CN103031139B - Device and method for preparing bio-oil through rapid biomass pyrolysis - Google Patents
Device and method for preparing bio-oil through rapid biomass pyrolysis Download PDFInfo
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Abstract
The invention belongs to the technical field of biomass energy utilization and in particular relates to a device and a method for preparing bio-oil through rapid biomass pyrolysis. The device comprises a hopper, a feeding system, a fluidized bed rapid pyrolysis reactor, a gas-solid separation system, a hot coke combustion heat exchange system, a cold sand heating system, a pyrolysis gas rapid condensation system and a non-condensable gas cycle system, wherein the hot coke combustion heat exchange system comprises a plurality of cyclone combustors/heat exchangers and is used for realizing coke combustion and totally transferring the heat released by combustion and sensible heat of hot coke and sand to high-temperature combustion flue gas; and in addition, the cold sand heating system comprises a plurality of cyclone combustors and totally transfers the sensible heat of the high-temperature flue gas to the sand, so that high-temperature sand is obtained and is returned to the fluidized bed rapid pyrolysis reactor, and the heat required by a pyrolysis reaction is provided; and therefore, the bio-oil is prepared through the self-heating rapid biomass pyrolysis.
Description
Technical field
The invention belongs to biomass energy utilization technologies field, be specifically related to a kind of apparatus and method of biomass fast pyrogenation preparing bio-oil.
Background technology
Rapidly pyrolysing and liquefying biomass is under oxygen free condition, make the quick decomposes of biomass, then the rapid condensation of pyrolysis gas is mainly obtained to product liquid bio oil (productive rate can reach 70-80%), obtain the process of a small amount of solid coke and two kinds of by products of combustible gas simultaneously.Obtaining the required reaction conditions of high yield bio oil generally comprises: the temperature of reaction of the heating rate being exceedingly fast, 500 ℃ of left and right, be no more than the gas residence time of 2 s and the rapid condensation of pyrolysis gas and collection etc.Bio oil, as a kind of novel product liquid, is expected part petroleum replacing and as liquid fuel, is applied to the heat power equipments such as Industrial Boiler, kiln and oil engine, also can be used as industrial chemicals for extraction or prepares various chemical.
For the required reaction conditions of rapidly pyrolysing and liquefying biomass, each R&D institution has researched and developed number of different types biomass fast pyrogenation core reaction device and corresponding utility appliance both at home and abroad, wherein with the most study of fluidized-bed reactor.Biomass fast pyrogenation is an endothermic process, and need provides heat continuously in reactor; In order to reduce the production cost of bio oil, generally adopt pyrolysis solid or gaseous product combustion heat supplying, thereby realize the rapidly pyrolysing and liquefying process of autothermal; Therefore how to realize the burning of by product and to heat supply in reactor, be a key problem of biomass fast pyrogenation preparing bio-oil device development.
Generally speaking, by pyrolysis byproducts, burn to pyrolysis reactor heat supply, mainly contain three kinds of feasible schemes: (1) by product burning post-heating pyrolysis reactor, the mode heat supply of conducting heat by Gu Bi; (2) by product burning post-heating carrier gas, brings heat into reactor by carrier gas; (3) by product burning post-heating thermal barrier (sand), brings heat into reactor by sand.Because sand has very large thermal capacitance, rely on sand to be easy to bring a large amount of heats into pyrolysis reactor, therefore (3) kind scheme is the most effective heat supply scheme; But how to realize this process, it is a technical barrier urgently to be resolved hurrily.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, a kind of apparatus and method of biomass fast pyrogenation preparing bio-oil are provided.
