CN202610180U - Device for extracting biological oil from biomass - Google Patents
Device for extracting biological oil from biomass Download PDFInfo
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- CN202610180U CN202610180U CN2012202449524U CN201220244952U CN202610180U CN 202610180 U CN202610180 U CN 202610180U CN 2012202449524 U CN2012202449524 U CN 2012202449524U CN 201220244952 U CN201220244952 U CN 201220244952U CN 202610180 U CN202610180 U CN 202610180U
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- 239000002028 Biomass Substances 0.000 title claims abstract description 84
- 238000000197 pyrolysis Methods 0.000 claims abstract description 115
- 238000002309 gasification Methods 0.000 claims abstract description 78
- 239000007789 gas Substances 0.000 claims description 91
- 239000000463 material Substances 0.000 claims description 61
- 238000002485 combustion reaction Methods 0.000 claims description 50
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 42
- 239000012075 bio-oil Substances 0.000 claims description 42
- 239000003546 flue gas Substances 0.000 claims description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 36
- 239000000428 dust Substances 0.000 claims description 30
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- 239000002737 fuel gas Substances 0.000 claims description 10
- 239000002826 coolant Substances 0.000 claims description 9
- 230000005587 bubbling Effects 0.000 claims description 8
- 239000002893 slag Substances 0.000 claims description 6
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims 2
- 238000000034 method Methods 0.000 abstract description 22
- 238000006243 chemical reaction Methods 0.000 abstract description 14
- 238000003860 storage Methods 0.000 abstract description 3
- 238000006392 deoxygenation reaction Methods 0.000 abstract description 2
- 238000010791 quenching Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 20
- 239000001257 hydrogen Substances 0.000 description 16
- 229910052739 hydrogen Inorganic materials 0.000 description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 13
- 239000003054 catalyst Substances 0.000 description 10
- 239000000571 coke Substances 0.000 description 8
- 239000000446 fuel Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 239000003921 oil Substances 0.000 description 5
- 238000007233 catalytic pyrolysis Methods 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000010729 system oil Substances 0.000 description 4
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000000969 carrier Substances 0.000 description 2
- 229910052681 coesite Inorganic materials 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- 229910052906 cristobalite Inorganic materials 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 238000012432 intermediate storage Methods 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229910052682 stishovite Inorganic materials 0.000 description 2
- 239000010902 straw Substances 0.000 description 2
- 229910052905 tridymite Inorganic materials 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical group O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 1
- 239000002154 agricultural waste Substances 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Processing Of Solid Wastes (AREA)
Abstract
The utility model discloses a device for extracting biological oil from biomass. The device comprises a pyrolysis reactor (1), a gasification reactor (2), a burning reactor (3) and a quench cooler (4). A method comprises the following steps that step 1, crushed and naturally-dried biomass enters a biomass dryer (6) firstly, and the moisture content of the biomass is dried by under 3 percent; step 2, the dried biomass passes through a storage bin (12) as a middle storage tank, a downcomer (13) and a feeder (14) to be sent to the pyrolysis reactor (1), the biomass is quickly pyrolyzed at the reaction temperature of 400-600 DEG C and under the reducing atmosphere, and the biomass is transformed and generated into pyrolysis gas and pyrolysis semicoke; and step 3, the pyrolysis semicoke from the semicoke outlet (1D) of the pyrolysis reactor (1) enters the gasification reactor (2) through a feed delivery pipe (9). The device effectively carries out deoxygenation in the pyrolysis process, the quality of biological oil is increased, and the energy efficiency of a system is high.
Description
Technical Field
The utility model discloses a device for preparing bio-oil from biomass, which relates to the field of biomass resource utilization.
Background
With the rapid development of human society and the increasing world energy demand, the fossil energy which people rely on for a long time is exhausted day by day, and the large-scale utilization of the fossil energy causes serious environmental pollution. Biomass (including agricultural straw, forestry waste, various organic wastes, and the like) is a renewable clean energy source and is the only renewable resource which can be converted into liquid fuel. The liquid fuel prepared by the biomass not only can reduce the dependence on petroleum, but also can greatly reduce the air pollution and the emission of greenhouse gases.
