil of condensation flows into 2 biomass oil tanks respectively.
Referring to Fig. 2; The pyrolysis steam of coming from solid separator enters in the quenching column from pyrolysis steam-in 21, and at this moment, the spray medium sprays into from high pressure spray nozzle 22 under the effect of recycle pump 12; The partial thermal decomposition vapor condensation becomes bio-oil; Uncooled pyrolysis steam, bio-oil, spray medium flow into temporary storage tank 14 at the bottom of the tower together, part spray medium also at the bottom of the tower temporary storage tank 14 tops spray into, make further to be condensed into bio-oil from pyrolysis vapour outlet 26 effusive pyrolysis steam.
In the laboratory scale biomass through pyrolysis reactor drum of the 1kg/h that sets up; Use the pine tree wood chip as biomass material, 500 ℃ of temperature of reaction, under the reaction conditions of the residence time of material of 0.83s; Only adopt the mode of three grades of water-cooled condenser biomass collection oil; The bio-oil productive rate is merely 45%, and adopts quenching column, water-cooled and the ice-cold oily mode of multi-stage condensing device biomass collection, and the bio-oil productive rate reaches 64.5%.
Claims (8)
1. biomass fast pyrolysis device is characterized in that being provided with and adds temporary storage tank at the bottom of feed bin, autofeed device, mass rate appearance, gas preheater, pyrolysis reactor, separator, charcoal scoop, water cooler, recycle pump, quenching column, the tower, the 1st bio-oil holding tank, water-cooled condenser, the 2nd bio-oil holding tank, water ice condenser, the 3rd bio-oil holding tank; The said discharge port that adds feed bin connects the biomass material import of pyrolysis reactor through the autofeed device; The import of mass rate appearance connects nitrogen inlet; The outlet of mass rate appearance connects the combi inlet port of pyrolysis reactor through gas preheater; The thermo-cracking steam charcoal of pyrolysis reactor and ash outlet connect the import of separator, and the charcoal of separator and ash outlet connect the import of charcoal scoop, and the thermo-cracking vapor outlet port of separator connects the import of quenching column; The outlet of the bio-oil of quenching column connects the import of temporary storage tank at the bottom of the tower; A way outlet of temporary storage tank connects the import of the 1st bio-oil holding tank at the bottom of the tower, and another way outlet of temporary storage tank connects quenching column through recycle pump and water cooler successively at the bottom of the tower, and quenching column is connected with water ice condenser with the 2nd bio-oil holding tank respectively through water-cooled condenser; The outlet of water ice condenser connects the 3rd bio-oil holding tank, the inlet that can not coagulating property pneumatic outlet connects the mass rate appearance of water ice condenser.
2. biomass fast pyrolysis device as claimed in claim 1 is characterized in that said separator establishes the 1st grade of separator and the 2nd grade of separator; Said receipts thing charcoal scoop is established the 1st grade of charcoal scoop and the 2nd grade of charcoal scoop, and the 1st grade of charcoal scoop is located at the 1st grade of separator lower end, and the 2nd grade of charcoal scoop established the 2nd grade of separator lower end.
3. biomass fast pyrolysis device as claimed in claim 1 is characterized in that said pyrolysis reactor adopts biomass bubbling fluidization bed bioreactor.
4. the method for biomass fast pyrolysis is characterized in that adopting biomass fast pyrolysis device according to claim 1, said method comprising the steps of:
1) sends into the step in the pyrolysis reactor to biomass material through feeder;
2) in pyrolysis reactor, biomass material carried out thermo-cracking and in separator, thermo-cracking steam and charcoal and ash carried out the step of gas solid separation;
3) in quenching column, thermo-cracking steam is sprayed the step that obtains the one-level bio oil;
4) in water-cooled condenser, the thermo-cracking vapor condensation obtained two stage biological oil and in ice-cold condensing surface, the further condensation of thermo-cracking steam obtained the step of three grades of bio oil.