The technical scheme that the device of biomass fast pyrogenation preparing bio-oil of the present invention adopts is:
This device comprises hopper, feed system, fluid bed fast pyrolysis reactor, gas solid separation system, hot coke combustion heat-exchange system, cold sand heating system, pyrolysis gas rapid condensation system and the condensible gas recycle system not;
The outlet of hopper is connected with the entrance of feed system, and the outlet of feed system is connected with the side wall lower ends entrance of fluid bed fast pyrolysis reactor; Fluid bed fast pyrolysis reactor bottom entrance is connected with the outlet of the condensible gas recycle system not, and upper end outlet is connected with the import of gas solid separation system; The air outlet of gas solid separation system is connected with the import of pyrolysis gas rapid condensation system; The outlet of pyrolysis gas rapid condensation system is divided into two-way, and a road is directly collected as combustion gas and used, and another road is connected with the entrance of the condensible gas recycle system not;
Described hot coke combustion heat-exchange system comprises a plurality of cyclone firing interchanger; Described a plurality of cyclone firing interchanger are connected from top to bottom, and this system is topmost cyclone firing interchanger first module, is followed successively by cyclone firing interchanger second unit downwards ..., cyclone firing interchanger most end unit; The discharge gate of cyclone firing interchanger first module is connected with the import of cyclone firing interchanger second unit, and the air outlet of cyclone firing interchanger second unit is connected with the import of cyclone firing interchanger first module; The discharge gate of cyclone firing interchanger second unit is connected with the import of cyclone firing interchanger Unit the 3rd, the air outlet of cyclone firing interchanger Unit the 3rd is connected with the import of cyclone firing interchanger second unit, the like to cyclone firing interchanger most end unit; The import of cyclone firing interchanger first module is also connected with the discharge gate of gas solid separation system, and the air outlet of cyclone firing interchanger first module is connected with the import of whirlwind heat exchanger first module in cold sand heating system; The discharge gate of cyclone firing interchanger most end unit is connected with collection box, directly collects cold sand and ash, and the import of cyclone firing interchanger most end unit is also connected with gas blower, directly air-supplied;
Described cold sand heating system comprises a plurality of whirlwind heat exchangers; Described a plurality of whirlwind heat exchangers are connected from bottom to top, and this system bottom is whirlwind heat exchanger first module, is upwards followed successively by whirlwind heat exchanger second unit ..., whirlwind heat exchanger most end unit; The air outlet of whirlwind heat exchanger first module is connected with the import of whirlwind heat exchanger second unit, and the discharge port of whirlwind heat exchanger second unit is connected with the import of whirlwind heat exchanger first module; The air outlet of whirlwind heat exchanger second unit is connected with the import of whirlwind heat exchanger Unit the 3rd, and the discharge port of whirlwind heat exchanger Unit the 3rd is connected with the import of whirlwind heat exchanger second unit, the like to whirlwind heat exchanger most end unit; The discharge port of whirlwind heat exchanger first module is also connected with fluid bed fast pyrolysis sidewall of reactor lower ending opening; The import of whirlwind heat exchanger most end unit also with for sandbox is connected, and directly feeds cold sand, and the air outlet of whirlwind heat exchanger most end unit directly communicates with atmosphere, and cold flue gas is entered to atmosphere.
Described hot coke combustion heat-exchange system at least comprises two cyclone firing/interchanger.
Described cold sand heating system at least comprises two whirlwind heat exchangers.
Described feed system is two-stage screw feeder.
Described fluid bed fast pyrolysis reactor is fast fluidized bed reactor.
Described gas solid separation system is cyclonic separator.
Described pyrolysis gas rapid condensation system is spraying and falling liquid film composite condensation system.
The method of the biomass fast pyrogenation preparing bio-oil based on described device provided by the invention, comprises the following steps:
Biomass material is sent into fluid bed fast pyrolysis reactor, take from not condensible gas that can not the condensing air recycle system is fluidized carrier gas, since the hot sand of self cooling sand heating system be thermal barrier, biomass under the effect of hot sand and fluidized carrier gas, decomposes rapidly;
First high temperature pyrolysis product enters gas solid separation system and realizes gas solid separation;
The solid that gas solid separation obtains enters hot coke combustion heat-exchange system, in multistage cyclone combustion heat-exchange device, the solid that gas solid separation obtains flows from top to bottom, freezing air flows from bottom to top, the solid that gas solid separation obtains passes through after burning and heat exchange, become cold ash and sand and discharge from cyclone firing interchanger most end unit, freezing air is first preheating and afterfire forms high-temperature flue gas; High-temperature flue gas enters in cold sand heating system, in multistage cyclone interchanger, high-temperature flue gas flows and transfers heat to cold sand from bottom to top, cold sand flows absorption heat from top to bottom and heats up, become hot sand, from whirlwind heat exchanger most end unit, discharge laggardly to enter fluidized-bed fast pyrolysis reactor;
Gas solid separation obtains high-temperature gas product, enter pyrolysis gas fast pyrogenation condenser system, after the composite condensation of spraying and falling liquid film, obtain liquid bio oil, condensible gas is not divided into two-way from outlet is flowed out, wherein a road is used as combustion gas after collecting, another Lu Zejing not condensible gas recycle system sends into the bottom inlet of fluid bed fast pyrolysis reactor after circulating, as fluidized carrier gas, use.