The biomass pyrolysis liquefaction is one of the main technologies for preparing liquid fuel bio-oil, and means that biomass is directly pyrolyzed to generate a gas product and solid coke under the conditions of 400-; the pyrolysis gas is rapidly cooled, a liquid product obtained by condensation is biological oil, and the uncondensed non-condensable gas and solid coke can provide a heat source for biomass pyrolysis or output as a byproduct. In order to improve the yield and quality of the bio-oil and meet the requirement of industrialization, various pyrolysis reactors including a fluidized bed reactor, a rotating cone reactor, a vacuum moving bed reactor, a microwave heating reactor and the like are developed in various countries around the world. By utilizing the existing pyrolysis liquefaction technology, the yield of the bio-oil can be between 40 and 80 percent, but because the biomass raw material has high oxygen content and large water content, the oxygen content in the bio-oil is high (35 to 40 weight percent), and the water content is large (15 to 30 weight percent), the bio-oil has strong acidity, unstable physicochemical property and low quality. In order to improve the quality of pyrolysis products, the current technical route concerned by researchers mainly comprises two aspects of catalytic pyrolysis and catalytic hydrogenation, wherein the researchers propose a method for preparing low-oxygen-content liquid fuel by adding a catalyst in the pyrolysis process, wherein the catalyst is generally a molecular sieve catalyst, an alkaline earth metal oxide and the like [ Shorui, Zhang stone, a method for preparing the low-oxygen-content liquid fuel by biomass online catalytic pyrolysis, 2011100003772.7 ], but the biggest problem faced by the catalytic pyrolysis is that the catalyst is easy to coke and deactivate, so that the service life of the catalyst is short, and the deoxidation rate is limited. The catalytic hydrogenation is to add hydrogen and a catalyst into the bio-oil under high pressure to realize bio-oil deoxygenation so as to obtain high-quality bio-oil, but the main obstacles at present are that a large amount of hydrogen sources are required to be consumed, the reaction pressure is high, generally more than 10MPa, the energy consumption is high, the economical efficiency is poor, and a noble metal catalyst is not suitable to be added in the biomass pyrolysis process. Recently, researchers have proposed that catalytic pyrolysis and catalytic hydrogenation are carried out under the condition of combining a noble metal Pt catalyst and a mesoporous molecular sieve catalyst to improve the quality of oil, but the problems of high cost and easy deactivation of the catalyst are faced. Therefore, the development of an efficient and economic biomass pyrolysis oil preparation process is of great significance.
Disclosure of Invention
The technical problem is as follows:according to the limitation of prior art, the utility model aims at providing a device for bio-oil is prepared to living beings to solve the problem that the bio-oil oxygen content height, moisture are big, system energy resource consumption is high that liquid fuel is prepared in current living beings pyrolysis, provide a bio-oil device and method of preparing low oxygen content, low moisture content through the hierarchical thermal conversion of living beings.
The technical scheme is as follows:in order to solve the technical problem, the utility model provides a device for preparing bio-oil from biomass, which comprises a pyrolysis reactor, a gasification reactor, a combustion reactor, a quencher, a feed water heater and a biomass dryer, a first cyclone dust collector, a second cyclone dust collector, a feed conveying pipe, a return pipe, a stock bin, a downcomer, a feeder and a connecting pipeline; wherein,
the pyrolysis reactor comprises a biomass feed inlet, a gas inlet, a pyrolysis gas outlet and a semicoke outlet; the gasification reactor comprises a semicoke inlet, a water vapor inlet, a gas product outlet, a circulating bed material outlet and a slag discharge port; the combustion reactor comprises a fuel gas inlet, an air/oxygen inlet, a circulating bed material inlet and a flue gas/circulating bed material outlet; the quencher comprises a pyrolysis gas inlet, a cooling medium inlet, a condensed bio-oil outlet and a non-condensable gas outlet; the feed water heater is a dividing wall type heat exchanger and comprises a high-temperature flue gas inlet, a flue gas outlet, a feed water inlet and a steam outlet; the biomass dryer is a contact heat exchanger and comprises a flue gas inlet, a flue gas outlet, a biomass inlet and a dried biomass outlet; wherein,
a semi-coke outlet of the pyrolysis reactor is connected with a semi-coke inlet of the gasification reactor through a conveying pipe, a pyrolysis gas outlet of the pyrolysis reactor is connected with a gas inlet of the first cyclone dust collector, and the dedusted pyrolysis gas is introduced into a pyrolysis gas inlet of the quencher; a gas product outlet of the gasification reactor is connected with a gas inlet of the pyrolysis reactor;
the material return pipe connects the circulating bed material outlet of the gasification reactor with the circulating bed material inlet of the combustion reactor; the outlet of the flue gas/circulating bed material is connected with the inlet of a second cyclone dust collector, and the dipleg of the second cyclone dust collector directly extends into the combustion reactor; a non-condensable gas outlet of the quencher is connected with a fuel gas inlet of the combustion reactor;
the gas outlet of the second cyclone dust collector is connected with the high-temperature flue gas inlet of the water supply heater, and the flue gas outlet of the water supply heater is connected with the flue gas inlet of the biomass dryer; the water vapor outlet of the feed water heater is directly connected with the water vapor inlet of the gasification reactor; the biomass dryer outlet is connected with the bin, the bin outlet is connected with the feeder inlet through a descending pipe, and the feeder outlet is directly connected with the pyrolysis reactor inlet.