5. the method for biomass fast pyrolysis as claimed in claim 4; It is characterized in that in step 1); The said step of sending into biomass material in the pyrolysis reactor through feeder is following: the not condensable gases that biomass through pyrolysis produces is as carrier gas; Through being preheated to 500～600 ℃, flow into through gas distributor from the pyrolysis reactor bottom, make thermal barrier and biomass material be in fluidization; Pyrolysis reactor is preheated to 400～600 ℃ in advance, and biomass material gets into pyrolysis reactor under the effect of autofeed device, and the temperature rise rate with 500～1000 ℃/s heats in reactor drum.
6. the method for biomass fast pyrolysis as claimed in claim 4; It is characterized in that in step 2) in; Said in pyrolysis reactor, biomass material to be carried out the step of thermo-cracking following: biomass material carries out thermo-cracking in pyrolysis reactor after; Thermo-cracking steam, charcoal and ash leave pyrolysis reactor and get into the two-stage solid separator, in the collection canister of separator lower end, collect charcoal and ash.
7. the method for biomass fast pyrolysis as claimed in claim 4; It is characterized in that in step 3); Said in quenching column, thermo-cracking steam to be sprayed the step that obtains the one-level bio oil following: the thermo-cracking steam that does not contain charcoal and ash gets into quenching column, uses to spray medium thermo-cracking steam is sprayed.
8. the method for biomass fast pyrolysis as claimed in claim 4; It is characterized in that in step 4); Said step in water-cooled condenser that thermo-cracking vapor condensation acquisition two stage biological is oily is following: after thermo-cracking steam leaves quenching column; Get into water cooling heat exchanger, after cooling, obtain second stage bio-oil; Behind the thermo-cracking steam leaving water cold heat exchanger, flow into ice-cold interchanger, further condensation obtains third stage bio-oil.
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|---|---|---|---|---|
| CN103131453A (en) * | 2013-03-11 | 2013-06-05 | 北京神雾环境能源科技集团股份有限公司 | Pyrolytic evaluation device for carbon-containing substances |
| CN103691429A (en) * | 2014-01-03 | 2014-04-02 | 北京林业大学 | Catalyst for rapid pyrolysis and liquefaction of biomass as well as preparation method and application thereof |
| CN104031671A (en) * | 2014-06-30 | 2014-09-10 | 厦门大学 | Method for preparing bio-oil through biomass pyrolysis |
| CN104662132A (en) * | 2012-08-07 | 2015-05-27 | 科伊奥股份有限公司 | Improved biomass feed system including gas assist |
| CN106244177A (en) * | 2016-07-27 | 2016-12-21 | 大港油田集团有限责任公司 | A kind of straw Continuous Heat cracking technology and cracking apparatus thereof |
| CN106635114A (en) * | 2016-12-06 | 2017-05-10 | 青岛理工大学 | Device and method for realizing catalytic cracking oil and gas cogeneration in fluidization state by waste rubber powder |
| CN108018054A (en) * | 2016-10-28 | 2018-05-11 | 杨晓林 | A kind of organic waste cracking system and treatment process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10273676A (en) * | 1997-03-31 | 1998-10-13 | Hitachi Zosen Corp | Apparatus for obtaining oil from waste plastic |
| CN1390915A (en) * | 2002-06-07 | 2003-01-15 | 浙江大学 | Biomass integrated thermocracking equipment for preparing liquid fuel |
| CN101531910A (en) * | 2008-03-11 | 2009-09-16 | 广州迪森热能技术股份有限公司 | System for rapidly pyrolysing and liquefying biomass |
| CN101602953A (en) * | 2009-07-22 | 2009-12-16 | 丁赤民 | The purification system of straw quick thermal cracking products |
| CN101602954A (en) * | 2009-07-22 | 2009-12-16 | 丁赤民 | The method of manufacturing fuel through straw quick thermal cracking and fuel product thereof |
-
2011
- 2011-10-12 CN CN201110308862.7A patent/CN102408901B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10273676A (en) * | 1997-03-31 | 1998-10-13 | Hitachi Zosen Corp | Apparatus for obtaining oil from waste plastic |
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