Described biomass material is lignocellulose-like biomass.
Temperature of reaction in described fluid bed fast pyrolysis reactor is 450-550 ℃, and gas residence time is 0.1 ~ 5s.
Coke in described hot coke combustion heat-exchange system and the excess air ratio of air combustion are 1.0 ~ 1.3.
In described cold sand heating system, the temperature out of hot sand is 550 ~ 800 ℃.
Beneficial effect of the present invention is:
The device of biomass fast pyrogenation preparing bio-oil of the present invention, a plurality of cyclone firing/interchanger based in hot coke combustion heat-exchange system, realize the perfect combustion of coke, and the heat that burning is discharged and the sensible heat of hot coke and hot sand self, be all transferred in high-temperature flue gas; In addition, based on cold sand heating system, again by the complete sensible heat of high-temperature flue gas, be all transferred to sand, then by sand, heat brought in fluid bed fast pyrolysis reactor, realize the fast pyrogenation reaction of biomass material.Thus, utilize hot coke combustion heat-exchange and two systems of cold sand heating, can greatly realize effective utilization of energy, and by the control to sand, can guarantee the steady running of biomass rapid pyrolysis reactor.
Accompanying drawing explanation
Fig. 1 is the apparatus structure schematic diagram of biomass fast pyrogenation preparing bio-oil of the present invention;
Number in the figure:
1-hopper; 2-feed system; 3-fluid bed fast pyrolysis reactor; 4-gas solid separation system; The hot coke combustion heat-exchange of 5-system; The cold sand heating system of 6-; 7-pyrolysis gas rapid condensation system; 8-is the condensible gas recycle system not.
Embodiment
The invention provides a kind of apparatus and method of biomass fast pyrogenation preparing bio-oil, below in conjunction with embodiment, the present invention will be further described.
Apparatus structure in each embodiment is identical, as shown in Figure 1.
The outlet of hopper 1 is connected with the entrance of feed system 2, and the outlet of feed system 2 is connected with the side wall lower ends entrance of fluid bed fast pyrolysis reactor 3; Fluid bed fast pyrolysis reactor 3 bottom inlets are connected with the outlet of the condensible gas recycle system 8 not, and upper end outlet is connected with the import of gas solid separation system 4; The air outlet of gas solid separation system 4 is connected with the import of pyrolysis gas rapid condensation system 7; The outlet of pyrolysis gas rapid condensation system 7 is divided into two-way, and a road is directly collected as combustion gas and used, and another road is connected with the entrance of the condensible gas recycle system 8 not.
Described hot coke combustion heat-exchange system 5 comprises a plurality of cyclone firing interchanger; Described a plurality of cyclone firing interchanger are connected from top to bottom, and this system is topmost cyclone firing interchanger first module I, is followed successively by cyclone firing interchanger second unit II downwards, cyclone firing interchanger most end unit N, wherein, N is not less than 2 integer; The discharge gate of cyclone firing interchanger first module I is connected with the import of cyclone firing interchanger second unit II, and the air outlet of cyclone firing interchanger second unit II is connected with the import of cyclone firing interchanger first module I; The discharge gate of cyclone firing interchanger second unit II is connected with the import of cyclone firing interchanger the 3rd unit III, the air outlet of cyclone firing interchanger the 3rd unit III is connected with the import of cyclone firing interchanger second unit II, the like to cyclone firing interchanger most end unit N; The import of cyclone firing interchanger first module I is also connected with the discharge gate of gas solid separation system 4, and the air outlet of cyclone firing interchanger first module I is connected with the import of whirlwind heat exchanger first module i in cold sand heating system 6; The discharge gate of cyclone firing interchanger most end unit N is connected with collection box, directly collects cold sand and ash, and the import of cyclone firing interchanger most end unit N is also connected with gas blower, directly air-supplied.