Preferably, the pyrolysis reactor is a spouted fluidized bed or a bubbling fluidized bed, and the gas inlet and the biomass feed inlet of the pyrolysis reactor are respectively positioned at the lower part of the pyrolysis reactor;
the gasification reactor is a spouted fluidized bed or a bubbling fluidized bed, and a steam inlet of the gasification reactor is positioned at the bottom of the gasification reactor;
the combustion reactor is a circulating fluidized bed, and a gas inlet and an air/oxygen inlet of the combustion reactor are respectively positioned at the lower part of the combustion reactor
The semicoke outlet of the pyrolysis reactor, the semicoke inlet of the gasification reactor, the circulating bed material outlet of the gasification reactor and the circulating bed material inlet of the combustion reactor are all positioned at the lower parts of the respective reactors, the semicoke outlet is higher than the semicoke inlet, and the circulating bed material outlet is higher than the circulating bed material inlet.
Has the advantages that:the utility model discloses a method realizes hierarchical thermal conversion utilization to the biomass, living beings fast pyrolysis obtains the bio-oil, noncondensable gas and semicoke, wherein the noncondensable gas that the pyrolysis generated provides the heat for biomass pyrolysis process and semicoke gasification process through the burning, utilize semicoke and vapor to carry out gasification reaction and provide hydrogen-rich gas for the pyrolysis process, and the gasification process of semicoke and noncondensable gaseous combustion process separately, under the condition of guaranteeing self-heating gasification, avoid inert gas and oxygen to sneak into in the gasification product gas, thereby provide high concentration's hydrogen for the pyrolytic reaction ware.
The utility model discloses a required hydrogen that adds in the process of technology living beings pyrolysis directly comes from the inside of living beings pyrolysis system oil system, has avoided the reliance of external hydrogen supply, has both reduced the economic cost and the energy consumption of living beings system oil, has reduced the oxygen content in the bio-oil again, improves the quality of bio-oil.
The utility model discloses a process is through the setting of each stage reactor, and the energy of make full use of living beings, including the burning of non-condensable gas, high temperature flue gas heating feedwater and dry living beings, improved the energy efficiency of living beings conversion bio-oil system, carry out dry preliminary treatment before the living beings pyrolysis moreover and be favorable to reducing bio-oil moisture content, improve the quality of bio-oil.
Drawings
Fig. 1 is a schematic view of the process and system apparatus of the present invention.
Detailed Description
The present invention will be further explained with reference to the accompanying drawings.
The following describes in detail an apparatus for producing bio-oil from biomass according to the present invention with reference to fig. 1 and specific examples.
The utility model discloses a device that bio-oil was prepared to living beings passes through the hierarchical thermal conversion of living beings, obtains bio-oil with quick pyrolysis of living beings under the hydrogen-rich reducing atmosphere of pyrolysis reactor, non-condensable gas and semicoke, wherein the non-condensable gas that the pyrolysis generated provides the heat for biomass pyrolysis process and semicoke gasification process through the burning, utilizes semicoke and vapor to carry out gasification reaction and provides hydrogen-rich gas for the pyrolysis process, and the high temperature flue gas of combustion reactor is used for heating feedwater and dry living beings, makes the device realize living beings pyrolysis system oil under self-heating source and self-hydrogen supply source, the utility model discloses not only effectively deoxidization at the pyrolysis process improves the bio-oil quality, and the energy efficiency of system is high moreover.