Described cold sand heating system 6 comprises a plurality of whirlwind heat exchangers; Described a plurality of whirlwind heat exchangers are connected from bottom to top, and this system bottom is whirlwind heat exchanger first module i, is upwards followed successively by whirlwind heat exchanger second unit ii ..., whirlwind heat exchanger most end unit n, wherein, n is not less than 2 integer; The air outlet of whirlwind heat exchanger first module i is connected with the import of whirlwind heat exchanger second unit ii, and the discharge port of whirlwind heat exchanger second unit ii is connected with the import of whirlwind heat exchanger first module i; The air outlet of whirlwind heat exchanger second unit ii is connected with the import of whirlwind heat exchanger the 3rd unit iii, and the discharge port of whirlwind heat exchanger the 3rd unit iii is connected with the import of whirlwind heat exchanger second unit ii, the like to whirlwind heat exchanger most end unit n; The discharge port of whirlwind heat exchanger first module i is also connected with fluid bed fast pyrolysis reactor 3 side wall lower ends openings; The import of whirlwind heat exchanger most end unit n also with for sandbox is connected, and directly feeds cold sand, and the air outlet of whirlwind heat exchanger most end unit n directly communicates with atmosphere, and cold flue gas is entered to atmosphere.
Feed system 2 is two-stage screw feeder, and fluid bed fast pyrolysis reactor 3 is fast fluidized bed reactor, and gas solid separation system 4 is cyclonic separator, and pyrolysis gas rapid condensation system 7 is spraying and falling liquid film composite condensation system.
Percentage composition in following embodiment, is quality percentage composition if no special instructions, and s represents second.
Embodiment 1
Adopt said apparatus preparing bio-oil.The poplar raw material that is 3mm by natural air drying, median size (moisture content is 8%) via hopper and two-stage screw feeder to send into an internal diameter be 700mm, highly in the fluid bed fast pyrolysis reactor of 3m, inlet amount is 150kg/h; It is fluidized carrier gas that this fluidized-bed reactor be take the not condensible gas that fast pyrogenation generates, and flow is 150Nm
3/ h, the sand that the temperature of take is 600 ℃ is thermal barrier, flow is 500kg/h; Poplar pyrolysis reaction temperature is 500 ℃, and the gas residence time of pyrolysis gas is about 3s; Pyrolysis product is after gas solid separation, and gaseous product enters in spraying and falling liquid film composite condensation system, through condensation, obtains bio oil, obtains not condensable gases simultaneously, and both productive rates are respectively 60% and 20%; Condensable gases total amount is not 180Nm
3/ h, wherein 150Nm
3/ h recycles as carrier gas.
The hot sand that gas solid separation is obtained and coke are sent into the hot coke combustion heat-exchange system that contains 4 cyclone firing interchanger, under the operating mode that is 1.2 at excess air ratio, burn and heat exchange, finally discharge the sand of 70 ℃ and grey mixture, obtain high-temperature flue gas simultaneously; This high-temperature flue gas is sent into the cold sand heating system that contains 3 whirlwind heat exchangers, the sand that is 500kg/h by inlet amount is heated to 600 ℃ from room temperature, discharges the flue gas of 130 ℃ simultaneously.
Embodiment 2
The apparatus structure that this fact Example adopts is identical with embodiment 1, with this, installs preparation bio oil.The pine that natural air drying, median size be 3mm of take is raw material (moisture content is 9%), and inlet amount is 150kg/h, and fluidized carrier gas flow is 150Nm
3/ h, sand temperature is that 620 ℃, flow are 500kg/h; The pyrolysis temperature of pine in fluidized-bed is 510 ℃, and the gas residence time of pyrolysis gas is about 3s, and the productive rate of bio oil is 59%, and the productive rate of condensible gas is not 20%.Under the operating mode that hot sand and coke are 1.2 at excess air ratio, carry out combustion heat-exchange, finally discharge the sand of 75 ℃ and grey mixture; High-temperature flue gas is heated to 620 ℃ by the sand of 500kg/h from room temperature simultaneously, discharges the flue gas of 135 ℃ simultaneously.
Embodiment 3
Compare with the device that embodiment 1 adopts, in cold sand heating system, whirlwind heat exchanger number changes 4 into, and all the other structures are identical, with this, install preparation bio oil.The rice husk that natural air drying, median size be 3mm of take is raw material (moisture content is 7.5%), and inlet amount is 150kg/h, and fluidized carrier gas flow is 150Nm
3/ h, sand temperature is that 610 ℃, flow are 500kg/h; The pyrolysis temperature of rice husk in fluidized-bed is 505 ℃, and the gas residence time of pyrolysis gas is about 3s, and the productive rate of bio oil is 50%, and the productive rate of condensible gas is not 21%.Under the operating mode that hot sand and coke are 1.3 at excess air ratio, carry out combustion heat-exchange, finally discharge the sand of 70 ℃ and grey mixture; High-temperature flue gas is heated to 610 ℃ by the sand of 500kg/h from room temperature simultaneously, discharges the flue gas of 80 ℃ simultaneously.