The utility model provides a device for preparing bio-oil from biomass, which comprises a pyrolysis reactor 1, a gasification reactor 2, a combustion reactor 3, a quencher 4, a feed water heater 5, a biomass dryer 6, a first cyclone dust collector 7, a second cyclone dust collector 8, a material conveying pipe 9, a material returning pipe 11, a stock bin 12, a descending pipe 13, a feeder 14 and a connecting pipeline; wherein,
the pyrolysis reactor 1 comprises a biomass feeding hole 1A, a gas inlet 1B, a pyrolysis gas outlet 1C and a semicoke outlet 1D; the gasification reactor 2 comprises a semicoke inlet 2A, a water vapor inlet 2B, a gas product outlet 2C, a circulating bed material outlet 2D and a slag discharge port 2E; the combustion reactor 3 comprises a fuel gas inlet 3A, an air/oxygen inlet 3B, a circulating bed material inlet 3C and a flue gas/circulating bed material outlet 3D; the quencher 4 comprises a pyrolysis gas inlet 4A, a cooling medium inlet 4D, a condensed bio-oil outlet 4B and a non-condensable gas outlet 4C; the feed water heater 5 is a dividing wall type heat exchanger and comprises a high-temperature flue gas inlet 5A, a flue gas outlet 5C, a feed water inlet 5B and a steam outlet 5D; the biomass dryer 6 is a contact heat exchanger and comprises a flue gas inlet 6A, a flue gas outlet 6C, a biomass inlet 6B and a dried biomass outlet 6D; wherein,
a semicoke outlet 1D of the pyrolysis reactor 1 is connected with a semicoke inlet 2A of the gasification reactor 2 through a material conveying pipe 9, a pyrolysis gas outlet 1C of the pyrolysis reactor 1 is connected with an air inlet of a first cyclone dust collector 7, and the dedusted pyrolysis gas is introduced into a pyrolysis gas inlet 4A of a quencher 4; a gas product outlet 2C of the gasification reactor 2 is connected with a gas inlet 1B of the pyrolysis reactor 1;
the material return pipe 11 connects a circulating bed material outlet 2D of the gasification reactor 2 with a circulating bed material inlet 3C of the combustion reactor 3; the flue gas/circulating bed material outlet 3D is connected with the inlet of the second cyclone dust collector 8, and a dipleg 10 of the second cyclone dust collector 8 directly extends into the combustion reactor 3; a non-condensable gas outlet 4C of the quencher 4 is connected with a fuel gas inlet 3A of the combustion reactor 3;
a gas outlet 8B of the second cyclone dust collector 8 is connected with a high-temperature flue gas inlet 5A of the feed water heater 5, and a flue gas outlet 5C of the feed water heater 5 is connected with a flue gas inlet 6A of the biomass dryer 6; a steam outlet 5D of the feed water heater 5 is directly connected with a steam inlet 2B of the gasification reactor 2; the outlet 6D of the biomass dryer 6 is connected with the bin 12, the outlet 12B of the bin is connected with the inlet of the feeder 14 through the downcomer 13, and the outlet of the feeder 14 is directly connected with the inlet 1A of the pyrolysis reactor 1.
The pyrolysis reactor 1 is a spouted fluidized bed or a bubbling fluidized bed, and a gas inlet 1B and a biomass feed inlet 1A of the pyrolysis reactor 1 are respectively positioned at the lower part of the pyrolysis reactor 1;
the gasification reactor 2 is a spouted fluidized bed or a bubbling fluidized bed, and a water vapor inlet 2B of the gasification reactor 2 is positioned at the bottom of the gasification reactor 2;
the combustion reactor 3 is a circulating fluidized bed, and a fuel gas inlet 3A and an air/oxygen inlet 3B of the combustion reactor 3 are respectively positioned at the lower part of the combustion reactor 3.
A semicoke outlet 1D of the pyrolysis reactor 1, a semicoke inlet 2A and a circulating bed material outlet 2D of the gasification reactor 2 and a circulating bed material inlet 3C of the combustion reactor 3 are all positioned at the lower parts of the respective reactors, the semicoke outlet 1D is higher than the semicoke inlet 2A, and the circulating bed material outlet 2D is higher than the circulating bed material inlet 3C.