Embodiment 4
Utilize the device preparing bio-oil described in embodiment 3.The cornstalk that natural air drying, median size be 3mm of take is raw material (moisture content is 10.5%), and inlet amount is 150kg/h, and fluidized carrier gas flow is 150Nm
3/ h, sand temperature is that 580 ℃, flow are 500kg/h; The pyrolysis temperature of cornstalk in fluidized-bed is 475 ℃, and the gas residence time of pyrolysis gas is about 3s, and the productive rate of bio oil is 55%, and the productive rate of condensible gas is not 22%.Under the operating mode that hot sand and coke are 1.3 at excess air ratio, carry out combustion heat-exchange, finally discharge the sand of 75 ℃ and grey mixture; High-temperature flue gas is heated to 580 ℃ by the sand of 500kg/h from room temperature simultaneously, discharges the flue gas of 75 ℃ simultaneously.
Claims (10)
1. the device of a biomass fast pyrogenation preparing bio-oil, comprise hopper (1), feed system (2), fluid bed fast pyrolysis reactor (3), gas solid separation system (4), hot coke combustion heat-exchange system (5), cold sand heating system (6), pyrolysis gas rapid condensation system (7) and the condensible gas recycle system (8) not, it is characterized in that:
The outlet of hopper (1) is connected with the entrance of feed system (2), and the outlet of feed system (2) is connected with the side wall lower ends entrance of fluid bed fast pyrolysis reactor (3); Fluid bed fast pyrolysis reactor (3) bottom inlet is connected with the outlet of the condensible gas recycle system (8) not, and upper end outlet is connected with the import of gas solid separation system (4); The air outlet of gas solid separation system (4) is connected with the import of pyrolysis gas rapid condensation system (7); The outlet of pyrolysis gas rapid condensation system (7) is divided into two-way, and a road is directly collected as combustion gas and used, and another road is connected with the entrance of the condensible gas recycle system (8) not;
Described hot coke combustion heat-exchange system (5) comprises a plurality of cyclone firing interchanger; Described a plurality of cyclone firing interchanger are connected from top to bottom, this system is topmost cyclone firing interchanger first module (I), be followed successively by cyclone firing interchanger second unit (II) downwards, until cyclone firing interchanger most end unit (N), wherein, N is not less than 2 integer; The discharge gate of cyclone firing interchanger first module (I) is connected with the import of cyclone firing interchanger second unit (II), and the air outlet of cyclone firing interchanger second unit (II) is connected with the import of cyclone firing interchanger first module (I); The discharge gate of cyclone firing interchanger second unit (II) is connected with the import of cyclone firing interchanger the 3rd unit (III), the air outlet of cyclone firing interchanger the 3rd unit (III) is connected with the import of cyclone firing interchanger second unit (II), the like to cyclone firing interchanger most end unit (N); The import of cyclone firing interchanger first module (I) is also connected with the discharge gate of gas solid separation system (4), and the air outlet of cyclone firing interchanger first module (I) is connected with the import of whirlwind heat exchanger first module (i) in cold sand heating system (6); The discharge gate of cyclone firing interchanger most end unit (N) is connected with collection box, directly collects cold sand and ash, and the import of cyclone firing interchanger most end unit (N) is also connected with gas blower, directly air-supplied;
Described cold sand heating system (6) comprises a plurality of whirlwind heat exchangers; Described a plurality of whirlwind heat exchangers are connected from bottom to top, this system bottom is whirlwind heat exchanger first module (i), is upwards followed successively by whirlwind heat exchanger second unit (ii), until whirlwind heat exchanger most end unit (n), wherein, n is not less than 2 integer; The air outlet of whirlwind heat exchanger first module (i) is connected with the import of whirlwind heat exchanger second unit (ii), and the discharge port of whirlwind heat exchanger second unit (ii) is connected with the import of whirlwind heat exchanger first module (i); The air outlet of whirlwind heat exchanger second unit (ii) is connected with the import of whirlwind heat exchanger the 3rd unit (iii), the discharge port of whirlwind heat exchanger the 3rd unit (iii) is connected with the import of whirlwind heat exchanger second unit (ii), the like to whirlwind heat exchanger most end unit (n); The discharge port of whirlwind heat exchanger first module (i) is also connected with fluid bed fast pyrolysis reactor (3) side wall lower ends opening; The import of whirlwind heat exchanger most end unit (n) also with for sandbox is connected, and directly feeds cold sand, and the air outlet of whirlwind heat exchanger most end unit (n) directly communicates with atmosphere, and cold flue gas is entered to atmosphere.
2. the device of biomass fast pyrogenation preparing bio-oil according to claim 1, is characterized in that: described feed system (2) is two-stage screw feeder.
3. the device of biomass fast pyrogenation preparing bio-oil according to claim 1, is characterized in that: described fluid bed fast pyrolysis reactor (3) is fast fluidized bed reactor.
4. the device of biomass fast pyrogenation preparing bio-oil according to claim 1, is characterized in that: described gas solid separation system (4) is cyclonic separator.
5. the device of biomass fast pyrogenation preparing bio-oil according to claim 1, is characterized in that: described pyrolysis gas rapid condensation system (7) is spraying and falling liquid film composite condensation system.
6. a method for the biomass fast pyrogenation preparing bio-oil based on claim 1-5 any one device, is characterized in that having following steps:
Biomass material is sent into fluid bed fast pyrolysis reactor (3), take from not condensible gas that can not the condensing air recycle system (8) is fluidized carrier gas, since the hot sand of self cooling sand heating system (6) be thermal barrier, biomass under the effect of hot sand and fluidized carrier gas, rapid decomposes;
First high temperature pyrolysis product enters gas solid separation system (4) and realizes gas solid separation;
The solid that gas solid separation obtains enters hot coke combustion heat-exchange system (5), in multistage cyclone combustion heat-exchange device, the solid that gas solid separation obtains flows from top to bottom, freezing air flows from bottom to top, the solid that gas solid separation obtains passes through after burning and heat exchange, become cold ash and sand and discharge from cyclone firing interchanger most end unit (N), freezing air is first preheating and afterfire forms high-temperature flue gas; High-temperature flue gas enters in cold sand heating system (6), in multistage cyclone interchanger, high-temperature flue gas flows and transfers heat to cold sand from bottom to top, cold sand flows absorption heat from top to bottom and heats up, become hot sand, from whirlwind heat exchanger most end unit (n), discharge laggardly to enter fluidized-bed fast pyrolysis reactor (3);
Gas solid separation obtains high-temperature gas product, enter pyrolysis gas fast pyrogenation condenser system (7), after the composite condensation of spraying and falling liquid film, obtain liquid bio oil, condensible gas is not divided into two-way from outlet is flowed out, wherein a road is used as combustion gas after collecting, another Lu Zejing not condensible gas recycle system (8) sends into the bottom inlet of fluid bed fast pyrolysis reactor (3) after circulating, as fluidized carrier gas, use.
7. the method for biomass fast pyrogenation preparing bio-oil according to claim 6, is characterized in that: described biomass material is lignocellulose-like biomass.
8. the method for biomass fast pyrogenation preparing bio-oil according to claim 6, is characterized in that: the temperature of reaction in described fluid bed fast pyrolysis reactor (3) is 450-550 ℃, and gas residence time is 0.1～5s.
9. the method for biomass fast pyrogenation preparing bio-oil according to claim 6, is characterized in that: the coke in described hot coke combustion heat-exchange system (5) and the excess air ratio of air combustion are 1.0～1.3.
10. the method for biomass fast pyrogenation preparing bio-oil according to claim 6, is characterized in that: in described cold sand heating system (6), the temperature out of hot sand is 550～800 ℃.
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| CN106336885B (en) * | 2016-10-11 | 2018-09-07 | 天津科技大学 | The system that a kind of biomass fast activating or fast pyrogenation prepare activated carbon or bio oil |
| CN106701142B (en) * | 2017-01-24 | 2018-09-18 | 东南大学 | The device and method that fuel is produced in catalysis pyrolysis are blended in high and low effective hydrogen-carbon ratio raw material |
| CN108003903A (en) * | 2017-11-15 | 2018-05-08 | 安徽工程大学 | A kind of pyrolysis liquefaction device of Biomedia |
| CN112805084A (en) * | 2018-08-03 | 2021-05-14 | 美国能源系统网控股有限公司 | Biomass treatment apparatus, system, and method |
| CN109847657B (en) * | 2019-01-22 | 2020-08-14 | 华中科技大学 | Fused salt heat supply fluidized bed pyrolysis reaction furnace and reaction method |
| CN112210395A (en) * | 2020-09-16 | 2021-01-12 | 周文今 | Preparation method for preparing clean fuel, carbon powder and heat energy by using agricultural and forestry wastes |
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