The method for preparing the bio-oil by the biomass comprises the following steps:
step 1: the biomass after being crushed and naturally dried firstly enters a biomass dryer 6, and the water content of the biomass is dried to be below 3 percent;
step 2: the dried biomass is fed into a pyrolysis reactor 1 through a bin 12 serving as an intermediate storage tank and a downcomer 13 from a feeder 14, fast pyrolysis is carried out at the reaction temperature of 400-600 ℃ in a reducing atmosphere, and the biomass is converted to generate pyrolysis gas and pyrolysis semicoke;
and step 3: the pyrolysis semicoke from a semicoke outlet 1D of a pyrolysis reactor 1 enters a gasification reactor 2 through a material conveying pipe 9 to be subjected to gasification reaction with gasification medium steam at the temperature of 750-900 ℃, and the gasification product is H2CO and CO2(ii) a The gasification products are fed into a pyrolysis reactor 1, so that biomass pyrolysis is carried out in a hydrogen-rich reducing atmosphere, and heat required by pyrolysis is provided at the same time;
and 4, step 4: pyrolysis gas at a pyrolysis gas outlet 1C of the pyrolysis reactor 1 is subjected to removal of fine semicoke particles carried with the gas flow by a first cyclone dust collector 7 and then enters a quencher 4 for cooling, the pyrolysis gas is separated into two parts of bio-oil and non-condensable gas after being cooled, wherein one part of the bio-oil is used as a product output device, and the other part of the bio-oil is sent into the quencher 4 from a cooling medium inlet 4D of the quencher 4 to be used as a cooling medium of the bio-oil;
and 5: the non-condensable gas at a non-condensable gas outlet 4C of the quencher 4 is fed into the combustion reactor 3 to be combusted with air/oxygen, circulating bed materials serving as heat carriers in the combustion reactor are heated, the operating temperature of the combustion reactor 3 is controlled to be 850-1000 ℃, the circulating bed materials are carried by combustion flue gas and are fed into the gasification reactor 2 through a dipleg 10 of the second cyclone dust collector 8, and heat is provided for semi-coke gasification; the high-temperature flue gas at the gas outlet 8B of the second cyclone dust collector 8 is firstly introduced into the feed water heater 5 and then is sent into the biomass dryer 6 and then is discharged out of the device.
The semicoke gasification product is hydrogen-rich gas, wherein the component H2 :50%～70%、CO 5%～15% and CO2 15-30 percent, and the gas inlet temperature of the pyrolysis reactor 1 is 700-850 ℃.
The downcomer 13 between the feeder 14 and the silo 12 is kept filled with biomass.
The temperature of the steam at the outlet of the feed water heater 5 is 450-600 ℃.
The cooling medium of the quencher 4 is circulating biological oil; the temperature of the bio-oil at the cooling medium inlet 4D of the quencher 4 is controlled to be below 25 ℃.
The operation temperature in the biomass dryer 6 is 80-200 ℃, and the smoke discharge temperature of the smoke outlet 6C is below 150 ℃.
The biomass is any one or any combination of naturally dried agricultural wastes, forestry wastes and the like, and the particle size of the crushed biomass is 0.5-5 mm.
The circulating bed material is an inert heat carrier and comprises ash and Al2O3、SiO2Any one of the above.
The utility model discloses a device includes: the biomass gasification device comprises a pyrolysis reactor 1, a gasification reactor 2, a combustion reactor 3, a quencher 4, a feed water heater 5, a biomass dryer 6, cyclone dust collectors 7 and 8, a feed delivery pipe 9, a return pipe 11, a storage bin 12, a downcomer 13, a feeder 14 and connecting pipelines. Wherein the pyrolysis reactor 1 comprises two inlets: biomass feed inlet 1A and gas inlet 1B, and two outlets: a pyrolysis gas outlet 1C and a semicoke outlet 1D; the gasification reactor 2 comprises a semicoke inlet 2A, a water vapor inlet 2B, a gasification product outlet 2C, a circulating bed material outlet 2D and a slag discharge port 2E; the combustion reactor 3 comprises 3 inlets and 1 outlet: a gas inlet 3A, an air/oxygen inlet 3B, a circulating bed material inlet 3C and a flue gas/circulating bed material outlet 3D; the quencher comprises a pyrolysis gas inlet 4A, a cooling medium inlet 4D, a condensed bio-oil outlet 4B and a non-condensable gas outlet 4C. Wherein the feed delivery pipe 9 connects a semicoke outlet 1D of the pyrolysis reactor 1 with a semicoke inlet 2A of the gasification reactor 2, and a gas product outlet 2C is connected with a gas inlet 1B of the pyrolysis reactor 1 through a pipeline; the material return pipe 11 connects a circulating bed material outlet 2D of the gasification reactor 2 with a circulating bed material inlet 3C of the combustion reactor 3; a flue gas/circulating bed material outlet 3D of the combustion reactor 3 is connected with a gas inlet 8A of a cyclone dust collector 8, and a dipleg 10 of the cyclone dust collector 8 directly extends into the combustion reactor 3; a pyrolysis gas outlet 1C of the pyrolysis reactor 1 is connected with an air inlet 7A of a cyclone dust collector 7, a gas outlet 7B is connected with an inlet 4A of a quencher 4, and a non-condensable gas outlet 4C of the quencher 4 is connected with a fuel gas inlet 3A of the combustion reactor 3; the feed water heater 5 is a dividing wall type heat exchanger and comprises a high-temperature flue gas inlet 5A, a medium-temperature flue gas outlet 5C, a feed water inlet 5B and a steam outlet 5D; the biomass dryer 6 is a contact heat exchanger and comprises a flue gas inlet 6A, a flue gas outlet 6C, a biomass inlet 6B and a dried biomass outlet 6D, wherein a gas outlet 8B of the cyclone dust collector 8 is connected with a high-temperature flue gas inlet 5A of the feed water heater 5, and a flue gas outlet 5C is connected with a flue gas inlet 6A of the biomass dryer 6; a steam outlet 5D of the feed water heater 5 is directly connected with a steam inlet 2B of the gasification reactor 2; a dried biomass outlet 6D of the biomass dryer 6 is connected with a bin 12 through a conveying pipeline, an outlet 12B of the bin 12 is connected with the upper end of a downcomer 13, the lower end of the downcomer 13 is connected with an inlet 14A of a feeder 14, and an outlet 14B of the feeder 14 is directly connected with a biomass inlet 1A of the pyrolysis reactor 1.
In addition, the pyrolysis reactor 1 is a spouted fluidized bed or a bubbling fluidized bed, the gas inlet 1B is positioned at the bottom below the air distribution plate of the reactor, and the biomass feed inlet 1A is positioned above the air distribution plate at the lower part of the reactor; the gasification reactor 2 is a spouted fluidized bed or a bubbling fluidized bed, and the water vapor inlet 2B is positioned at the bottom below an air distribution plate of the gasification reactor 2; the combustion reactor 3 is a circulating fluidized bed, and a fuel gas inlet 3A and an air/oxygen inlet 3B are positioned at the lower part of the reactor; the semicoke outlet 1D of the pyrolysis reactor 1, the semicoke inlet 2A and the circulating bed material outlet 2D of the gasification reactor 2 and the circulating bed material inlet 3C of the combustion reactor 3 are all positioned at the lower part of the respective reactors, and the outlet 1D is higher than the inlet 2A, and the outlet 2D is higher than the inlet 3C.
In the device, the process of preparing oil by pyrolyzing biomass comprises the following steps: naturally drying and crushing the biomass to be 0.5-2mm such as biomass straws, forestry wood chips and the like, firstly entering a biomass dryer 6, and drying at 80-200 ℃ by using the waste heat of system flue gas to obtain the dried biomass with the water content of less than 3%. Then the dried living beings get into feed bin 12 as the intermediate storage tank, send into pyrolytic reaction ware 1 through dispenser 14 through unloading pipe 13, and the raw materials in feed bin 12 and the unloading pipe 13 play the gaseous effect of keeping apart biomass dryer 6 and pyrolytic reaction ware 1, avoids gaseous mixing, in addition through the rotational speed of adjusting dispenser 14, the handling capacity of adjustable device living beings pyrolysis system oil.
The pyrolysis reactor 1 is simultaneously supplied with gasification product gas H from the gasification reactor 22CO and CO2And the biomass is rapidly pyrolyzed in the range of 400-550 ℃ in the hydrogen-rich reducing atmosphere and is converted into pyrolysis gas and semicoke.
Pyrolysis gas enters a cyclone dust collector 7 through an outlet 1C at the upper part of a pyrolysis reactor 1, fine semicoke particles carried by the pyrolysis gas are removed and then enter a quencher 4, a fine semicoke particle discharging device at a dust outlet 7C of the cyclone dust collector 7 is fed into a gasification reactor 2, the pyrolysis gas is separated into condensable product bio-oil and non-condensable gas in the quencher 4, the bio-oil is output from an outlet 4B at the lower part of the quencher 4, one part of the bio-oil is used as a product output device, and the other part of the bio-oil is used as a cooling medium of the bio-oil and is fed into the quencher 4 from an inlet 4D of the quencher 4; the non-condensable gas is output through an outlet 4C at the upper part of the quencher 4 and is sent into the combustion reactor 3 through a gas pipeline.
In addition, the pyrolysis semicoke at the outlet of the pyrolysis reactor 1 enters the gasification reactor 2 through the material conveying pipe 9 to be subjected to gasification reaction with gasification medium steam at 800-900 ℃, and the gasification product is a hydrogen-rich gas containing H250-70 percent of CO, 5-15 percent of CO and CO2 15% -30%; the gasification product gas with the temperature of 750-850 ℃ is sent into a pyrolysis reactor 1, so that the biomass pyrolysis is carried out in a hydrogen-rich reducing atmosphere, the heat required by the pyrolysis is provided, and the heat required by the semi-coke gasification is generated from the gasCirculating bed materials between the gasification reactor 2 and the combustion reactor 3 are provided, namely the gasification reactor 2 is directly connected with the combustion reactor 3, non-condensable gas from a quencher 4 is combusted with air/oxygen in the combustion reactor 3, the operating temperature of the combustion reactor 3 is controlled to be 850-1000 ℃, the circulating bed materials in the combustion reactor are heated, high-temperature circulating bed materials are carried by combustion flue gas and are sent into the gasification reactor 2 through a dipleg 10 of a cyclone dust collector 8, the circulating bed materials serve as heat carriers to provide heat for semicoke gasification and circulate between the combustion reactor 3 and the gasification reactor 2, and the circulating bed materials are ash residues and Al2O3Or SiO2And the inert materials are used for realizing self-heating of the gasification of the biomass semi-coke, and the combustion process is separated from the gasification process, so that inert gas and oxygen are prevented from being mixed into gasification product gas, and hydrogen-rich gas with hydrogen content of over 50 percent is provided for the pyrolysis reactor. The lower part of the gasification reactor 2 is provided with a slag discharge port 2E, partial ash and bed materials can be discharged from the slag discharge port 2E after the device is operated for a period of time, the height of the bed layer in the reactor is kept stable, and the discharged ash and bed materials can be mixed with gasification product gas at the outlet of the gasification reactor 2 and then are sent into the pyrolysis reactor 1.
The above description is only a preferred embodiment of the present invention, and the protection scope of the present invention is not limited to the above embodiment, but all equivalent modifications or changes made by those skilled in the art according to the present invention should be included in the protection scope of the claims.
Claims (2)
1. A device for preparing bio-oil from biomass is characterized in that: the device comprises a pyrolysis reactor (1), a gasification reactor (2), a combustion reactor (3), a quencher (4), a feed water heater (5), a biomass dryer (6), a first cyclone dust collector (7), a second cyclone dust collector (8), a material conveying pipe (9), a material returning pipe (11), a material bin (12), a descending pipe (13), a feeder (14) and a connecting pipeline; wherein,
the pyrolysis reactor (1) comprises a biomass feed inlet (1A), a gas inlet (1B), a pyrolysis gas outlet (1C) and a semicoke outlet (1D); the gasification reactor (2) comprises a semicoke inlet (2A), a steam inlet (2B), a gas product outlet (2C), a circulating bed material outlet (2D) and a slag discharge port (2E); the combustion reactor (3) comprises a fuel gas inlet (3A), an air/oxygen inlet (3B), a circulating bed material inlet (3C) and a flue gas/circulating bed material outlet (3D); the quencher (4) comprises a pyrolysis gas inlet (4A), a cooling medium inlet (4D), a condensed bio-oil outlet (4B) and a non-condensable gas outlet (4C); the feed water heater (5) is a dividing wall type heat exchanger and comprises a high-temperature flue gas inlet (5A), a flue gas outlet (5C), a feed water inlet (5B) and a steam outlet (5D); the biomass dryer (6) is a contact heat exchanger and comprises a flue gas inlet (6A), a flue gas outlet (6C), a biomass inlet (6B) and a dried biomass outlet (6D); wherein,
a semicoke outlet (1D) of the pyrolysis reactor (1) is connected with a semicoke inlet (2A) of the gasification reactor (2) through a conveying pipe (9), a pyrolysis gas outlet (1C) of the pyrolysis reactor (1) is connected with a gas inlet of a first cyclone dust collector (7), and the dedusted pyrolysis gas is introduced into a pyrolysis gas inlet (4A) of a quencher (4); a gas product outlet (2C) of the gasification reactor (2) is connected with a gas inlet (1B) of the pyrolysis reactor (1);
a material return pipe (11) connects a circulating bed material outlet (2D) of the gasification reactor (2) with a circulating bed material inlet (3C) of the combustion reactor (3); a flue gas/circulating bed material outlet (3D) is connected with an inlet of a second cyclone dust collector (8), and a dipleg (10) of the second cyclone dust collector (8) directly extends into the combustion reactor (3); a non-condensable gas outlet (4C) of the quencher (4) is connected with a fuel gas inlet (3A) of the combustion reactor (3);
a gas outlet (8B) of the second cyclone dust collector (8) is connected with a high-temperature flue gas inlet (5A) of the water supply heater (5), and a flue gas outlet (5C) of the water supply heater (5) is connected with a flue gas inlet (6A) of the biomass dryer (6); a steam outlet (5D) of the feed water heater (5) is directly connected with a steam inlet (2B) of the gasification reactor (2); an outlet (6D) of the biomass dryer (6) is connected with a bin (12), an outlet (12B) of the bin is connected with an inlet of a feeder (14) through a descending pipe (13), and an outlet of the feeder (14) is directly connected with an inlet (1A) of the pyrolysis reactor (1).
2. The device for preparing bio-oil from biomass according to claim 1, wherein: the pyrolysis reactor (1) is a spouted fluidized bed or a bubbling fluidized bed, and a gas inlet (1B) and a biomass feed inlet (1A) of the pyrolysis reactor (1) are respectively positioned at the lower part of the pyrolysis reactor (1);
the gasification reactor (2) is a spouted fluidized bed or a bubbling fluidized bed, and a steam inlet (2B) of the gasification reactor (2) is positioned at the bottom of the gasification reactor (2);
the combustion reactor (3) is a circulating fluidized bed, and a fuel gas inlet (3A) and an air/oxygen inlet (3B) of the combustion reactor (3) are respectively positioned at the lower part of the combustion reactor (3)
A semicoke outlet (1D) of the pyrolysis reactor (1), a semicoke inlet (2A) and a circulating bed material outlet (2D) of the gasification reactor (2) and a circulating bed material inlet (3C) of the combustion reactor (3) are positioned at the lower parts of the respective reactors, the semicoke outlet (1D) is higher than the semicoke inlet (2A), and the circulating bed material outlet (2D) is higher than the circulating bed material inlet (3C).
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102703098A (en) * | 2012-05-29 | 2012-10-03 | 东南大学 | Device and method for preparing biological oil from biomass |
| CN104212495A (en) * | 2014-04-02 | 2014-12-17 | 刘国海 | Integrated device and method for preparing oil product and synthetic gas from fine coal |
| CN105505477A (en) * | 2015-12-07 | 2016-04-20 | 浙江大学 | Multi-graded pyrolysis and gasification device of solid fuel and application method of multi-graded pyrolysis and gasification device |
| CN108070405A (en) * | 2017-12-20 | 2018-05-25 | 武汉凯迪工程技术研究总院有限公司 | Biomass multi-production method and its system based on low temperature fluidized bed in three |
| CN109963927A (en) * | 2016-10-12 | 2019-07-02 | Ws-热处理技术有限责任公司 | Method and apparatus for gasified bio-matter amount |
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2012
- 2012-05-29 CN CN2012202449524U patent/CN202610180U/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102703098A (en) * | 2012-05-29 | 2012-10-03 | 东南大学 | Device and method for preparing biological oil from biomass |
| CN102703098B (en) * | 2012-05-29 | 2013-12-11 | 东南大学 | Device and method for preparing biological oil from biomass |
| CN104212495A (en) * | 2014-04-02 | 2014-12-17 | 刘国海 | Integrated device and method for preparing oil product and synthetic gas from fine coal |
| CN105505477A (en) * | 2015-12-07 | 2016-04-20 | 浙江大学 | Multi-graded pyrolysis and gasification device of solid fuel and application method of multi-graded pyrolysis and gasification device |
| CN109963927A (en) * | 2016-10-12 | 2019-07-02 | Ws-热处理技术有限责任公司 | Method and apparatus for gasified bio-matter amount |
| CN109963927B (en) * | 2016-10-12 | 2021-10-29 | Ws-热处理技术有限责任公司 | Method and device for gasifying biomass |
| US11236278B2 (en) | 2016-10-12 | 2022-02-01 | WS-Wärmeprozeßtechnik GmbH | Process for gasifying biomass with tar adsorption |
| CN108070405A (en) * | 2017-12-20 | 2018-05-25 | 武汉凯迪工程技术研究总院有限公司 | Biomass multi-production method and its system based on low temperature fluidized bed in three |
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